Organic dielectric heat transfer fluids and processes

Abstract

The present applications pertains to heat transfer fluids and processes of employing them to, for example, cool electronic devices. In one embodiment, the heat transfer fluids include an alkylene carbonate and at least one organic solvent. Suitable organic solvents include, for example, an alkylene glycol or a glycol ether. The fluids typically are dielectric liquids with less than 30 weight percent of water. Advantageously, the fluids often have an effective beat capacity greater than water which is useful for cooling an electronic device such as a battery, a computer, a server, and the like.

Description

CROSS-REFERENCE TO RELATED APPLICATIONS

[0001] The instant application is a continuation of pending Ser. No. 19 / 055,975 filed on Feb. 18, 2025 which is a divisional of Ser. No. 18 / 487,702 filed on Oct. 16, 2023 issued as U.S. Pat. No. 12,228,344.

[0002] Ser. No. 18 / 487,702 is a divisional of U.S. patent application Ser. No. 17 / 166,658 filed on Feb. 3, 2021 now U.S. Pat. No. 11,788,798.

[0003] Ser. No. 17 / 166,658 is a continuation-in-part of U.S. application Ser. No. 16 / 826,469 filed Mar. 23, 2020 and issued as U.S. Pat. No. 10,948,224. Ser. No. 17 / 166,658 also claims priority to U.S. Provisional Application No. 62 / 969,211 filed Feb. 3, 2020 and U.S. Provisional Application No. 62 / 969,774 filed Feb. 4, 2020 and U.S. Provisional Application No. 63 / 030,966 filed May 28, 2020.

[0004] U.S. application Ser. No. 16 / 826,469 issued as U.S. Pat. No. 10,948,224 claims priority to U.S. provisional application No. 62 / 822,501 filed Mar. 22, 2019; 62 / 872,851 filed Jul. 11, 2019; 62 / 976,398 filed Feb. 14, 2020; 62 / 984,394 filed Mar. 3, 2020 and 62 / 988,999 filed Mar. 13, 2020.

[0005] The instant application is also a continuation of pending Ser. No. 18 / 527,918 filed Dec. 4, 2023 issued as U.S. Pat. No. 11,835,269. Ser. No. 18 / 527,918 claims priority from U.S. Provisional Application No. 63 / 529,453 filed Jul. 28, 2023 and U.S. Provisional Application No. 63 / 597,381 filed Nov. 9, 2023.

[0006] Ser. No. 18 / 527,918 was a continuation-in-part application of U.S. application Ser. No. 18 / 093,147 filed Jan. 4, 2023 issued as U.S. Pat. No. 11,835,269. U.S. Application No. 18,093,147 claimed priority to U.S. Provisional Application No. 63 / 296,336 filed Jan. 4, 2022.

[0007] U.S. Application No. 18,093,147 also claimed priority to U.S. application Ser. No. 17 / 166,700 filed Feb. 3, 2021 which is now U.S. Pat. No. 11,796,229. U.S. application Ser. No. 17 / 166,700 is a continuation-in-part of U.S. application Ser. No. 16 / 826,469 filed Mar. 23, 2020 which is now U.S. Pat. No. 10,948,224.

[0008] U.S. application Ser. No. 17 / 166,700 claims priority from U.S. Provisional Application No. 62 / 696,211 filed Feb. 3, 2020; 62 / 969,774 filed Feb. 4, 2020; 63 / 030,966 filed May 28, 2020; 63 / 064,290 filed Aug. 11, 2020. No. 62 / 822,501 filed Mar. 22, 2019; 62 / 872,851 filed Jul. 11, 2019; 62 / 976,398 filed Feb. 14, 2020; 62 / 984,394 filed Mar. 3, 2020; 62 / 988,999 filed Mar. 13, 2020.

[0009] U.S. Application No. 18,093,147 also claimed priority to pending U.S. application Ser. No. 17 / 008,165 filed Aug. 31, 2020 which is now U.S. Pat. No. 11,643,583. U.S. application Ser. No. 17 / 008,165 is a continuation of Ser. No. 16 / 580,962 filed Sep. 24, 2019 which is now U.S. Pat. No. 10,808,156. Ser. No. 16 / 580,962 is a continuation of Ser. No. 16 / 445,855 filed Jun. 19, 2019 which is now U.S. Pat. No. 10,472,550. Ser. No. 16 / 445,855 is a continuation of U.S. Ser. No. 16 / 258,384 filed Jan. 25, 2019 which is now U.S. Pat. No. 10,414,961. Ser. No. 16 / 258,384 claims priority to U.S. Provisional application No. 62 / 622,528 filed Jan. 26, 2018; 62 / 670,117 filed May 11, 2018; and 62 / 771,902 filed Nov. 27, 2018.

[0010] All of the aforementioned applications are incorporated herein by reference.

[0011] The present application employs the specification of U.S. application Ser. No. 16 / 826,469 filed Mar. 23, 2020 and issued as U.S. Pat. No. 10,948,224 although all the above applications are incorporated herein by reference.BACKGROUND AND SUMMARY

[0012] The present invention pertains to cooling, heating, and refrigeration cycles. The present invention pertains to refrigeration cycles employing liquid-liquid phase transitions to pump heat or transfer heat or a combination thereof. Embodiments of the present invention may comprise systems, methods, or processes for liquid-liquid phase transition refrigeration cycles pumping heat across temperature differences greater than the adiabatic temperature change of a liquid-liquid phase transition within said liquid-liquid phase transition refrigeration cycle. Embodiments of the present invention may comprise powering said liquid-liquid phase transition refrigeration cycle using electricity, heat, ‘cold’, the mixing of a saltwater and freshwater, the mixing of high osmotic pressure liquid and low osmotic pressure liquid, or a combination thereof. Embodiments of the present invention may comprise the integration or application or incorporation of said liquid-liquid phase transition refrigeration cycle in a gas separation process to facilitate gas separation, or increase energetic efficiency of gas separation, or reduce OPEX or reduce CAPEX, or a combination thereof. Embodiments of the present invention may involve adjustment of phase transition temperature or initiating liquid-liquid phase transitions in liquid-liquid phase transition refrigeration cycles and heat transfer.BRIEF DESCRIPTION OF THE FIGURES

[0013] FIG. 1: FIG. 1 may comprise a liquid phase refrigeration cycle with temperature zones with liquid-liquid phase transitions occurring in Heat Exchanger #1 and Heat Exchanger #3.

[0014] FIG. 2: FIG. 1 may comprise a liquid phase refrigeration cycle with temperature zones with liquid-liquid phase transitions occurring before Heat Exchanger #1 and Heat Exchanger #3.

[0015] FIG. 3A: FIG. 3A may comprise a liquid phase refrigeration cycle with temperature zones with liquid-liquid phase transitions occurring before Heat Exchanger #1 and Heat Exchanger #3.

[0016] FIG. 3B: FIG. 3B may comprise a liquid phase refrigeration cycle with temperature zones with example temperature labels representative of example temperatures of each liquid stream during an example instance of operation.

[0017] FIG. 4: FIG. 4 may comprise a liquid phase refrigeration cycle with temperature zones wherein concentration adjustment using a membrane occurs after Heat Exchanger #2.

[0018] FIG. 5: FIG. 5 may comprise a liquid phase refrigeration cycle with temperature zones wherein concentration adjustment using a membrane occurs after Heat Exchanger #2.

[0019] FIG. 6: FIG. 6 may comprise a liquid phase refrigeration cycle with temperature zones wherein concentration adjustment using a membrane occurs after Heat Exchanger #2 and may involve rejecting or releasing at least a portion of heat using evaporative cooling or wet surface contactor or a combination thereof.

[0020] FIG. 7: FIG. 7 may comprise a liquid phase refrigeration cycle with temperature zones wherein concentration adjustment using a membrane occurs after Heat Exchanger #2 and may involve rejecting or releasing at least a portion of heat using evaporative cooling or wet surface contactor or a combination thereof.

[0021] FIG. 8: FIG. 8 may comprise a liquid phase refrigeration cycle with temperature zones wherein concentration adjustment using a membrane occurs after Heat Exchanger #2.

[0022] FIG. 9: FIG. 9 may comprise a liquid phase refrigeration cycle wherein solvent may be added and removed to drive liquid-liquid phase transitions to ‘pump’ heat, and wherein solvent removal may be conducted using forward osmosis and / or powered by heat or ‘cold’.

[0023] FIG. 10: FIG. 10 may be the same as FIG. 9, except further comprises a step for separating residual organic Composition #2 or other residual reagents in the regeneration portion from the regenerated solvent before adding said regenerated solvent to the refrigeration cycle portion.

[0024] FIG. 11: FIG. 11 may comprise a liquid phase refrigeration cycle with temperature zones, and / or forward osmosis, and / or forward osmosis regenerated / powered by heat or ‘cold’.

[0025] FIG. 12: FIG. 12 may be the same as FIG. 11, except further comprises a step for separating residual organic Composition #2 or other residual reagents in the regeneration portion from the regenerated solvent before adding said regenerated solvent to the refrigeration cycle portion.

[0026] FIG. 13: FIG. 13 may be the same as FIG. 9 or FIG. 10, except may further comprise adding the added solvent by employing organic Composition #1 as a draw solution in a forward osmosis or osmotically assisted reverse osmosis step.

[0027] FIG. 14: FIG. 14 may comprise a liquid phase refrigeration cycle adjusting a concentration using forward osmosis and / or powered by the osmotic pressure difference of a low or lesser osmotic pressure solution and a high or greater osmotic pressure solution.

[0028] FIG. 15: FIG. 15 may be the same as FIG. 14, except the added solvent added to the refrigeration cycle may comprise reagents other than water or reagents in addition to water.

[0029] FIG. 16: FIG. 16 may be the same as FIG. 14 or FIG. 15, except may further comprise adding the added solvent by employing organic Composition #1 as a draw solution in a forward osmosis or osmotically assisted reverse osmosis step.

[0030] FIG. 17: FIG. 17 may comprise a liquid phase refrigeration cycle with temperature zones powered by the mixing or indirect mixing of a low or lesser osmotic pressure solution and a high or greater osmotic pressure solution and / or employing forward osmosis for adjusting a concentration of a reagent.

[0031] FIG. 18: FIG. 18 may be the same as FIG. 12, except employ a UCST based liquid-liquid phase transition regeneration in the Regeneration Portion.

[0032] FIG. 19: FIG. 19 may be the same as FIG. 12, except employ a UCST based liquid-liquid phase transition in the Refrigeration Cycle Portion.

[0033] FIG. 20: FIG. 20 may be the same as FIG. 12, except employ a UCST based liquid-liquid phase transition in the Refrigeration Cycle Portion and Regeneration Portion.

[0034] FIG. 21: FIG. 21 be the same as FIG. 16, except shows Liquid A undergoing a treatment step (RO) before Liquid A is added to the process.

[0035] FIG. 22: FIG. 22 be the same as FIG. 17, except shows Liquid A undergoing a treatment step (RO) before Liquid A is added to the process.

[0036] FIG. 23: FIG. 23 shows a liquid phase only refrigeration cycle functioning as a secondary refrigeration cycle and / or heat transfer liquid connected to a conventional vapor compression refrigeration cycle chiller

[0037] FIG. 24: Same as FIG. 23, except with example stream temperatures shown.

[0038] FIG. 25: A figure of a chilled water loop provided for reference to show the significantly greater temperature internal difference required to achieve the same resulting temperatures as FIG. 24.

[0039] FIG. 26: Embodiment with Liquid-Liquid Separation of Multi-Liquid Phase Mixture of Excess or Spillover Liquid (which may be produced due to reagents added for, for example, phase transition temperature adjustment) and Batch Reagent Regeneration.

[0040] FIG. 27: Embodiment with Batch Based Regeneration of Excess or Spillover Liquid

[0041] FIG. 28: Heat Transfer and / or Refrigeration Cycle Embodiment with Liquid-Liquid Separation of, for example, Excess Liquid or Spillover, and Distillation Based Regeneration of Phase Transition Temperature Adjustment Reagents or Compositions

[0042] FIG. 29: Heat Transfer and / or Refrigeration Cycle Embodiment with Excess Liquid or Spillover and Distillation Based Regeneration of Phase Transition Temperature Adjustment Reagents or Compositions

[0043] FIG. 30: Heat Transfer and / or Refrigeration Cycle Embodiment with Liquid-Liquid Separation of, for example, Excess Liquid or Spillover and Membrane Based Regeneration of Phase Transition Temperature Adjustment Reagents or Compositions

[0044] FIG. 31: Heat Transfer and / or Refrigeration Cycle Embodiment with Excess Liquid or Spillover and Membrane Based Regeneration of Phase Transition Temperature Adjustment Reagents or Compositions

[0045] FIG. 32A: Heat Transfer and / or Refrigeration Cycle Embodiment with Pressure Based Phase Transition Temperature Adjustment. 32A shows constant pressure operation.

[0046] FIG. 32B: Heat Transfer and / or Refrigeration Cycle Embodiment with Pressure Based Phase Transition Temperature Adjustment. 32B shows system pressurizing.

[0047] FIG. 32C: Heat Transfer and / or Refrigeration Cycle Embodiment with Pressure Based Phase Transition Temperature Adjustment. 32C shows system depressurizing.

[0048] FIG. 33: FIG. 33 may show an example simplified liquid-liquid refrigeration cycle based chiller.

[0049] FIG. 34: Gas separation embodiment with liquid-liquid phase transition internal heat pump and / or organic solvent nanofiltration or other concentration adjustment or membrane-based process before a cross heat exchanger.

[0050] FIG. 35: Gas separation embodiment with liquid-liquid phase transition internal heat pump and / or organic solvent nanofiltration or other concentration adjustment or membrane-based process after a cross heat exchanger.

[0051] FIG. 36: Gas separation embodiment with liquid-liquid phase transition internal heat pump where the organic phase and the aqueous phase are in a biphasic or multi-liquid phase mixture before, during, or after, or a combination thereof absorption.

[0052] FIG. 37: Liquid-liquid phase transition heat pump gas separation embodiment where liquid-liquid phase change may occur in the absorber and may be in part triggered or facilitated by or driven by heat released and / or solubility changes due to the increased concentration of one or more gases or gas derivatives in solution.

[0053] FIG. 38: Liquid-liquid phase transition heat pump gas separation embodiment wherein a combined single liquid phase solution is employed throughout gas absorption.

[0054] FIG. 39: A gas separation embodiment wherein the desired gases may primarily concentrate in an organic phase during the formation of a multi-liquid phase mixture or biphasic mixture and / or may condense into a liquid phase output or a combination thereof.

[0055] FIG. 40: Liquid-liquid phase transition heat pump gas separation embodiment configured to separate condensable gases, or highly soluble gases, or gases which can be separated with physical solvents, or a combination thereof.

[0056] FIG. 41: Liquid-liquid phase transition heat pump gas separation embodiment configured to separate condensable gases, or highly soluble gases, or gases which can be separated with physical solvents, or a combination thereof.

[0057] FIG. 42: A liquid-liquid phase transition gas separation embodiment employing distillation or desorption to separate desired gas or regenerate the gas separation solution or a combination thereof.

[0058] FIG. 43: Example gas separation embodiment step-by-step description flowchart for FIG. 34.DETAILED DESCRIPTION OF THE INVENTIONExample Definitions

[0059] Single Liquid Phase Solution, or Combined Single Liquid Phase Solution, or Single Liquid Phase Combined Solution:

[0060] A solution which may have originated from two separate liquid phases or liquid streams

[0061] Wherein said Single Liquid Phase Solution, or Combined Single Liquid Phase Solution, or Single Liquid Phase Combined Solution comprises the solution resulting from the dissolution of said two liquid streams in each other

[0062] Wherein one of said two liquid streams may comprise mostly water

[0063] Wherein one of said two liquid streams may comprise mostly organic

[0064] Wherein said Single Liquid Phase Solution, or Combined Single Liquid Phase Solution, or Single Liquid Phase Combined Solution comprises the solution resulting from said liquid stream comprising mostly water dissolving in said liquid stream comprising mostly organic

[0065] Wherein said Single Liquid Phase Solution, or Combined Single Liquid Phase Solution, or Single Liquid Phase Combined Solution comprises the solution resulting from said liquid stream comprising mostly organic dissolving in said liquid stream comprising mostly water

[0066] A solution which resulted from an exothermic liquid-liquid phase transition, wherein said exothermic phase transition comprises the dissolution of a first liquid phase into a second liquid phase

[0067] Wherein said dissolution comprises at least 99% of said first liquid phase dissolving into said second liquid phase

[0068] Wherein said dissolution comprises at least 95% of said first liquid phase dissolving into said second liquid phase

[0069] Wherein said dissolution comprises at least 90% of said first liquid phase dissolving into said second liquid phase

[0070] Wherein said dissolution comprises at least 80% of said first liquid phase dissolving into said second liquid phase

[0071] Wherein said dissolution comprises at least 70% of said first liquid phase dissolving into said second liquid phase

[0072] Wherein said dissolution comprises at least 60% of said first liquid phase dissolving into said second liquid phase

[0073] Wherein said dissolution comprises at least 50% of said first liquid phase dissolving into said second liquid phase

[0074] Wherein said dissolution comprises at least 40% of said first liquid phase dissolving into said second liquid phase

[0075] Wherein said dissolution comprises at least 30% of said first liquid phase dissolving into said second liquid phase

[0076] Wherein said dissolution comprises at least 20% of said first liquid phase dissolving into said second liquid phase

[0077] Wherein said dissolution comprises at least 10% of said first liquid phase dissolving into said second liquid phase

[0078] A solution which resulted from an endothermic liquid-liquid phase transition, wherein said endothermic phase transition comprises the dissolution of a first liquid phase into a second liquid phase

[0079] Wherein said dissolution comprises at least 99% of said first liquid phase dissolving into said second liquid phase

[0080] Wherein said dissolution comprises at least 95% of said first liquid phase dissolving into said second liquid phase

[0081] Wherein said dissolution comprises at least 90% of said first liquid phase dissolving into said second liquid phase

[0082] Wherein said dissolution comprises at least 80% of said first liquid phase dissolving into said second liquid phase

[0083] Wherein said dissolution comprises at least 70% of said first liquid phase dissolving into said second liquid phase

[0084] Wherein said dissolution comprises at least 60% of said first liquid phase dissolving into said second liquid phase

[0085] Wherein said dissolution comprises at least 50% of said first liquid phase dissolving into said second liquid phase

[0086] Wherein said dissolution comprises at least 40% of said first liquid phase dissolving into said second liquid phase

[0087] Wherein said dissolution comprises at least 30% of said first liquid phase dissolving into said second liquid phase

[0088] Wherein said dissolution comprises at least 20% of said first liquid phase dissolving into said second liquid phase

[0089] Wherein said dissolution comprises at least 10% of said first liquid phase dissolving into said second liquid phase

[0090] Adiabatic Temperature Change or Adiabatic Temperature Difference:

[0091] Comprises the change in temperature of a liquid-liquid phase transitioning composition if a liquid-liquid phase transition occurs in an adiabatic environment or a container where no heat enters or exits. The adiabatic temperature change may be the change in temperature of a liquid-liquid phase transitioning solution due to an enthalpy of phase transition in an insulated container or environment.

[0092] In practical terms, the adiabatic temperature change may be calculated by dividing the enthalpy of phase transition of a liquid-liquid phase transition (ΔH_((L-L))) by the baseline specific heat capacity (C_p).Adiabatic⁢ Temperature⁢ Change=Δ⁢H(L-L)÷CpFor example, if the total enthalpy of phase transition is 27 kJ / kg and the baseline specific heat capacity of a total liquid is 3.6 J / g° C., then the adiabatic temperature change is 7.5° C. or 7.5° KIf the liquid-liquid phase transition is undergoing an exothermic liquid-liquid phase transition, the adiabatic temperature change is known as an adiabatic temperature rise

[0095] If the liquid-liquid phase transition is undergoing an endothermic liquid-liquid phase transition, the adiabatic temperature change is known as an adiabatic temperature dropBaseline Specific Heat Capacity:Specific heat capacity of a liquid under conditions where no liquid-liquid phase transition is occurring, and / or no other phase transitions or reactions are occurringOperatively Connected or Operably Connected or LinkedMay involve two or more process operations where mass is transferred or exchanged between the two or more process operations.For example, in the instance of temperature zones, liquids are transferred between temperature zones.

[0099] For example, at least a portion of mass of liquids may be transferred from one temperature zone to another temperature zones. Liquid mass entering a temperature zone may be heat exchanged with liquid mass exiting said temperature zone.

[0100] For example, liquids may be transferred from one temperature zone to another temperature zone.

[0101] The concentration of a reagent in said liquids may be adjusted in one or more of said temperature zones. The concentration of a reagent in one temperature zone or a portion of one temperature zone may be different than the concentration of said reagent in another operatively connected temperature zone. Although the concentration of a reagent may be adjusted in a temperature zone, at least a portion of liquid mass in both temperature zones is exchanged or transferred between temperature zones (for example: liquid mass in a first temperature zone is transferred to a second temperature zone and liquid mass in a second temperature zone is transferred to a first temperature zone).OrganicOrganic may comprise a reagent which comprises more than 40% or more than 50% reagents or a reagent which is a non-water reagent. A non-water reagent comprises a reagent which is not water.

[0103] In the context of a liquid phase or ‘an organic liquid phase’ or ‘mostly organic phase’, organic may comprise a liquid phase with a greater concentration of a non-water reagent than another liquid phase used for comparison. Said ‘another liquid phase used for comparison’ may comprise a liquid phase which contains reagents which were previously dissolved in or dissolved with or in the same solution as said organic liquid phase before a liquid-liquid phase transition. Said ‘another liquid phase used for comparison’ may comprise a greater concentration of water than said organic phase. Said ‘another liquid phase used for comparison’ may comprise a greater concentration of salt or phase transition adjustment reagent than said organic phase. Organic phase may be insoluble or possess limited solubility in said ‘another liquid phase used for comparison’. Organic phase may be soluble or possess greater solubility in said ‘another liquid phase used for comparison’ if said ‘another liquid phase used for comparison’ possessed a lesser concentration of salt or phase transition temperature adjustment reagent. Alternatively or additionally, organic phase may be soluble or possess greater solubility in said ‘another liquid phase used for comparison’ if said organic phase possessed a lesser concentration of salt or phase transition temperature adjustment reagent.

[0104] A reagent which may possess liquid-liquid phase transition properties or exhibit a liquid-liquid phase transition temperature range or both in a solution comprising water.

[0105] May also be described as Organic phase, or Non-Aqueous, or Non-Aqueous Phase, or Non-Water Reagent, phase transition reagents rich phase or organic-rich phaseDiluted Salt Solution or Phase Transition Temperature Adjustment Reagent Solution:May comprise a solution which originated from the dissolution of a salt or phase transition temperature adjustment reagent or the dissolution of a concentrated solution of salt or phase transition temperature adjustment reagent in a solution without or with a lesser concentration of a salt or phase transition temperature adjustment reagent.

[0107] May comprise a solution which possesses a sufficient concentration of a salt or phase transition temperature adjustment reagent for an organic liquid phase to be insoluble or possess limited solubility in said solution and / or to enable the formation of a separate organic liquid phase.

[0108] A solution comprising ‘another liquid phase used for comparison’ (as described in the definition of ‘Organic’).Heat Exchanger Delta T:In a counterflow heat exchanger, the temperature difference between a ‘cold’ input stream and a ‘cooled’ output stream

[0110] In a counterflow heat exchanger, the temperature difference between a ‘warm’ input stream and a ‘warmed’ or ‘heated’ output stream

[0111] In a parallel heat exchanger, the temperature difference between a heated output stream and cooled output streamReagent:May comprise a single chemical or a composition comprising multiple chemicals or a combination thereofDraw Solution Reagent:A reagent which functions as a draw solution in a forward osmosis or osmotically assisted reverse osmosis or a combination thereof processA reagent which may be different from the liquid-liquid phase transitioning reagents within a liquid phase refrigeration cycle and may be employed as a draw solution to regenerate or concentrate a reagent within the refrigeration cycle using forward osmosisLiquid-Liquid Phase Transition Temperature Range:The temperature range which a composition transitions from a single liquid phase to multiple liquid phases or from multiple liquid phases to a single liquid phaseA temperature range wherein a composition exhibits heat absorbing or heat releasing characteristics (endothermic or exothermic phase transitions) beyond the baseline specific heat capacity of the composition

[0117] An intrinsic property of a liquid composition

[0118] A temperature range wherein two liquid phases exists

[0119] A temperature range wherein a single liquid phase exists

[0120] A temperature range wherein the number of or relative volume of or relative composition of or a combination thereof of liquid phases changes when heat is added or removed from a composition. Wherein said composition comprises said liquid phasesLiquid-Liquid Phase Transition:When the number of or relative volume of or relative composition of or a combination thereof of liquid phases changes in a liquid composition or liquid mixture. Wherein said composition or mixture comprises a liquid phases or multiple liquid phases.

[0122] When a liquid composition exhibits heat absorbing or heat releasing characteristics (endothermic or exothermic phase transitions) beyond the baseline specific heat capacity of the composition while remaining a liquid phase. It may exclude heat absorbing or releasing phenomena due to solid-liquid, gas-liquid, gas-gas, liquid-gas, and / or liquid-solid phase transition.

[0123] When a liquid composition transitions from a single liquid phase to multiple liquid phases or from multiple liquid phases to a single liquid phase.Temperature Zone Refrigeration Cycle with Pressurized Membrane Regeneration Summary of Embodiments:

[0124] The present invention comprises a refrigeration cycle employing liquid-liquid phase transitions. The present invention may involve reversible endothermic and exothermic phase transitions which are facilitated or engineered to occur at different temperatures. Advantageously, some embodiments described herein may enable the refrigeration cycle to generate a temperature difference greater than the adiabatic temperature rise (or fall) of an enthalpy of phase transition of the liquid-liquid phase transitioning liquid.

[0125] Some embodiments of the present invention may involve employing heat exchanging to create two separate temperature zones. Said temperature zones may involve a ‘warm temperature zone’ and a ‘cold temperature zone’. Said ‘warm temperature zone’ (or second temperature zone) may involve releasing heat and said ‘cold temperature zone’ (or first temperature zone) may involve absorbing heating. Said heat exchanging may involve heat exchanging ‘cold’ solutions from the cold temperature zone entering the warm temperature zone with ‘warm’ solutions from the warm temperature zone entering the cold temperature zone. Said heat exchanging may enable a liquid phase refrigeration cycle which possesses a temperature difference greater than the adiabatic temperature change of an enthalpy of liquid-liquid phase transition. It may be desirable for phase transition temperature adjustment or solubility adjustment or concentration adjustment or composition adjustment or a combination thereof to enable an endothermic phase transition to occur in the cold temperature zone and an exothermic phase transition to occur in the warm temperature zone. It may be desirable for said phase transition temperature adjustments, system solutions, or a combination thereof to be reversible or reversed within the process. The temperature difference which can be generated in some embodiments may be dependent on the greatest temperature of an adjusted exothermic liquid-liquid phase transition and the greatest temperature of an adjusted endothermic liquid-liquid phase transition within a system.Figure Summaries:

[0126] FIG. 1: FIG. 1 may comprise a liquid phase refrigeration cycle. FIG. 1 may possess a LCST or an UCST liquid-liquid phase transition or reagents which possess liquid-liquid phase transitions when the concentration of one or more reagents are adjusted or a combination thereof. FIG. 1 may involve heat exchanging such that it possesses a ‘warm temperature zone’ and a ‘cold temperature zone’. FIG. 1 may possess liquid-liquid phase transitions which occur during heat exchanging with one or more applications requiring cooling or heating and / or after phase transition temperature adjustment.

[0127] FIG. 2: FIG. 2 may comprise a liquid phase refrigeration cycle. FIG. 2 may possess a LCST or an UCST liquid-liquid phase transition or reagents which possess liquid-liquid phase transitions when the concentration of one or more reagents are adjusted or a combination thereof. FIG. 2 may involve heat exchanging such that it possesses a ‘warm temperature zone’ and a ‘cold temperature zone’. FIG. 2 may possess liquid-liquid phase transitions which occur before or during heat exchanging with one or more applications requiring cooling or heating and / or before or during phase transition temperature adjustment.

[0128] FIG. 3: FIG. 3 may comprise a liquid phase refrigeration cycle. FIG. 3 may possess a LCST or an UCST liquid-liquid phase transition or reagents which possess liquid-liquid phase transitions when the concentration of one or more reagents are adjusted or a combination thereof. FIG. 3 may involve heat exchanging such that it possesses a ‘warm temperature zone’ and a ‘cold temperature zone’. FIG. 3 may possess liquid-liquid phase transitions which occur before or during heat exchanging with one or more applications requiring cooling or heating and / or before or during phase transition temperature adjustment. FIG. 3 may show example temperatures for each stream in an example embodiment of the present invention.

[0129] FIG. 4: FIG. 4 may comprise a liquid phase refrigeration cycle. FIG. 4 may possess a LCST or an UCST liquid-liquid phase transition or reagents which possess liquid-liquid phase transitions when the concentration of one or more reagents are adjusted or a combination thereof. FIG. 1 may involve heat exchanging such that it possesses a ‘warm temperature zone’ and a ‘cold temperature zone’. FIG. 4 may possess liquid-liquid phase transitions which occur during heat exchanging with one or more applications requiring cooling or heating and / or after phase transition temperature adjustment. FIG. 4 may possess phase transition temperature adjustment and / or concentration adjustment in a different temperature zone than FIG. 3.

[0130] FIG. 5: FIG. 5 may comprise a liquid phase refrigeration cycle. FIG. 5 may possess a LCST or an UCST liquid-liquid phase transition or reagents which possess liquid-liquid phase transitions when the concentration of one or more reagents are adjusted or a combination thereof. FIG. 5 may involve heat exchanging such that it possesses a ‘warm temperature zone’ and a ‘cold temperature zone’. FIG. 5 may possess liquid-liquid phase transitions which occur before or during heat exchanging with one or more applications requiring cooling or heating and / or before or during phase transition temperature adjustment. FIG. 5 may possess phase transition temperature adjustment and / or concentration adjustment in a different temperature zone than FIG. 3.

[0131] FIG. 6: FIG. 6 may comprise a liquid phase refrigeration cycle. FIG. 6 may possess a LCST or an UCST liquid-liquid phase transition or reagents which possess liquid-liquid phase transitions when the concentration of one or more reagents are adjusted or a combination thereof. FIG. 6 may involve heat exchanging such that it possesses a ‘warm temperature zone’ and a ‘cold temperature zone’. FIG. 6 may possess liquid-liquid phase transitions which occur before or during heat exchanging with one or more applications requiring cooling or heating and / or before or during phase transition temperature adjustment. FIG. 6 may involve rejecting or releasing at least a portion of heat using evaporative cooling or wet surface contactor or a combination thereof. For example, FIG. 6 may involve direct evaporative cooling of a mostly freshwater stream within the process to, for example, facilitate cooling and minimize heat exchanger Delta-T. A cooling tower or evaporative cooling contactor may be configured to minimize biofouling or loss of reagents, which may include, but is not limited to, for example, using a gas-liquid or air-liquid membrane contactor. Evaporated water may be replenished with makeup water or makeup liquid water.

[0132] FIG. 7: FIG. 7 may comprise a liquid phase refrigeration cycle. FIG. 7 may possess a LCST or an UCST liquid-liquid phase transition or reagents which possess liquid-liquid phase transitions when the concentration of one or more reagents are adjusted or a combination thereof. FIG. 7 may involve heat exchanging such that it possesses a ‘warm temperature zone’ and a ‘cold temperature zone’. FIG. 7 may possess liquid-liquid phase transitions which occur before or during heat exchanging with one or more applications requiring cooling or heating and / or before or during phase transition temperature adjustment. FIG. 7 may involve rejecting or releasing at least a portion of heat using evaporative cooling or wet surface contactor or a combination thereof. For example, FIG. 7 may involve direct evaporative cooling of a mostly organic stream which may contain a portion of water to, for example, facilitate cooling and minimize heat exchanger Delta-T. A cooling tower or evaporative cooling contactor may be configured to minimize biofouling or minimize loss of reagents or both, which may include, but is not limited to, for example, using a gas-liquid or air-liquid membrane contactor. Evaporated water may be replenished with makeup water or makeup liquid water.

[0133] FIG. 8: FIG. 8 is the same as FIG. 5, except shows L-4 heat exchanging in Heat Exchanger #2.Definitions

[0134] Single Liquid Phase Combined Solution: May comprise a solution of organic liquid-liquid phase transition reagent(s) dissolved in water or other solvent.

[0135] Multi-Liquid Phase Mixture: May comprise a mixture of liquid phases. May comprise a mixture of liquid phases, wherein at least one liquid phase comprises mostly organic, and / or at least one liquid phase comprises mostly water or aqueous solution or solvent.Temperature Zones:Cold Temperature Zone: A temperature zone which may at a lesser temperature than another portion of a process and may exhibit an endothermic phase transition.

[0137] Warm Temperature Zone: A temperature zone which may at a greater temperature than another portion of a process and may exhibit an exothermic phase transition.

[0138] LCST: May involve a liquid composition which undergoes an exothermic phase transition when transforming from two liquid phases to a single liquid phase and an endothermic phase transition when transforming from a single liquid phase to two liquid phases.

[0139] UCST: May involve a liquid composition which undergoes an exothermic phase transition when transforming from a single liquid phase to two liquid phases and an endothermic phase transition when transforming from two liquid phases to a single liquid phase.

[0140] ‘Salting-Out’ Reagent or Phase Transition Temperature Adjustment Reagent: May comprise a salt or an organic or a combination thereof. May also be described as phase transition temperature adjustment reagent or reagent with high affinity for water relative to the organic phase

[0141] Example desirable properties of salts may include, but are not limited to, one or more or a combination of the following:

[0142] Capability to reduce phase transition temperature or salt out Organic with minimal salt concentration or osmotic pressure.

[0143] Insoluble or minimally soluble or only partial solubility or a combination thereof in organic liquid phase.

[0144] Ratio of phase transition temperature adjustment relative to salt concentration or osmotic pressure of salt in solution

[0145] Enthalpy of phase transition of organic when a liquid-liquid phase transition is driven by ‘salting out’ or phase transition temperature adjustment

[0146] Concentration of residual organic in an aqueous phase after liquid-liquid phase transition or ‘salting-out’ into a multi-liquid phase mixture

[0147] Chemical compatibility with other reagents and / or materials and / or equipment in the process

[0148] Example desirable properties of phase transition temperature adjustment or ‘salting-out’ organics may include

[0149] Capability to reduce phase transition temperature or salt out a liquid-liquid phase transitioning organic with minimal salt concentration or osmotic pressure.

[0150] Insoluble or minimally soluble or only partial solubility or a combination thereof in a liquid-liquid phase transitioning organic

[0151] If the concentration adjustment involves adjusting the concentration within an organic phase—greater solubility in or affinity to a liquid-liquid phase transitioning phase than an aqueous or solvent phase.

[0152] Ratio of phase transition temperature adjustment relative to phase transition temperature adjustment or ‘salting-out’ organic concentration or osmotic pressure of said phase transition temperature adjustment or ‘salting-out’ organic in solution

[0153] Enthalpy of phase transition of liquid-liquid phase transitioning organic when a liquid-liquid phase transition is driven by ‘salting out’ or phase transition temperature adjustment

[0154] Concentration of residual phase transition organic in an aqueous liquid phase after ‘salting out’

[0155] Chemical compatibility with other reagents and / or materials and / or equipment in the process.Example Step-by-Step DescriptionsFIG. 2:1—Mixing Reagents to Form Endothermic Phase Transition: A solution comprising mostly single liquid phase combined solution (L-2) may be mixed with a solution concentrated in ‘salting-out’ reagent or phase transition temperature adjustment reagent (L-4) in a mixing device (Mix #2). Said mixing of L-4 and L-2 may result in an endothermic liquid-liquid phase transition into a multi-liquid phase mixture. L-4 may dissolve in the aqueous component of L-2, which may result in at least an organic reagent becoming at least partially insoluble and / or forming a separate liquid phase in a liquid-liquid phase transition. A resulting multi-liquid phase mixture (LL-1) may comprise a mostly organic liquid phase and a mostly aqueous dilute ‘salting-out’ reagent or mostly phase transition temperature adjustment reagent liquid phase. The previously described liquid-liquid phase transition may be endothermic and may result in the temperature of LL-1 being less than the mean temperature of L-2 and L-4. In some embodiments, step 1 and step 2 may be combined. For example, in some embodiments, Mix #2 may be combined with Heat Exchanger #1.

[0157] 2—Heat Absorbing Heat Exchange: LL-1 may be heat exchanged (Heat Exchanger #1) with a heat source or an application requiring cooling or an enthalpy source or a combination thereof. LL-1 may absorb heat from or ‘cool’ said heat source or an application requiring cooling or an enthalpy source or a combination thereof, while said heat source or an application requiring cooling or an enthalpy source or a combination thereof may be cooled or supply heat to LL-1. Depending on the liquid state of LL-1, the temperature of LL-1, the temperature of Heat Exchanger #1, and phase transition properties of LL-1, LL-1 may absorb heat in Heat Exchanger #1 due to an enthalpy of liquid-liquid phase transition, or specific heat capacity due to an enthalpy of phase transition, or specific heat capacity or a combination thereof. LL-1 may exit Heat Exchanger #1 at a greater enthalpy or temperature or a combination thereof state and / or may comprise at least a portion a multi-liquid phase solution (LL-2).

[0158] 3—Liquid-Liquid Separation: LL-2 may be separated into two separate liquid streams using a liquid-liquid separation device (LLS-1). One of the two liquid phases may comprise a mostly organic liquid phase (L-8 and L-9). One of the liquid phases may comprise mostly aqueous dilute ‘salting-out’ reagent or mostly phase transition temperature adjustment reagent solution (L-5).

[0159] 4—Membrane Based Concentrating: Mostly aqueous dilute ‘salting-out’ reagent or mostly phase transition temperature adjustment reagent solution (L-5) may be pumped (P-1) and fed (L-6) into a reverse osmosis or nanofiltration or ultrafiltration or a combination thereof system (Reverse Osmosis). A portion of water or other permeable solvent in L-6 may permeate across a semi-permeable membrane, while ‘salting-out’ reagent or phase transition temperature adjustment reagent in L-6 may be rejected by said membrane. Reverse Osmosis may concentrate L-6 into a retentate solution comprising a concentrated solution of salting-out’ reagent or phase transition temperature adjustment reagent (L-3 and L-4) and form a permeate comprising water or other solvent or a combination thereof (L-7).

[0160] 5—Heat Exchange to Heat L-7 and L-9 into ‘Warm’ Temperature Zone: ‘Cold’ liquid phase comprising mostly organic (L-9) and a ‘cold’ liquid phase comprising mostly water or other solvent (L-7) may be heat exchanged (Heat Exchanger #2) with ‘warm’ mostly single liquid phase combined solution (L-1), which may result in ‘warm’ L-7 (L-10) and warm L-9 (L-11) and ‘cold’ L-1 (L-2). L-7 and L-9 may be non-contiguously separate liquid streams during Heat Exchanger #2 to, for example, prevent dissolution of L-7 into L-9 before or during Heat Exchanger #2.

[0161] 6—Mixing Reagents to Form Exothermic Phase Transition: L-10 may be mixed with L-11 in a mixing device, Mix #1, forming L-12. Depending on the liquid-liquid phase transition temperature range, the temperature of L-10 and L-11, and the enthalpy of the liquid-liquid phase transition, L-12 may comprise a multi-liquid phase mixture, or a multi-liquid phase mixture with some L-10 dissolved in L-11, or a single liquid phase combined solution.

[0162] 7—Heat Releasing Heat Exchange: L-12 may be heat exchanged with an application requiring heating, a heat sink, or a combination thereof using a heat exchanger (Heat Exchanger #3). L-12 may release heat to said application requiring heating, a heat sink, or a combination thereof, while said application requiring heating, a heat sink, or a combination thereof may cool L-12. Depending on the liquid state of L-12, the temperature of L-12, the temperature of the Heat Exchanger #3, and the phase transition properties of L-12, L-12 may release heat in the Heat Exchanger #3 due to an enthalpy of liquid-liquid phase transition, or specific heat capacity due to an enthalpy of phase transition, or specific heat capacity or a combination thereof. L-12 may exit Heat Exchanger #3 at a lower enthalpy or temperature or a combination thereof state and may comprise at least a portion a single liquid phase combined solution (L-1).

[0163] 8—Heat Exchange to ‘Cool’ L-1 into ‘Cold’ Temperature one: ‘Warm’ mostly single liquid phase combined solution (L-1) may be heat exchanged (Heat Exchanger #2) with a ‘cold’ liquid phase comprising mostly organic (L-9) and a ‘cold’ liquid phase comprising mostly water or other solvent (L-7), which may result in ‘warm’ L-9 (L-11) and warm L-7 (L-10) and ‘cold’ L-1 (L-2). L-7 and L-9 may be non-contiguously separate liquid streams during Heat Exchanger #2 to, for example, prevent dissolution of L-7 into L-9 before or during Heat Exchanger #2.Figure KeysExample Figure Key for FIG. 2Label inFIG.DescriptionL-1L-1 may comprise a solution comprising a combined solution of an organicand aqueous reagents. L-1 may comprise at least a portion a single liquidphase combined solution. L-1 may comprise L-12, except after heat removalfrom L-12 in, for example, the Heat Exchanger #3. Heat removed in theHeat Exchanger #3 may include, but is not limited to, heat from enthalpy ofliquid-liquid phase transition and / or heat from specific heat capacity. L-1 isan output of Heat Exchanger #3.HeatHeat Exchanger #2 may involve a heat exchange between ‘warm’ L-1 andExchanger #2‘cold’ L-7 and L-9, which may result in ‘cold’ L-1 (L-2) and ‘warm’ L-7(L-10) and L-9 (L-11). L-7 and L-9 may be heat exchanged with L-1 in HeatExchanger #2 as non-contiguously separate liquid phases to, for example,prevent L-7 and L-9 from dissolving in each other and / or releasing anenthalpy of phase transition during Heat Exchanger #2. Heat Exchanger #2may enable two separate temperature zones within the Refrigeration Cycleportion of the process. For example, L-10, L-11, Mix #1, L-12, HeatExchanger #3, and L-1 may comprise a first temperature zone, while L-2,Mix #2, LL-1, Heat Exchanger #1, LL-2. LLS-1, L-5, L-8, L-6, L-3, L-4,L-7, and L-9 may comprise a second temperature zone which may be at asignificantly different temperature or temperature range than the firsttemperature zone. Said significantly different temperature may comprise atemperature difference greater than the adiabatic temperature change of aenthalpy of the liquid-liquid phase transition. Said temperature zones mayenable the refrigeration cycle to move heat or pump heat across atemperature difference greater than the adiabatic temperature change of theenthalpy of liquid-liquid phase transition.L-2L-2 may comprise L-1 after heat exchange in Heat Exchanger #2. L-2 maybe at a significantly different temperature than L-1, such as, for example, atemperature difference greater than the adiabatic temperature change of theliquid-liquid phase transition of L-11 dissolving in L-10.Mix #2Mix #1 may involve mixing or combining L-2 and L-4 to form a multi-liquidphase solution, LL-1. Said mixing may result in a liquid-liquid phasetransition, which may possess an enthalpy of phase transition. Said enthalpyof phase transition may be endothermic or exothermic, although may beendothermic in the present embodiment.L-4L-4 may comprise L-3 after pumping (P-3). L-4 may comprise aconcentrated solution of ‘salting-out reagent’ or ‘phase transitiontemperature adjustment reagent’ or a ‘concentrate’ or a ‘retentate’. L-4 mayalso comprise some residual organic reagent, which may be due to,including, but not limited to, residual from L-6 and / or an incompleteseparation in LLS-1 and / or residual organic liquid phase dissolved in L-6.The concentrate or retentate may be generated by a membrane-basedprocess, such as reverse osmosis or nanofiltration.LL-1LL-1 may comprise a multi-liquid phase mixture, which may have resultedfrom the mixing of L-2 and L-4 in Mix #2. LL-1 may possess a lessertemperature and / or lesser enthalpy than L-4 and L-2. LL-1 may possess saidlesser temperature, due to, for example, an endothermic liquid-liquid phasetransition in Mix #2. LL-1 may possess a latent endothermic enthalpy ofphase transition, which may absorb heat in Heat Exchanger #1. LL-1 maypossess a lesser temperature than LL-2, which may enable the absorption ofheat in Heat Exchanger #1 due to specific heat capacity.HeatHeat Exchanger #1 may comprise a heat exchanger between LL-1 and anExchanger #1application requiring cooling or a heat source or enthalpy source. LL-1 mayabsorb heat in a heat exchange with an application requiring cooling or aheat source or enthalpy source, which may result in a higher temperatureand / or enthalpy LL-1 (for example: LL-2) and a lower temperature and / orless enthalpy application requiring cooling or heat source or enthalpy source.LL-2LL-2 may comprise the same overall composition as LL-1, except at a highertemperature and / or greater enthalpy. LL-2 may comprise LL-1 after heatexchanging in Heat Exchanger #1. LL-2 may comprise at least a portion amulti-liquid phase mixture. It may be desirable for at least one liquid phaseof said multi-liquid phase mixture to comprise a liquid phase of mostlyorganic. It may be desirable for at least one liquid phase of said multi-liquidphase mixture to comprise mostly water or a dilute aqueous solution of‘salting-out’ reagent or dilute aqueous ‘phase transition temperatureadjustment’ reagent.LLS-1LLS-1 may comprise a liquid-liquid separation device. LLS-1 may separateLL-2 into constituent liquid phases, which may comprise L-5 and L-8.L-5L-5 may comprise a dilute solution of ‘salting-out reagent’. L-5 maycomprise an aqueous solution. L-5 may comprise one of the liquid phasesseparated by LLS-1 from multi-liquid phase mixture LL-2. L-5 may containa portion of residual organic liquid phase, which may be due to, for example,an incomplete separation in LLS-1 and / or residual organic dissolved in L-5.L-6L-6 may comprise L-5 after pressurization using a feed pump (P-1).L-8L-8 may comprise a solution comprising mostly organic liquid phase. L-8may comprise one of the liquid phases separated by LLS-1 from multi-liquidphase mixture LL-2. L-8 may contain a portion of residual water and / or‘salting-out’ reagent, which may be due to, for example, an incompleteseparation in LLS-1 and / or residual water and / or ‘salting-out’ reagentand / or ‘phase transition temperature adjustment’ reagent dissolved in L-8.L-9L-9 may comprise L-8 after pumping (P-2).Reverse‘Reverse Osmosis' may comprise a membrane-based separation process,Osmosissuch as reverse osmosis, nanofiltration, ultrafiltration, or a combinationthereof. Reverse osmosis may involve a feed solution comprising L-6,which may be separated into a concentrate or retentate, L-3, and a permeate,L-7.L-7L-7 may comprise a permeate from ‘Reverse Osmosis'. L-7 may comprisemostly water or other solvent and may comprise a significantly lesserconcentration of ‘salting-out reagent’ or ‘phase transition temperatureadjustment reagent’ than L-6.L-3L-3 may comprise a concentrate from ‘Reverse Osmosis'. L-3 maycomprise mostly water or other solvent and may comprise a significantlygreater concentration of ‘salting-out reagent’ or ‘phase transition temperatureadjustment reagent’ than L-6. L-4 may comprise a concentrated solution of‘salting-out reagent’ or ‘phase transition temperature adjustment reagent’ ora ‘concentrate’ or a ‘retentate’. L-4 may also comprise some residualorganic reagent, which may be due to, including, but not limited to, residualfrom L-6 and / or an incomplete separation in LLS-1 and / or residualorganic liquid phase dissolved in L-6. The concentrate or retentate may begenerated by a membrane-based process, such as reverse osmosis ornanofiltration.L-11L-11 may comprise L-9 after heat exchange in Heat Exchanger #2. L-11may be at a significantly different temperature than L-9, such as, forexample, a temperature difference greater than the adiabatic temperaturechange of an enthalpy of a liquid-liquid phase transition. L-11 may be non-contiguously separate from L-10.L-10L-10 may comprise L-7 after heat exchange in Heat Exchanger #2. L-10may be at a significantly different temperature than L-7, such as, forexample, a temperature difference greater than the adiabatic temperaturechange of an enthalpy of a liquid-liquid phase transition. L-10 may be non-contiguously separate from L-11.Mix #1Mix #1 may involve mixing or combining L-10 and L-11 to form, including,but not limited to, one or more or a combination of the following: a multi-liquid phase solution, L-12, or at least a portion single liquid phase combinedsolution, L-12, or a single liquid phase combined solution, L-12. L-10 andL-11 may Mix in Mix #1 to form an exothermic or endothermic liquid-liquidphase transition, although the present embodiment may form an exothermicphase transition. It may be desirable for the adiabatic temperature change ofsaid enthalpy of said liquid-liquid phase transition to be greater than theapproach temperature and / or heat exchanger Delta-T of Heat Exchanger #2or the temperature difference between L-2 and L-11 or L-10.L-12L-12 may comprise a combination of L-10 and L-11. L-12 may compriseincluding, but not limited to, one or more or a combination of the following:a multi-liquid phase solution, or at least a portion single liquid phasecombined solution, or a single liquid phase combined solution. L-12 may beat a greater temperature and / or greater enthalpy than L-1.HeatHeat Exchanger #3 may involve heat exchanging L-12 with an applicationExchanger #3temperature and / or lesser enthalpy L-12 (for example: L-1) and a greatertemperature and / or greater enthalpy application requiring heating or a heatrequiring heating or a heat sink or a cold source, which may result in a lessersink or a cold source.Example Exemplary Embodiments

[0164] A refrigeration cycle comprising:

[0165] A first step comprising a liquid-liquid phase transition from a single liquid phase to multiple liquid phases absorbing heat

[0166] A second step comprising a liquid-liquid phase transition from multiple liquid phases to a single liquid phase releasing heat

[0167] Wherein a liquid-liquid phase transition temperature is adjusted between the first and second steps

[0168] Wherein the first step and second step occur at different temperature ranges in different temperature ‘zones’

[0169] Wherein temperature zones are maintained by heat exchanging the liquids exiting the first step temperature zone with the liquids exiting the second step temperature zoneExample Notes:Note: Any or each liquid stream in the present invention may be stored in a storage container in the present invention. Storing in a storage container may enable numerous benefits. For example, storing one or more or a combination of liquid phases may enable the desynchronization of the components which consume electricity or heat or cold or work or a combination thereof from the components or steps involved with absorbing or releasing heat. Said desynchronization may enable, for example, the operation of said components which consume electricity or heat or cold or work or a combination thereof when it is most optimal or least costly (for example: when cost of electricity or heat is the least expensive) and the operation of said components or steps involved with absorbing or releasing heat when cooling or heating is needed.

[0171] A liquid phase only refrigeration cycle may require less heat exchangers than a gas-liquid phase transition refrigeration cycle based processes.

[0172] For example, a vapor compression refrigeration cycle based geothermal ground source heat pump requires a heat exchanger between an anti-freeze-water loop heat exchanging with the ground and the refrigeration cycle and also a heat exchanger between the refrigeration cycle and the chilled or heated water circulating through the building (or other application requiring heating or cooling from the heat pump). These two heat exchangers require a combined approach temperature of at least 6-10° C., which means the temperature difference created by the refrigeration cycle must be at least 6-10° C. greater than the temperature difference between the heat source and heat sink.

[0173] A liquid-phase only refrigeration cycle heat may eliminate the need for said two heat exchangers. Instead of heat exchanging between a non-volatile liquid heat transfer liquid and a gas-liquid phase transition refrigerant, the liquids employed in a liquid phase only refrigeration cycle can simultaneously function as both a non-volatile liquid heat transfer liquid and phase transition refrigeration (liquid-liquid phase transition).

[0174] Heat exchanger between before “mixing” and stream after heat releasing heat exchanger.

[0175] May allow process to operate at a temperature difference greater than the adiabatic temperature rise.Liquid Phase Refrigeration Cycle Powered by Osmotic Pressure Differences or by Temperature Differences or BothSummary

[0176] The present inventions pertain to liquid phase refrigeration cycles. The present inventions may pertain to refrigeration cycles driven by liquid-liquid phase transitions which are engineered to occur at two or more different temperatures. The present inventions may involve engineering said liquid-liquid phase transitions to occur at two or more different temperatures by adjusting a concentration of a reagent. The present inventions may involve adjusting a concentration of a reagent by employing a membrane based process, which may include, but is not limited to, one or more or a combination of the following: forward osmosis, osmotically assisted reverse osmosis, reverse osmosis, nanofiltration, ultrafiltration, electrodialysis, or membrane distillation. The present inventions may involve adjusting the concentration of a reagent by the addition of a solvent, such a water, or the removal of a solvent, such as water, or both. In some embodiments, said addition and removal of a solvent, such as water, may involve membrane based processes which occur exclusively or almost exclusively at a liquid phase within the refrigeration cycle.

[0177] In some embodiments, said addition and removal of a solvent is reversible within the system. For example, said reversible addition and removal may involve water added at one point in the cycle being removed at another point in the cycle. For example, in some embodiments, said reversible addition and removal may further comprise regenerating the ‘added solvent’ from the removed solvent.

[0178] In some embodiments, removed solvent may comprise the same or relatively similar composition to said added solvent, and said removed solvent may be employed as said added solvent with minimal additional treatment steps, if any at all. Said some embodiments may include, but are not limited to, embodiments wherein solvent is removed using reverse osmosis, osmotically assisted reverse osmosis, nanofiltration, or ultrafiltration, or membrane distillation.

[0179] In some embodiments, solvent may be removed by means of a draw solution of in forward osmosis or osmotically assisted reverse osmosis. In some embodiments, a water-lean draw solution (or draw solution) may remove solvent by means of forward osmosis or osmotically assisted reverse osmosis, and may become water-rich draw solution (or diluted draw solution). Said water-rich draw solution may regenerated into a mostly water liquid phase and a water-lean draw solution liquid phase by means of a liquid-liquid phase transition, which may be thermally driven. Said water lean draw solution may comprise a solution with greater osmotic pressure which may be employed as a draw solution to remove solvent. Said mostly water liquid phase may comprise a solution with a lesser osmotic pressure which may be employed as said added solvent or may be employed as said added solvent after treatment to remove residual reagents, such as draw solution reagent or other potential residual reagents.

[0180] Said regenerating may involve a natural or engineered system which may involve a relatively plentiful source of lesser osmotic pressure solution and a relatively plentiful source of greater osmotic pressure solution. Said relatively plentiful source of lesser osmotic pressure solution may include, but is not limited to, one or more or a combination of the following: rainwater, river water, lake water, brackish water, seawater, dew, or groundwater, wastewater, non-potable water, or a derivative thereof. Said relatively plentiful source of greater osmotic pressure solution may include, but is not limited to, one or more or a combination of the following: seawater, saline aquifer, salt mine, or frackwater, or mine tailings, brine pond, solar pond, evaporation pond, reverse osmosis brine, desalination brine, waste brine, or mining water, or hypersaline lake, or antifreeze reagent, or sugar concentrate, or molasses, or organically derived draw solution, or lubricant, or a derivative thereof.

[0181] In some embodiments, solvent addition or removal or both may be conducted using a membrane based process.

[0182] The present refrigeration cycles may be powered by the enthalpy of mixing of two or more solutions with different osmotic pressures. For example, an added solvent may comprise a solution with a lesser osmotic pressure. For example, added solvent may comprise water or freshwater. For example, the draw solution employed to remove solvent in a forward osmosis or osmotically assisted reverse osmosis process may comprise a solution with a greater osmotic pressure. Solvent may be added in one portion of the refrigeration cycle. Solvent may be removed at another portion of the refrigeration cycle, whereby said removing may involve the formation of a diluted draw solution or solution with a greater osmotic pressure than said added solvent, which may involve forward osmosis or osmotically assisted reverse osmosis. Said two or more solutions with different osmotic pressures may be regenerated internally, or regenerated externally, or may be naturally occurring, or a combination thereof. For example, regenerating internally may involve regenerating a diluted draw solution by a liquid-liquid phase transition, which may include, but is not limited to, a thermally driven liquid-liquid phase transition or a light driven liquid-liquid phase transition or a combination thereof. For example, regenerating internally may involve regenerating by means of reverse osmosis, or nanofiltration, or ultra-filtration, or osmotically assisted reverse osmosis. For example, regenerating internally may involve regenerating a diluted draw solution by a liquid-liquid phase transition, which may include, but is not limited to, a thermally driven liquid-liquid phase transition or a light driven liquid-liquid phase transition or a combination thereof, and further regenerating by means of reverse osmosis, or nanofiltration, or ultra-filtration, or osmotically assisted reverse osmosis. For example, regenerating externally may involve a distillation process, or an evaporation process, or a process employing regenerating for an external use. For example, a process employing regenerating for an external use may involve a seawater desalination process, such reverse osmosis or MSF or cryodesalination or other desalination process, which may generate brine or concentrate or retentate, which may be employed as a high osmotic pressure solution. For example, said naturally occurring two or more solutions with different osmotic pressures may be involve a lesser osmotic pressure solution derived from rainwater, river water, lake water, brackish water, seawater, dew, or groundwater, and a greater osmotic pressure solution derived from seawater, saline aquifer, salt mine, or frackwater, or mining tailings, or mining, or hypersaline lake. For example, a combination of naturally and external regeneration may involve a rainwater or other ‘naturally’ occurring source of freshwater as a lesser osmotic pressure solution and a greater osmotic pressure solution comprising a saline water source regenerated in a solar pond or evaporation pond or evaporative cooling system or evaporation system.

[0183] Advantages of the present invention may include, but are not limited to, one or more or a combination of the following:

[0184] The capability of powering refrigeration cycles, including heating or cooling, using small temperature differences. Said small temperature differences may comprise low temperature heat, which may be at too low of a temperature to efficiently or effectively power prior art refrigeration cycles. Said small temperature differences may comprise higher temperature ‘cold’, which may be at too high of a temperature to efficiently or effectively power prior art refrigeration cycles.

[0185] The capability of achieving high coefficients of performance or energy efficiency with a thermally powered refrigeration cycle or with small temperature differences or a combination thereof.

[0186] The ability to power a refrigeration cycle with thermal input or heat or temperature differences operating using liquid-liquid phase transitions.

[0187] The ability to create a refrigeration cycle powered by heat or temperature differences without a gas-liquid phase transition, or gas-solid phase transition, or solid-liquid phase transition.

[0188] The ability to power a refrigeration cycle, or heating, or cooling using the enthalpy of mixing of two or more liquids with different osmotic pressures or using two or more liquids with different osmotic pressures.

[0189] It is important to note that the vapor pressure difference, if any, between said two or more liquids with different osmotic pressures may be too small or insignificant to be employed or to be effective in an absorption refrigeration cycle. For example, the vapor pressure difference between solutions such as freshwater and seawater, or freshwater and saline lake water, or brackish water and seawater, or brackish water and saline lake water, or seawater and saline lake water, or a combination thereof may be too insignificant for an absorption refrigeration cycle, however the osmotic pressure difference between said solutions may significant enough or sufficient to power the refrigeration cycles introduced herein in the present invention.Figure Summaries

[0190] FIG. 9: FIG. 9 may comprise a liquid phase refrigeration cycle wherein solvent may be added and removed to drive liquid-liquid phase transitions to ‘pump’ heat, and wherein solvent removal may be conducted using forward osmosis. FIG. 9 may involve regenerating an added solvent and a draw solution for removing added solvent by means of a thermally driven liquid-liquid phase transition and / or separation of the resulting liquid phases. FIG. 9 may involve employing a solution with lesser osmotic pressure as an added solvent and a solution with greater osmotic pressure as a draw solution or organic Composition #2.

[0191] FIG. 10: FIG. 10 may be the same as FIG. 9, except further comprises a step for separating residual organic Composition #2 or other residual reagents in the regeneration portion from the regenerated solvent before adding said regenerated solvent to the refrigeration cycle portion. Said step may comprise a membrane-based process, such as reverse osmosis, or nanofiltration, or ultrafiltration, or forward osmosis, or osmotically assisted reverse osmosis, or a combination thereof.

[0192] FIG. 11: FIG. 11 may comprise a liquid phase refrigeration cycle employing a heat exchanger to generate or form or create two temperature zones. The refrigeration cycle may involve an endothermic liquid-liquid phase transition in the cold temperature zone and an exothermic liquid-liquid phase transition in the warm temperature zone. The temperature difference between the temperature zones may be greater than the temperature difference which may be generated by the adiabatic temperature difference generated by an enthalpy of liquid-liquid phase transition in the refrigeration cycle. It may be desirable for the adiabatic temperature difference generated by an enthalpy of liquid-liquid phase transition in the refrigeration cycle to be greater than the delta-T or approach temperature or temperature difference between the outputs of the heat exchange or a combination thereof. Said temperature zones may be interconnected by said heat exchanger. FIG. 11 may enable a liquid phase refrigeration cycle which may be capable of generating a temperature difference or pumping heat across a temperature difference greater than the temperature difference generated by the adiabatic temperature difference generated by an enthalpy of liquid-liquid phase transition in the refrigeration cycle.

[0193] FIG. 12: FIG. 12 may be the same as FIG. 11, except further comprises a step for separating residual organic Composition #2 or other residual reagents in the regeneration portion from the regenerated solvent before adding said regenerated solvent to the refrigeration cycle portion. Said step may comprise a membrane-based process, such as reverse osmosis, or nanofiltration, or ultrafiltration, or forward osmosis, or osmotically assisted reverse osmosis, or a combination thereof.

[0194] FIG. 13: FIG. 13 may be the same as FIG. 9 or FIG. 10, except may further comprise adding the added solvent by employing organic Composition #1 as a draw solution in a forward osmosis or osmotically assisted reverse osmosis step.

[0195] FIG. 14: FIG. 14 may comprise a liquid phase refrigeration cycle wherein solvent may be added and removed to drive liquid-liquid phase transitions to ‘pump’ heat, and wherein solvent removal may be conducted using forward osmosis. FIG. 14 may involve employing a solution with lesser osmotic pressure as an added solvent and a solution with greater osmotic pressure as a draw solution or organic Composition #2. FIG. 14 may involve a lesser osmotic pressure solution which is naturally sourced or externally regenerated and / or a greater osmotic pressure solution which is naturally sourced or externally regenerated. Said lesser osmotic pressure solution may be treated with one or more treatment processes, such as membrane processes, reverse osmosis, nanofiltration, filtration, UV, or other processes described herein, or other liquid treatment processes known in the art, before being added. For example, said treatment may be conducted to remove contaminants which may accumulate or may impact or may be detrimental to the operation of the refrigeration cycle if not removed or remediated or reduced.

[0196] FIG. 15: FIG. 15 may be the same as FIG. 14, except the added solvent added to the refrigeration cycle may comprise reagents other than water or reagents in addition to water.

[0197] FIG. 16: FIG. 16 may be the same as FIG. 14 or FIG. 15, except may further comprise adding the added solvent by employing organic Composition #1 as a draw solution in a forward osmosis or osmotically assisted reverse osmosis step.

[0198] FIG. 17: FIG. 17 may comprise a liquid phase refrigeration cycle wherein solvent may be added and removed to drive liquid-liquid phase transitions to ‘pump’ heat, and wherein solvent removal may be conducted using forward osmosis. FIG. 17 may involve employing a solution with lesser osmotic pressure as an added solvent and a solution with greater osmotic pressure as a draw solution or organic Composition #2. FIG. 17 may involve a lesser osmotic pressure solution which is naturally sourced or externally regenerated and / or a greater osmotic pressure solution which is naturally sourced or externally regenerated. FIG. 17 may comprise a liquid phase refrigeration cycle employing a heat exchanger to generate or form or create two temperature zones. The refrigeration cycle may involve an endothermic liquid-liquid phase transition in the cold temperature zone and an exothermic liquid-liquid phase transition in the warm temperature zone. The temperature difference between the temperature zones may be greater than the temperature difference which may be generated by the adiabatic temperature difference generated by an enthalpy of liquid-liquid phase transition in the refrigeration cycle. It may be desirable for the adiabatic temperature difference generated by a enthalpy of liquid-liquid phase transition in the refrigeration cycle to be greater than the delta-T or approach temperature or temperature difference between the outputs of the heat exchange or a combination thereof. Said temperature zones may be interconnected by said heat exchanger. FIG. 17 may enable a liquid phase refrigeration cycle which may be capable of generating a temperature difference or pumping heat across a temperature difference greater than the temperature difference generated by the adiabatic temperature difference generated by a enthalpy of liquid-liquid phase transition in the refrigeration cycle.

[0199] FIG. 18: FIG. 18 may be the same as FIG. 12, except employ a UCST based liquid-liquid phase transition regeneration in the Regeneration Portion. In FIG. 18, Organic Composition #2 may possess a UCST liquid-liquid phase transition. In FIG. 18, Organic Composition #1 may possess a LCST liquid-liquid phase transition.

[0200] FIG. 19: FIG. 19 may be the same as FIG. 12, except employ a UCST based liquid-liquid phase transition in the Refrigeration Cycle Portion. In FIG. 19, Organic Composition #1 may possess a UCST liquid-liquid phase transition. In FIG. 19, Organic Composition #2 may possess a LCST liquid-liquid phase transition.

[0201] FIG. 20: FIG. 20 may be the same as FIG. 12, except employ a UCST based liquid-liquid phase transition in the Refrigeration Cycle Portion and a UCST based liquid-liquid phase transition in the Regeneration Portion. In FIG. 20, Organic Composition #1 may possess a UCST liquid-liquid phase transition and Organic Composition #2 may possess a UCST liquid-liquid phase transition.

[0202] FIG. 21: FIG. 21 be the same as FIG. 16, except shows Liquid A undergoing a treatment step (RO) before Liquid A is added to the process.

[0203] FIG. 22: FIG. 22 be the same as FIG. 17, except shows Liquid A undergoing a treatment step (RO) before Liquid A is added to the process.Definitions

[0204] Organic Composition #1: Organic Composition #1 comprises the organic or liquid-liquid phase transition component or a combination thereof of the ‘Refrigeration Cycle Portion’.

[0205] Organic Composition #2: Organic Composition #2 comprises the organic or liquid-liquid phase transition component or a combination thereof of the ‘Regeneration Portion’. Organic Composition #2 may also be described as ‘draw solution reagent’ when described in the context of the Regeneration Portion of the process. Alternatively, Organic Composition #2 may simply comprise a draw solution employed to remove solvent from the refrigeration cycle in, for example, Forward Osmosis, Osmotically Assisted Reverse Osmosis, or another membrane based process, or another process, or a combination thereof.

[0206] Regeneration Portion: Regeneration Portion may comprise components and reagents in the process related to adding solvent, or removing solvent, or regenerating removed solvent, or regenerating draw solution for the removal of solvent, or a combination thereof.

[0207] Refrigeration Cycle Portion: Refrigeration Cycle Portion may comprise components and reagents in the process related to moving or pumping heat or absorbing heat and releasing heat between two different locations or initiating exothermic or endothermic phase transitions due to concentration adjustment or a combination thereof.

[0208] Regenerated Solvent: May comprise liquid which permeable and / or transferrable into the Refrigeration Cycle Portion. Regenerated Solvent may include, but is not limited to, water, or low molecular weight organic solvent, or ammonia, or amine, or a combination thereof. Regenerated Solvent may also be referred to as solvent or permeate or added solvent or a mostly water solution.

[0209] Single Liquid Phase Combined Solution: May comprise a solution of Organic Composition #1 dissolved in water or an aqueous solution or solvent, or Organic Composition #2 dissolved in water or an aqueous solution or solvent, or a combination thereof.

[0210] Multi-Liquid Phase Mixture: May comprise a mixture of liquid phases. May comprise a mixture of liquid phases, wherein at least one liquid phase comprises mostly Organic Composition #1 or Organic Composition #2, and / or at least one liquid phase comprises mostly water or aqueous solution or solvent.

[0211] LCST: May involve a liquid composition which undergoes an exothermic phase transition when transforming from two liquid phases to a single liquid phase and an endothermic phase transition when transforming from a single liquid phase to two liquid phases.

[0212] UCST: May involve a liquid composition which undergoes an exothermic phase transition when transforming from a single liquid phase to two liquid phases and an endothermic phase transition when transforming from two liquid phases to a single liquid phase.

[0213] ‘Salting-Out’ Reagent: May comprise a salt or an organic or a combination thereof. May also be described as phase transition temperature adjustment reagent.

[0214] Example desirable properties of salts may include, but are not limited to, one or more or a combination of the following:

[0215] Capability to reduce phase transition temperature or salt out Organic Composition #1 with minimal salt concentration or osmotic pressure.

[0216] Insoluble or minimally soluble or only partial solubility or a combination thereof in Organic Composition #1 and / or Organic Composition #2.

[0217] Ratio of phase transition temperature adjustment relative to salt concentration or osmotic pressure of salt in solution

[0218] Enthalpy of phase transition Organic Composition #1 when a liquid-liquid phase transition is driven by ‘salting out’ or phase transition temperature adjustment

[0219] Concentration of residual Organic Composition #1 and / or Organic Composition #2 after ‘salting out’

[0220] Chemical compatibility with other reagents and / or materials and / or equipment in the process

[0221] Example desirable properties of organics may include

[0222] Capability to reduce phase transition temperature or salt out Organic Composition #1 with minimal salt concentration or osmotic pressure.

[0223] Insoluble or minimally soluble or only partial solubility or a combination thereof in Organic Composition #1 and / or Organic Composition #2.

[0224] Ratio of phase transition temperature adjustment relative to salt concentration or osmotic pressure of salt in solution

[0225] Enthalpy of phase transition Organic Composition #1 when a liquid-liquid phase transition is driven by ‘salting out’ or phase transition temperature adjustment

[0226] Concentration of residual Organic Composition #1 and / or Organic Composition #2 after ‘salting out’

[0227] Chemical compatibility with other reagents and / or materials and / or equipment in the process.Step-by-Step DescriptionsFIG. 9:Refrigeration Cycle Portion:1A—Mixing Reagents to Form Endothermic Phase Transition: A solution comprising mostly single liquid phase combined solution (L-1) may be mixed with a solution concentrated in ‘salting-out’ reagent or phase transition temperature adjustment reagent (L-4) in a mixing device (Mix #1). Said mixing of L-4 and L-1 may result in an endothermic liquid-liquid phase transition into a multi-liquid phase mixture. L-4 may dissolve in the aqueous component of L-1, which may result in Organic Composition #1 becoming at least partially insoluble and / or forming a separate liquid phase in a liquid-liquid phase transition. A resulting multi-liquid phase mixture (LL-2) may comprise a mostly Organic Composition #1 liquid phase and an aqueous dilute ‘salting-out’ reagent or mostly phase transition temperature adjustment reagent liquid phase. The previously described liquid-liquid phase transition may be endothermic and may result in the temperature of LL-2 being less than the mean temperature of L-1 and L-4. In some embodiments, step 1A and step 2A may be combined. For example, in some embodiments, Mix #1 may be combined with the Enthalpy Source Heat Exchanger.

[0229] 2A—Heat Absorbing Heat Exchange: LL-2 may be heat exchanged (Enthalpy Source Heat Exchanger) with a heat source or an application requiring cooling or an enthalpy source or a combination thereof. LL-2 may absorb heat from or ‘cool’ said heat source or an application requiring cooling or an enthalpy source or a combination thereof, while said heat source or an application requiring cooling or an enthalpy source or a combination thereof may be cooled or supply heat to LL-2. Depending on the liquid state of LL-2, the temperature of LL-2, the temperature of the Enthalpy Heat Source Heat Exchanger, and phase transition properties of LL-2, LL-2 may absorb heat in the Enthalpy Heat Source Heat Exchanger due to an enthalpy of liquid-liquid phase transition, or specific heat capacity due to an enthalpy of phase transition, or specific heat capacity or a combination thereof. LL-2 may exit the Enthalpy Source Heat Exchanger at a greater enthalpy or temperature or a combination thereof state and / or may comprise at least a portion a multi-liquid phase solution (LL-3).

[0230] 3A—Liquid-Liquid Separation: LL-3 may be separated into two separate liquid streams using a liquid-liquid separation device (LLS-1). One of the two liquid phases may comprise a mostly organic liquid phase (L-3), such as mostly Organic Composition #1. One of the liquid phases may comprise mostly aqueous dilute ‘salting-out’ reagent or mostly phase transition temperature adjustment reagent solution (L-2).

[0231] 4A—Forward Osmosis Concentrating: Mostly aqueous dilute ‘salting-out’ reagent or mostly phase transition temperature adjustment reagent solution (L-2) may be fed into a forward osmosis or osmotically assisted reverse osmosis or a combination thereof system (FO). L-2 may function as a feed solution, while L-9, which may comprise mostly organic Composition #2, may function as a draw solution. A portion of water or other permeable solvent in L-2 may permeate from L-2 to L-9 across a semi-permeable membrane, while ‘Salting-out’ reagent or phase transition temperature adjustment reagent in L-2 may be rejected by said membrane. FO may concentrate L-2 into a retentate solution comprising a concentrated solution of salting-out reagent or phase transition temperature adjustment reagent (L-4). FO may dilute L-9 into a diluted solution of organic Composition #2 (L-5), which may have been diluted by FO permeate, which may comprise water and / or other solvent permeate.

[0232] 5A—Mixing Reagents to Form Exothermic Phase Transition: L-3, which may comprise a liquid phase comprising mostly organic Composition #1, may be mixed with a solution comprising mostly water, L-10, in a mixing device, Mix #2, forming LL-1. L-10 may be purified to remove residual organic Composition #2 and / or other potential contaminants from the Regeneration Portion before or during Mix #2. Depending on the liquid-liquid phase transition temperature range, the temperature of L-10 and L-3, and the enthalpy of the liquid-liquid phase transition, LL-1 may comprise a multi-liquid phase mixture, or a multi-liquid phase mixture with some L-3 dissolved in L-10, or a single liquid phase combined solution. In some embodiments, step 5A and step 6A may be combined. For example, in some embodiments, Mix #2 may be combined with the Enthalpy Sink Heat Exchanger.

[0233] 6A—Heat Releasing Heat Exchange: LL-1 may be heat exchanged with an application requiring heating, a heat sink, or a combination thereof using a heat exchanger (Enthalpy Sink Heat Exchanger). LL-1 may release heat to said application requiring heating, a heat sink, or a combination thereof, while said application requiring heating, a heat sink, or a combination thereof may cool LL-1. Depending on the liquid state of LL-1, the temperature of LL-1, the temperature of the Enthalpy Heat Sink Heat Exchanger, and phase transition properties of LL-1, LL-1 may release heat in the Enthalpy Heat Sink Heat Exchanger due to an enthalpy of liquid-liquid phase transition, or specific heat capacity due to an enthalpy of phase transition, or specific heat capacity or a combination thereof. LL-1 may exit the Enthalpy Sink Heat Exchanger at a lower enthalpy or temperature or a combination thereof state and may comprise at least a portion a single liquid phase combined solution (L-1).Regeneration Portion:1B—Preheating Diluted Draw Solution in Heat Exchange: ‘Cold’ diluted Organic Composition #2 draw solution (L-5) may be preheated in a heat exchange (Heat Exchanger #3) with ‘warm’ mostly Organic Composition #2 liquid phase (L-7) and ‘warm’ mostly water or other solvent liquid phase (L-8). The pre-heated L-5 (L-6) which may result from the heat exchange in Heat Exchanger #3 may be near, or at, or below or above a liquid-liquid phase transition temperature range of L-6.

[0235] 2B—Liquid-Liquid Phase Transition into Multi-Liquid Phase Mixture: L-6 may be further heated by a heat source (Thermal Source). In Thermal Source, L-6 may be heated such that it undergoes a liquid-liquid phase transition into a multi-liquid phase mixture, LL-4. LL-4 may be near, or at, or above a liquid-liquid phase transition temperature range of L-6.

[0236] 3B—Liquid-Liquid Separation: LL-4 may be separated into non-contiguously separate liquid phases (L-7 and L-8) using a liquid-liquid separation device, LLS-2. L-7 and L-8 may comprise the constituent liquid phases of LL-4. L-7 may comprise mostly Organic Composition #2 and L-8 may comprise mostly water or other solvent or a combination thereof.

[0237] 4B—Cooling Separated Liquid Phases in Heat Exchange: ‘Warm’ L-7 and L-8 may be heat exchanged with ‘Cold’ L-5 in a heat exchange (Heat Exchanger #3), which may result in cooler temperature L-7 and L-8 (L-9 and L-10) and warmer temperature L-5 (L-6). L-7 and L-8 may be heat exchanged as separate liquid phases to, for example, prevent L-7 and / or L-8 from dissolving in each other, as they may be cooled below a liquid-liquid phase transition temperature while heat exchanged in Heat Exchanger #3. If desirable, L-9 or L-10 may be further cooled before FO and / or Mix #2. Said further cooling, may include, but is not limited to, one or more or a combination of the following: heat exchange cooling, evaporative cooling, or wet surface air heat exchanger cooling. L-9 may be transferred to step 4A and L-10 may be transferred to Step 5A.FIG. 10:Refrigeration Cycle Portion:1A—Mixing Reagents to Form Endothermic Phase Transition: A solution comprising mostly single liquid phase combined solution (L-1) may be mixed with a solution concentrated in ‘salting-out’ reagent or phase transition temperature adjustment reagent (L-4) in a mixing device (Mix #1). Said mixing of L-4 and L-1 may result in an endothermic liquid-liquid phase transition into a multi-liquid phase mixture. L-4 may dissolve in the aqueous component of L-1, which may result in Organic Composition #1 becoming at least partially insoluble and / or forming a separate liquid phase in a liquid-liquid phase transition. A resulting multi-liquid phase mixture (LL-2) may comprise a mostly Organic Composition #1 liquid phase and a mostly aqueous dilute ‘salting-out’ reagent liquid phase or mostly phase transition temperature adjustment reagent liquid phase. The previously described liquid-liquid phase transition may be endothermic and may result in the temperature of LL-2 being less than the mean temperature of L-1 and L-4. In some embodiments, step 1A and step 2A may be combined. For example, in some embodiments, Mix #1 may be combined with the Enthalpy Source Heat Exchanger.

[0239] 2A—Heat Absorbing Heat Exchange: LL-2 may be heat exchanged (Enthalpy Source Heat Exchanger) with a heat source or an application requiring cooling or an enthalpy source or a combination thereof. LL-2 may absorb heat from or ‘cool’ said heat source or an application requiring cooling or an enthalpy source or a combination thereof, while said heat source or an application requiring cooling or an enthalpy source or a combination thereof may be cooled or supply heat to LL-2. Depending on the liquid state of LL-2, the temperature of LL-2, the temperature of the Enthalpy Heat Source Heat Exchanger, and phase transition properties of LL-2, LL-2 may absorb heat in the Enthalpy Heat Source Heat Exchanger due to an enthalpy of liquid-liquid phase transition, or specific heat capacity due to an enthalpy of phase transition, or specific heat capacity or a combination thereof. LL-2 may exit the Enthalpy Source Heat Exchanger at a greater enthalpy or temperature or a combination thereof state and / or may comprise at least a portion a multi-liquid phase solution (LL-3).

[0240] 3A—Liquid-Liquid Separation: LL-3 may be separated into two separate liquid streams using a liquid-liquid separation device (LLS-1). One of the two liquid phases may comprise a mostly organic liquid phase (L-3), such as mostly Organic Composition #1. One of the liquid phases may comprise mostly aqueous dilute ‘salting-out’ reagent or mostly phase transition temperature adjustment reagent solution (L-2).

[0241] 4A—Forward Osmosis Concentrating: Mostly aqueous dilute ‘salting-out’ reagent or mostly phase transition temperature adjustment reagent solution (L-2) may be fed into a forward osmosis or osmotically assisted reverse osmosis or a combination thereof system (FO). L-2 may function as a feed solution, while L-10, which may comprise mostly organic Composition #2, may function as a draw solution. A portion of water or other permeable solvent in L-2 may permeate from L-2 to L-10 across a semi-permeable membrane, while ‘salting-out’ reagent or phase transition temperature adjustment reagent in L-2 may be rejected by said membrane. FO may concentrate L-2 into a retentate solution comprising a concentrated solution of ‘salting-out’ reagent or phase transition temperature adjustment reagent (L-4). FO may dilute L-10 into a diluted solution of organic Composition #2 (L-5), which may have been diluted by FO permeate, which may comprise water and / or other solvent permeate.

[0242] 5A—Mixing Reagents to Form Exothermic Phase Transition: L-3, which may comprise a liquid phase comprising mostly organic Composition #1, may be mixed with a solution comprising mostly water, L-13, in a mixing device, Mix #2, forming LL-1. Depending on the liquid-liquid phase transition temperature range, the temperature of L-13 and L-3, and the enthalpy of the liquid-liquid phase transition, LL-1 may comprise a multi-liquid phase mixture, or a multi-liquid phase mixture with some L-3 dissolved in L-13, or a single liquid phase combined solution. In some embodiments, step 5A and step 6A may be combined. For example, in some embodiments, Mix #2 may be combined with the Enthalpy Sink Heat Exchanger.

[0243] 6A—Heat Releasing Heat Exchange: LL-1 may be heat exchanged with an application requiring heating, a heat sink, or a combination thereof using a heat exchanger (Enthalpy Sink Heat Exchanger). LL-1 may release heat to said application requiring heating, a heat sink, or a combination thereof, while said application requiring heating, a heat sink, or a combination thereof may cool LL-1. Depending on the liquid state of LL-1, the temperature of LL-1, the temperature of the Enthalpy Heat Sink Heat Exchanger, and phase transition properties of LL-1, LL-1 may release heat in the Enthalpy Heat Sink Heat Exchanger due to an enthalpy of liquid-liquid phase transition, or specific heat capacity due to an enthalpy of phase transition, or specific heat capacity or a combination thereof. LL-1 may exit the Enthalpy Sink Heat Exchanger at a lower enthalpy or temperature or a combination thereof state and may comprise at least a portion a single liquid phase combined solution (L-1).Regeneration Portion:1B—Mixing Diluted Draw Solution with Recovered Residual Organic Composition #2 from RO: ‘Cold’ diluted Organic Composition #2 draw solution (L-5) may be mixed with an aqueous retentate solution (L-12) from ‘RO’ comprising residual organic Composition #2 recovered from L-11 in a mixing device (Mix #3). Said mixing of L-5 and L-12 in Mix #3 may result in a combined solution of L-5 and L-12 (L-6). If desirable, L-6 may comprise a more dilute concentration of organic Composition #2 compared to L-5. If desirable, L-12 and L-6 may contain liquid-liquid phase transition facilitator reagents, or ‘salting-out’ reagents, or phase transition temperature adjustment reagents or a combination thereof to, for example, facilitate liquid-liquid phase transition and / or liquid-liquid separation in, for example, step 2B, or 3B, or 4B, or a combination thereof. If desirable, said liquid-liquid phase transition facilitator reagents, or ‘salting-out’ reagents, or phase transition temperature adjustment reagents or a combination thereof may be rejected by RO in step 6B and may, if desirable, be separate from reagents employed in the Refrigeration Cycle Portion.

[0245] 2B—Preheating Diluted Draw Solution in Heat Exchange: L-6 may be preheated in a heat exchange (Heat Exchanger #3) with ‘warm’ mostly Organic Composition #2 liquid phase (L-8) and ‘warm’ mostly water or other solvent liquid phase (L-9). The pre-heated L-6 (L-7) which may result from the heat exchange in Heat Exchanger #3, may be near, or at, or below or above a liquid-liquid phase transition temperature range of L-7.

[0246] 3B—Liquid-Liquid Phase Transition into Multi-Liquid Phase Mixture: L-7 may be further heated by a heat source (Thermal Source). In Thermal Source, L-7 may be heated such that it undergoes a liquid-liquid phase transition into a multi-liquid phase mixture, LL-4. LL-4 may be near, or at, or above a liquid-liquid phase transition temperature range of L-7.

[0247] 4B—Liquid-Liquid Separation: LL-4 may be separated into non-contiguously separate liquid phases (L-8 and L-9) using a liquid-liquid separation device, LLS-2. L-8 and L-9 may comprise the constituent liquid phases of LL-4. L-8 may comprise mostly Organic Composition #2 and L-9 may comprise mostly water or other solvent or a combination thereof.

[0248] 5B—Cooling Separated Liquid Phases in Heat Exchange: ‘Warm’ L-8 and L-9 may be heat exchanged with ‘Cold’ L-6 in a heat exchanger (Heat Exchanger #3), which may result in cooler temperature L-8 and L-9 (L-10 and L-11) and warmer temperature L-6 (L-7). L-8 and L-9 may be heat exchanged as separate liquid phases to, for example, prevent L-8 and / or L-9 from dissolving in each other, as they may be cooled below a liquid-liquid phase transition temperature while heat exchanged in Heat Exchanger #3. If desirable, L-10 or L-11 may be further cooled before FO, RO, and / or Mix #2. Said further cooling, may include, but is not limited to, one or more or a combination of the following: heat exchange cooling, evaporative cooling, or wet surface air heat exchanger cooling. L-10 may be transferred to step 4A and L-11 may be transferred to Step 6B.

[0249] 6B—Reverse Osmosis or Nanofiltration or Ultrafiltration Purification: L-11 may comprise mostly water or other solvent, although may contain residual reagents, which may include, but are not limited to: residual organic Composition #2 and / or phase transition facilitator reagents, or ‘salting-out’ reagents, or phase transition temperature adjustment reagents or a combination thereof. Said residual reagents may be separated from water and / or other solvent. For example, L-11 may comprise a feed solution to a membrane-based process, which may include, but is not limited to, reverse osmosis, or nanofiltration, or ultrafiltration, or forward osmosis, or osmotically assisted reverse osmosis, or a combination thereof process (RO). Said residual reagents may be at least in part rejected by said membrane based process. RO may separate L-11 into a water or other solvent permeate (L-13) and a retentate solution comprising a greater concentration of said residual reagents than L-11 (L-12). L-12 may be transferred to step 1B. L-13 may be transferred to step 5A.FIG. 13:Refrigeration Cycle Portion:1A—Mixing Reagents to Form Endothermic Phase Transition: A solution comprising mostly single liquid phase combined solution (L-1) may be mixed with a solution concentrated in ‘salting-out’ reagent or phase transition temperature adjustment reagent (L-4) in a mixing device (Mix #1). Said mixing of L-4 and L-1 may result in an endothermic liquid-liquid phase transition into a multi-liquid phase mixture. L-4 may dissolves in the aqueous component of L-1, which may result in Organic Composition #1 becoming at least partially insoluble and / or forming a separate liquid phase in a liquid-liquid phase transition. A resulting multi-liquid phase mixture (LL-2) may comprise a mostly Organic Composition #1 liquid phase and a mostly aqueous dilute ‘salting-out’ reagent liquid phase or mostly phase transition temperature adjustment reagent liquid phase. The previously described liquid-liquid phase transition may be endothermic and may result in the temperature of LL-2 being less than the mean temperature of L-1 and L-4. In some embodiments, step 1A and step 2A may be combined. For example, in some embodiments, Mix #1 may be combined with the Enthalpy Source Heat Exchanger.

[0251] 2A—Heat Absorbing Heat Exchange: LL-2 may be heat exchanged (Enthalpy Source Heat Exchanger) with a heat source or an application requiring cooling or an enthalpy source or a combination thereof. LL-2 may absorb heat from or ‘cool’ said heat source or an application requiring cooling or an enthalpy source or a combination thereof, while said heat source or an application requiring cooling or an enthalpy source or a combination thereof may be cooled or supply heat to LL-2. Depending on the liquid state of LL-2, the temperature of LL-2, the temperature of the Enthalpy Heat Source Heat Exchanger, and phase transition properties of LL-2, LL-2 may absorb heat in the Enthalpy Heat Source Heat Exchanger due to an enthalpy of liquid-liquid phase transition, or specific heat capacity due to an enthalpy of phase transition, or specific heat capacity or a combination thereof. LL-2 may exit the Enthalpy Source Heat Exchanger at a greater enthalpy or temperature or a combination thereof state and / or may comprise at least a portion a multi-liquid phase solution (LL-3).

[0252] 3A—Liquid-Liquid Separation: LL-3 may be separated into two separate liquid streams using a liquid-liquid separation device (LLS-1). One of the two liquid phases may comprise a mostly organic liquid phase (L-3), such as mostly Organic Composition #1. One of the liquid phases may comprise mostly aqueous dilute ‘salting-out’ reagent or mostly phase transition temperature adjustment reagent solution (L-2).

[0253] 4A—Forward Osmosis Concentrating: Mostly aqueous dilute ‘salting-out’ reagent or mostly phase transition temperature adjustment reagent solution (L-2) may be fed into a forward osmosis or osmotically assisted reverse osmosis or a combination thereof system (FO #1). L-2 may function as a feed solution, while L-10, which may comprise mostly organic Composition #2, may function as a draw solution. A portion of water or other permeable solvent in L-2 may permeate from L-2 to L-10 across a semi-permeable membrane, while ‘salting-out’ reagent or phase transition temperature adjustment reagent in L-2 may be rejected by said membrane. FO #1 may concentrate L-2 into a retentate solution comprising a concentrated solution of ‘salting-out’ reagent or phase transition temperature adjustment reagent (L-4). FO #1 may dilute L-10 into a diluted solution of organic Composition #2 (L-5), which may have been diluted by FO permeate, which may comprise water and / or other solvent permeate.

[0254] 5A—FO Mixing Reagents to form Exothermic Phase Transition: L-3, which may comprise a liquid phase comprising mostly organic Composition #1, may comprise a draw solution in a forward osmosis, or osmotically assisted reverse osmosis, or combination thereof process (FO #2). A solution comprising mostly water, L-11 may comprise a feed solution. L-3 may draw water or other permeable solvent from L-11 across a membrane, while said membrane may reject non-permeable residual reagents. During FO #2, L-3 may be diluted to form LL-1 or L-1, which may comprise an exothermic liquid-liquid phase transition. During FO #2, residual reagents in L-11 may be concentrated to form retentate L-12. The present step may enable water to be transferred or returned or recovered from the Regeneration Portion to the Refrigeration Cycle Portion while preventing the contamination of the Refrigeration Cycle Portion with reagents from the Regeneration Portion. Advantageously, the present step may enable water to be transferred or returned or recovered from the Regeneration Portion to the Refrigeration Cycle portion while preventing the contamination of the Refrigeration Cycle Portion with reagents from the Regeneration Portion and utilizing a passive or non-valuable energy consuming process. In the present embodiment, it may be desirable to combine step 5A and step 6A. For example, FO #2 may be integrated with the Enthalpy Sink Heat Exchanger, which may enable L-3 to be cooled at or below its liquid-liquid phase transition temperature range to enable its operation as a draw solution.

[0255] 6A—Heat Releasing Heat Exchange: LL-1 may be heat exchanged with an application requiring heating, a heat sink, or a combination thereof using a heat exchanger (Enthalpy Sink Heat Exchanger). LL-1 may release heat to said application requiring heating, a heat sink, or a combination thereof, while said application requiring heating, a heat sink, or a combination thereof may cool LL-1. Depending on the liquid state of LL-1, the temperature of LL-1, the temperature of the Enthalpy Heat Sink Heat Exchanger, and phase transition properties of LL-1, LL-1 may release heat in the Enthalpy Heat Sink Heat Exchanger due to an enthalpy of liquid-liquid phase transition, or specific heat capacity due to an enthalpy of phase transition, or specific heat capacity or a combination thereof. LL-1 may exit the Enthalpy Sink Heat Exchanger at a lower enthalpy or temperature or a combination thereof state and may comprise at least a portion a single liquid phase combined solution (L-1).Regeneration Portion:1B—Mixing Diluted Draw Solution with Recovered Residual Organic Composition #2 from FO #2: ‘Cold’ diluted Organic Composition #2 draw solution (L-5) may be mixed with an aqueous retentate solution (L-12) from ‘FO #2’ comprising residual organic Composition #2 recovered from L-11, in a mixing device (Mix #3). Said mixing of L-5 and L-12 in Mix #3 may result in a combined solution of L-5 and L-12 (L-6). If desirable, L-6 may comprise a more dilute concentration of organic Composition #2 compared to L-5. If desirable, L-12 and L-6 may contain liquid-liquid phase transition facilitator reagents, or ‘salting-out’ reagents, or phase transition temperature adjustment reagents or a combination thereof to, for example, facilitate liquid-liquid phase transition and / or liquid-liquid separation in, for example, step 2B, or 3B, or 4B, or a combination thereof. If desirable, said liquid-liquid phase transition facilitator reagents, or ‘salting-out’ reagents, or phase transition temperature adjustment reagents or a combination thereof may be rejected by FO #2 in step 6B and may, if desirable, be separate from reagents employed in the Refrigeration Cycle Portion.

[0257] 2B—Preheating Diluted Draw Solution in Heat Exchange: L-6 may be preheated in a heat exchange (Heat Exchanger #3) with ‘warm’ mostly Organic Composition #2 liquid phase (L-8) and ‘warm’ mostly water or other solvent liquid phase (L-9). The pre-heated L-6 (L-7) which may result from the heat exchange in Heat Exchanger #3, may be near, or at, or below or above a liquid-liquid phase transition temperature range of L-7.

[0258] 3B—Liquid-Liquid Phase Transition into Multi-Liquid Phase Mixture: L-7 may be further heated by a heat source (Thermal Source). In Thermal Source, L-7 may be heated such that it undergoes a liquid-liquid phase transition into a multi-liquid phase mixture, LL-4. LL-4 may be near, or at, or above a liquid-liquid phase transition temperature range of L-7.

[0259] 4B—Liquid-Liquid Separation: LL-4 may be separated into non-contiguously separate liquid phases (L-8 and L-9) using a liquid-liquid separation device, LLS-2. L-8 and L-9 may comprise the constituent liquid phases of LL-4. L-8 may comprise mostly Organic Composition #2 and L-9 may comprise mostly water or other solvent or a combination thereof.

[0260] 5B—Cooling Separated Liquid Phases in Heat Exchange: ‘Warm’ L-8 and L-9 may be heat exchanged with ‘Cold’ L-6 in a heat exchanger (Heat Exchanger #3), which may result in cooler temperature L-8 and L-9 (L-10 and L-11) and warmer temperature L-6 (L-7). L-8 and L-9 may be heat exchanged as separate liquid phases to, for example, prevent L-8 and / or L-9 from dissolving in each other, as they may be cooled below a liquid-liquid phase transition temperature while heat exchanged in Heat Exchanger #3. If desirable, L-10 or L-11 may be further cooled before FO, RO, and / or Mix #2. Said further cooling, may include, but is not limited to, one or more or a combination of the following: heat exchange cooling, evaporative cooling, or wet surface air heat exchanger cooling. L-10 may be transferred to step 4A and L-11 may be transferred to Step 5A.FIG. 11:Refrigeration Cycle Portion:1A—Mixing Reagents to Form Endothermic Phase Transition: A solution comprising mostly single liquid phase combined solution (L-2) may be mixed with a solution concentrated in ‘salting-out’ reagent or phase transition temperature adjustment reagent (L-4) in a mixing device (Mix #2). Said mixing of L-4 and L-2 may result in an endothermic liquid-liquid phase transition into a multi-liquid phase mixture. L-4 may dissolve in the aqueous component of L-2, which may result in Organic Composition #1 becoming at least partially insoluble and / or forming a separate liquid phase in a liquid-liquid phase transition. A resulting multi-liquid phase mixture (LL-1) may comprise a mostly Organic Composition #1 liquid phase and an aqueous dilute ‘salting-out’ reagent or mostly phase transition temperature adjustment reagent liquid phase. The previously described liquid-liquid phase transition may be endothermic and may result in the temperature of LL-1 being less than the mean temperature of L-2 and L-4. In some embodiments, step 1A and step 2A may be combined. For example, in some embodiments, Mix #2 may be combined with Heat Exchanger #1.

[0262] 2A—Heat Absorbing Heat Exchange: LL-1 may be heat exchanged (Heat Exchanger #1) with a heat source or an application requiring cooling or an enthalpy source or a combination thereof. LL-1 may absorb heat from or ‘cool’ said heat source or an application requiring cooling or an enthalpy source or a combination thereof, while said heat source or an application requiring cooling or an enthalpy source or a combination thereof may be cooled or supply heat to LL-1. Depending on the liquid state of LL-1, the temperature of LL-1, the temperature of Heat Exchanger #1, and phase transition properties of LL-1, LL-1 may absorb heat in Heat Exchanger #1 due to an enthalpy of liquid-liquid phase transition, or specific heat capacity due to an enthalpy of phase transition, or specific heat capacity or a combination thereof. LL-1 may exit Heat Exchanger #1 at a greater enthalpy or temperature or a combination thereof state and / or may comprise at least a portion a multi-liquid phase solution (LL-2).

[0263] 3A—Liquid-Liquid Separation: LL-2 may be separated into two separate liquid streams using a liquid-liquid separation device (LLS-1). One of the two liquid phases may comprise a mostly organic liquid phase (L-5), such as mostly Organic Composition #1. One of the liquid phases may comprise mostly aqueous dilute ‘salting-out’ reagent or mostly phase transition temperature adjustment reagent solution (L-3).

[0264] 4A—Forward Osmosis Concentrating: Mostly aqueous dilute ‘salting-out’ reagent or mostly phase transition temperature adjustment reagent solution (L-3) may be fed into a forward osmosis or osmotically assisted reverse osmosis or a combination thereof system (FO). L-3 may function as a feed solution, while L-13, which may comprise mostly organic Composition #2, may function as a draw solution. A portion of water or other permeable solvent in L-3 may permeate from L-3 to L-13 across a semi-permeable membrane, while ‘salting-out’ reagent or phase transition temperature adjustment reagent in L-3 may be rejected by said membrane. FO may concentrate L-3 into a retentate solution comprising a concentrated solution of salting-out’ reagent or phase transition temperature adjustment reagent (L-4). FO may dilute L-13 into a diluted solution of organic Composition #2 (L-14), which may have been diluted by FO permeate, which may comprise water and / or other solvent permeate.

[0265] 5A—Heat Exchange to Heat L-5 and L-12 into ‘Warm’ Temperature Zone: ‘Cold’ liquid phase comprising mostly Organic Composition #1 (L-5) and a ‘cold’ liquid phase comprising mostly water or other solvent (L-12) may be heat exchanged (Heat Exchanger #2) with ‘warm’ mostly single liquid phase combined solution (L-1), which may result in ‘warm’ L-5 (L-6) and warm L-12 (L-7) and ‘cold’ L-1 (L-2). L-5 and L-12 may be non-contiguously separate liquid streams during Heat Exchanger #2 to, for example, prevent dissolution of L-5 into L-12 before or during Heat Exchanger #2. L-12 may be purified to remove residual organic Composition #2 and / or other potential contaminants from the Regeneration Portion before or during Heat Exchanger #2 or Mix #1.

[0266] 6A—Mixing Reagents to Form Exothermic Phase Transition: L-6 may be mixed with L-7 in a mixing device, Mix #1, forming L-8. L-7 may be purified to remove residual organic Composition #2 and / or other potential contaminants from the Regeneration Portion before or during Mix #1. Depending on the liquid-liquid phase transition temperature range, the temperature of L-6 and L-7, and the enthalpy of the liquid-liquid phase transition, L-8 may comprise a multi-liquid phase mixture, or a multi-liquid phase mixture with some L-6 dissolved in L-7, or a single liquid phase combined solution.

[0267] 7A—Heat Releasing Heat Exchange: L-8 may be heat exchanged with an application requiring heating, a heat sink, or a combination thereof using a heat exchanger (Heat Exchanger #3). L-8 may release heat to said application requiring heating, a heat sink, or a combination thereof, while said application requiring heating, a heat sink, or a combination thereof may cool L-8. Depending on the liquid state of L-8, the temperature of L-8, the temperature of the Heat Exchanger #3, and phase transition properties of L-8, L-8 may release heat in the Heat Exchanger #3 due to an enthalpy of liquid-liquid phase transition, or specific heat capacity due to an enthalpy of phase transition, or specific heat capacity or a combination thereof. L-8 may exit Heat Exchanger #3 at a lower enthalpy or temperature or a combination thereof state and may comprise at least a portion a single liquid phase combined solution (L-1).

[0268] 8A—Heat Exchange to ‘Cool’ L-1 into ‘Cold’ Temperature Zone: ‘Warm’ mostly single liquid phase combined solution (L-1) may be heat exchanged (Heat Exchanger #2) with a ‘cold’ liquid phase comprising mostly Organic Composition #1 (L-5) and a ‘cold’ liquid phase comprising mostly water or other solvent (L-12), which may result in ‘warm’ L-5 (L-6) and warm L-12 (L-7) and ‘cold’ L-1 (L-2). L-5 and L-12 may be non-contiguously separate liquid streams during Heat Exchanger #2 to, for example, prevent dissolution of L-5 into L-12 before or during Heat Exchanger #2. L-12 may be purified to remove residual organic Composition #2 and / or other potential contaminants from the Regeneration Portion before or during Heat Exchanger #2 or Mix #1.Regeneration Portion:1B—Preheating Diluted Draw Solution in Heat Exchange: ‘Cold’ diluted Organic Composition #2 draw solution (L-14) may be preheated in a heat exchange (Heat Exchanger #4) with ‘warm’ mostly Organic Composition #2 liquid phase (L-11) and ‘warm’ mostly water or other solvent liquid phase (L-10). The pre-heated L-14 (L-9) which may result from the heat exchange in Heat Exchanger #3 may be near, or at, or below or above a liquid-liquid phase transition temperature range of L-9.

[0270] 2B—Liquid-Liquid Phase Transition into Multi-Liquid Phase Mixture: L-9 may be further heated by a heat source (Thermal Source). In Thermal Source, L-9 may be heated such that it undergoes a liquid-liquid phase transition into a multi-liquid phase mixture, LL-3. LL-3 may be near, or at, or above a liquid-liquid phase transition temperature range of L-9.

[0271] 3B—Liquid-Liquid Separation: LL-3 may be separated into non-contiguously separate liquid phases (L-10 and L-11) using a liquid-liquid separation device, LLS-2. L-10 and L-11 may comprise the constituent liquid phases of LL-3. L-11 may comprise mostly Organic Composition #2 and L-10 may comprise mostly water or other solvent or a combination thereof.

[0272] 4B—Cooling Separated Liquid Phases in Heat Exchange: ‘Warm’ L-10 and L-11 may be heat exchanged with ‘Cold’ L-14 in a heat exchange (Heat Exchanger #4), which may result in cooler temperature L-10 and L-11 (L-12 and L-13) and warmer temperature L-14 (L-9). L-10 and L-11 may be heat exchanged as separate liquid phases to, for example, prevent L-10 and / or L-11 from dissolving in each other, as they may be cooled below a liquid-liquid phase transition temperature while heat exchanged in Heat Exchanger #4. If desirable, L-12 or L-13 may be further cooled before contacting or exchanging with the Refrigeration Cycle Portion. For example, if desirable, L-12 or L-13 may be further cooled before Heat Exchanger #2 or FO. Said further cooling, may include, but is not limited to, one or more or a combination of the following: heat exchange cooling, evaporative cooling, or wet surface air heat exchanger cooling. L-12 may be transferred to step 5A and L-13 may be transferred to Step 4A.FIG. 12:Refrigeration Cycle Portion:1A—Mixing Reagents to Form Endothermic Phase Transition: A solution comprising mostly single liquid phase combined solution (L-2) may be mixed with a solution concentrated in ‘salting-out’ reagent or phase transition temperature adjustment reagent (L-4) in a mixing device (Mix #2). Said mixing of L-4 and L-2 may result in an endothermic liquid-liquid phase transition into a multi-liquid phase mixture. L-4 may dissolve in the aqueous component of L-2, which may result in Organic Composition #1 becoming at least partially insoluble and / or forming a separate liquid phase in a liquid-liquid phase transition. A resulting multi-liquid phase mixture (LL-1) may comprise a mostly Organic Composition #1 liquid phase and a aqueous dilute ‘salting-out’ reagent or mostly phase transition temperature adjustment reagent liquid phase. The previously described liquid-liquid phase transition may be endothermic and may result in the temperature of LL-1 being less than the mean temperature of L-2 and L-4. In some embodiments, step 1A and step 2A may be combined. For example, in some embodiments, Mix #2 may be combined with Heat Exchanger #1.

[0274] 2A—Heat Absorbing Heat Exchange: LL-1 may be heat exchanged (Heat Exchanger #1) with a heat source or an application requiring cooling or an enthalpy source or a combination thereof. LL-1 may absorb heat from or ‘cool’ said heat source or an application requiring cooling or an enthalpy source or a combination thereof, while said heat source or an application requiring cooling or an enthalpy source or a combination thereof may be cooled or supply heat to LL-1. Depending on the liquid state of LL-1, the temperature of LL-1, the temperature of Heat Exchanger #1, and phase transition properties of LL-1, LL-1 may absorb heat in Heat Exchanger #1 due to an enthalpy of liquid-liquid phase transition, or specific heat capacity due to an enthalpy of phase transition, or specific heat capacity or a combination thereof. LL-1 may exit Heat Exchanger #1 at a greater enthalpy or temperature or a combination thereof state and / or may comprise at least a portion a multi-liquid phase solution (LL-2).

[0275] 3A—Liquid-Liquid Separation: LL-2 may be separated into two separate liquid streams using a liquid-liquid separation device (LLS-1). One of the two liquid phases may comprise a mostly organic liquid phase (L-5), such as mostly Organic Composition #1. One of the liquid phases may comprise mostly aqueous dilute ‘salting-out’ reagent or phase transition temperature adjustment reagent solution (L-3).

[0276] 4A—Forward Osmosis Concentrating: Mostly aqueous dilute ‘salting-out’ reagent or mostly phase transition temperature adjustment reagent solution (L-3) may be fed into a forward osmosis or osmotically assisted reverse osmosis or a combination thereof system (FO). L-3 may function as a feed solution, while L-15, which may comprise mostly organic Composition #2, may function as a draw solution. A portion of water or other permeable solvent in L-3 may permeate from L-3 to L-15 across a semi-permeable membrane, while ‘salting-out’ reagent or phase transition temperature adjustment reagent in L-3 may be rejected by said membrane. FO may concentrate L-3 into a retentate solution comprising a concentrated solution of salting-out’ reagent or phase transition temperature adjustment reagent (L-4). FO may dilute L-15 into a diluted solution of organic Composition #2 (L-16), which may have been diluted by FO permeate, which may comprise water and / or other solvent permeate.

[0277] 5A—Heat Exchange to Heat L-5 and L-14 into ‘Warm’ Temperature Zone: ‘Cold’ liquid phase comprising mostly Organic Composition #1 (L-5) and a ‘cold’ liquid phase comprising mostly water or other solvent (L-14) may be heat exchanged (Heat Exchanger #2) with ‘warm’ mostly single liquid phase combined solution (L-1), which may result in ‘warm’ L-5 (L-6) and warm L-14 (L-7) and ‘cold’ L-1 (L-2). L-5 and L-14 may be non-contiguously separate liquid streams during Heat Exchanger #2 to, for example, prevent dissolution of L-5 into L-14 before or during Heat Exchanger #2. L-14 may be purified to remove residual organic Composition #2 and / or other potential contaminants from the Regeneration Portion before or during Heat Exchanger #2 or Mix #1.

[0278] 6A—Mixing Reagents to Form Exothermic Phase Transition: L-6 may be mixed with L-7 in a mixing device, Mix #1, forming L-8. L-7 may be purified to remove residual organic Composition #2 and / or other potential contaminants from the Regeneration Portion before or during Mix #1. Depending on the liquid-liquid phase transition temperature range, the temperature of L-6 and L-7, and the enthalpy of the liquid-liquid phase transition, L-8 may comprise a multi-liquid phase mixture, or a multi-liquid phase mixture with some L-6 dissolved in L-7, or a single liquid phase combined solution.

[0279] 7A—Heat Releasing Heat Exchange: L-8 may be heat exchanged with an application requiring heating, a heat sink, or a combination thereof using a heat exchanger (Heat Exchanger #3). L-8 may release heat to said application requiring heating, a heat sink, or a combination thereof, while said application requiring heating, a heat sink, or a combination thereof may cool L-8. Depending on the liquid state of L-8, the temperature of L-8, the temperature of the Heat Exchanger #3, and phase transition properties of L-8, L-8 may release heat in the Heat Exchanger #3 due to an enthalpy of liquid-liquid phase transition, or specific heat capacity due to an enthalpy of phase transition, or specific heat capacity or a combination thereof. L-8 may exit Heat Exchanger #3 at a lower enthalpy or temperature or a combination thereof state and may comprise at least a portion a single liquid phase combined solution (L-1).

[0280] 8A—Heat Exchange to ‘Cool’ L-1 into ‘Cold’ Temperature Zone: ‘Warm’ mostly single liquid phase combined solution (L-1) may be heat exchanged (Heat Exchanger #2) with a ‘cold’ liquid phase comprising mostly Organic Composition #1 (L-5) and a ‘cold’ liquid phase comprising mostly water or other solvent (L-14), which may result in ‘warm’ L-5 (L-6) and warm L-14 (L-7) and ‘cold’ L-1 (L-2). L-5 and L-14 may be non-contiguously separate liquid streams during Heat Exchanger #2 to, for example, prevent dissolution of L-5 into L-14 before or during Heat Exchanger #2. L-14 may be purified to remove residual organic Composition #2 and / or other potential contaminants from the Regeneration Portion before or during Heat Exchanger #2 or Mix #1.Regeneration Portion:1B—Mixing Diluted Draw Solution with Recovered Residual Organic Composition #2 from RO: ‘Cold’ diluted Organic Composition #2 draw solution (L-16) may be mixed with an aqueous retentate solution (L-13) from ‘RO’ comprising residual organic Composition #2 recovered from L-12 in a mixing device (Mix #3). Said mixing of L-16 and L-13 in Mix #3 may result in a combined solution of L-16 and L-13 (L-17). If desirable, L-17 may comprise a more dilute concentration of organic Composition #2 compared to L-16. If desirable, L-13 and L-17 may contain liquid-liquid phase transition facilitator reagents, or ‘salting-out’ reagents, or phase transition temperature adjustment reagents or a combination thereof to, for example, facilitate liquid-liquid phase transition and / or liquid-liquid separation. If desirable, said liquid-liquid phase transition facilitator reagents, or ‘salting-out’ reagents, or phase transition temperature adjustment reagents or a combination thereof may be rejected by RO and may, if desirable, be separate from reagents employed in the Refrigeration Cycle Portion.

[0282] 2B—Preheating Diluted Draw Solution in Heat Exchange: ‘Cold’ diluted Organic Composition #2 draw solution and RO retentate combined solution (L-17) may be preheated in a heat exchange (Heat Exchanger #4) with ‘warm’ mostly Organic Composition #2 liquid phase (L-11) and ‘warm’ mostly water or other solvent liquid phase (L-10). The pre-heated L-17 (L-9) which may result from the heat exchange in Heat Exchanger #3 may be near, or at, or below or above a liquid-liquid phase transition temperature range of L-9.

[0283] 3B—Liquid-Liquid Phase Transition into Multi-Liquid Phase Mixture: L-9 may be further heated by a heat source (Thermal Source). In Thermal Source, L-9 may be heated such that it undergoes a liquid-liquid phase transition into a multi-liquid phase mixture, LL-3. LL-3 may be near, or at, or above a liquid-liquid phase transition temperature range of L-9.

[0284] 4B—Liquid-Liquid Separation: LL-3 may be separated into non-contiguously separate liquid phases (L-10 and L-11) using a liquid-liquid separation device, LLS-2. L-10 and L-11 may comprise the constituent liquid phases of LL-3. L-11 may comprise mostly Organic Composition #2 and L-10 may comprise mostly water or other solvent or a combination thereof.

[0285] 5B—Cooling Separated Liquid Phases in Heat Exchange: ‘Warm’ L-10 and L-11 may be heat exchanged with ‘Cold’ L-17 in a heat exchange (Heat Exchanger #4), which may result in cooler temperature L-10 and L-11 (L-12 and L-15) and warmer temperature L-17 (L-9). L-10 and L-11 may be heat exchanged as separate liquid phases to, for example, prevent L-10 and / or L-11 from dissolving in each other, as they may be cooled below a liquid-liquid phase transition temperature while heat exchanged in Heat Exchanger #4. If desirable, L-12 or L-15 may be further cooled before contacting or exchanging with the Refrigeration Cycle Portion. For example, if desirable, L-12 or L-15 may be further cooled before RO, or Heat Exchanger #2, or FO. Said further cooling, may include, but is not limited to, one or more or a combination of the following: heat exchange cooling, evaporative cooling, or wet surface air heat exchanger cooling. L-12 may be transferred to step 6B and L-15 may be transferred to Step 4A.

[0286] 6B—Reverse Osmosis or Nanofiltration or Ultrafiltration Purification: L-12 may comprise mostly water or other solvent, although may contain residual reagents, which may include, but are not limited to: residual organic Composition #2 and / or phase transition facilitator reagents, or ‘salting-out’ reagents, or phase transition temperature adjustment reagents or a combination thereof. Said residual reagents may be separated from water and / or other solvent. For example, L-12 may comprise a feed solution to a membrane-based process, which may include, but is not limited to, reverse osmosis, or nanofiltration, or ultrafiltration, or forward osmosis, or osmotically assisted reverse osmosis, or a combination thereof process (RO). Said residual reagents may be at least in part rejected by said membrane based process (RO). RO may separate L-12 into a water or other solvent permeate (L-14) and a retentate solution comprising a greater concentration of said residual reagents than L-12 (L-13). L-13 may be transferred to step 1B. L-14 may be transferred to step 5A.FIG. 14Refrigeration Cycle Portion:1A—Mixing Reagents to Form Endothermic Phase Transition: A solution comprising mostly single liquid phase combined solution (L-1) may be mixed with a solution concentrated in ‘salting-out’ reagent or phase transition temperature adjustment reagent (L-4) in a mixing device (Mix #1). Said mixing of L-4 and L-1 may result in an endothermic liquid-liquid phase transition into a multi-liquid phase mixture. L-4 may dissolves in the aqueous component of L-1, which may result in Organic Composition #1 becoming at least partially insoluble and / or forming a separate liquid phase in a liquid-liquid phase transition. A resulting multi-liquid phase mixture (LL-2) may comprise a mostly Organic Composition #1 liquid phase and a aqueous dilute ‘salting-out’ reagent or mostly phase transition temperature adjustment reagent liquid phase. The previously described liquid-liquid phase transition may be endothermic and may result in the temperature of LL-2 being less than the mean temperature of L-1 and L-4. In some embodiments, step 1A and step 2A may be combined. For example, in some embodiments, Mix #1 may be combined with the Enthalpy Source Heat Exchanger.

[0288] 2A—Heat Absorbing Heat Exchange: LL-2 may be heat exchanged (Enthalpy Source Heat Exchanger) with a heat source or an application requiring cooling or an enthalpy source or a combination thereof. LL-2 may absorb heat from or ‘cool’ said heat source or an application requiring cooling or an enthalpy source or a combination thereof, while said heat source or an application requiring cooling or an enthalpy source or a combination thereof may be cooled or supply heat to LL-2. Depending on the liquid state of LL-2, the temperature of LL-2, the temperature of the Enthalpy Heat Source Heat Exchanger, and phase transition properties of LL-2, LL-2 may absorb heat in the Enthalpy Heat Source Heat Exchanger due to an enthalpy of liquid-liquid phase transition, or specific heat capacity due to an enthalpy of phase transition, or specific heat capacity or a combination thereof. LL-2 may exit the Enthalpy Source Heat Exchanger at a greater enthalpy or temperature or a combination thereof state and / or may comprise at least a portion a multi-liquid phase solution (LL-3).

[0289] 3A—Liquid-Liquid Separation: LL-3 may be separated into two separate liquid streams using a liquid-liquid separation device (LLS-1). One of the two liquid phases may comprise a mostly organic liquid phase (L-3), such as mostly Organic Composition #1. One of the liquid phases may comprise mostly aqueous dilute ‘salting-out’ reagent or mostly phase transition temperature adjustment reagent solution (L-2).

[0290] 4A—Forward Osmosis Concentrating: Mostly aqueous dilute ‘salting-out’ reagent or mostly phase transition temperature adjustment reagent solution (L-2) may be fed into a forward osmosis or osmotically assisted reverse osmosis or a combination thereof system (FO). L-2 may function as a feed solution, while L-5, which may comprise mostly brine or high osmotic pressure solution, may function as a draw solution. A portion of water or other permeable solvent in L-2 may permeate from L-2 to L-5 across a semi-permeable membrane, while ‘Salting-out’ reagent or phase transition temperature adjustment reagent in L-2 may be rejected by said membrane. FO may concentrate L-2 into a retentate solution comprising a concentrated solution of salting-out’ reagent or phase transition temperature adjustment reagent (L-4). FO may dilute L-5 into a diluted solution (L-6), which may have been diluted by FO permeate, which may comprise water and / or other solvent permeate.

[0291] 5A—Mixing Reagents to Form Exothermic Phase Transition: L-3, which may comprise a liquid phase comprising mostly organic Composition #1, may be mixed with a solution comprising mostly water, L-7, in a mixing device, Mix #2, forming LL-1. L-7 may be purified to remove potential contaminants before or during Mix #2. Depending on the liquid-liquid phase transition temperature range, the temperature of L-7 and L-3, and the enthalpy of the liquid-liquid phase transition, LL-1 may comprise a multi-liquid phase mixture, or a multi-liquid phase mixture with some L-3 dissolved in L-7, or a single liquid phase combined solution. In some embodiments, step 5A and step 6A may be combined. For example, in some embodiments, Mix #2 may be combined with the Enthalpy Sink Heat Exchanger.

[0292] 6A—Heat Releasing Heat Exchange: LL-1 may be heat exchanged with an application requiring heating, a heat sink, or a combination thereof using a heat exchanger (Enthalpy Sink Heat Exchanger). LL-1 may release heat to said application requiring heating, a heat sink, or a combination thereof, while said application requiring heating, a heat sink, or a combination thereof may cool LL-1. Depending on the liquid state of LL-1, the temperature of LL-1, the temperature of the Enthalpy Heat Sink Heat Exchanger, and phase transition properties of LL-1, LL-1 may release heat in the Enthalpy Heat Sink Heat Exchanger due to an enthalpy of liquid-liquid phase transition, or specific heat capacity due to an enthalpy of phase transition, or specific heat capacity or a combination thereof. LL-1 may exit the Enthalpy Sink Heat Exchanger at a lower enthalpy or temperature or a combination thereof state and may comprise at least a portion a single liquid phase combined solution (L-1).FIG. 16:Refrigeration Cycle Portion:1A—Mixing Reagents to Form Endothermic Phase Transition: A solution comprising mostly single liquid phase combined solution (L-1) may be mixed with a solution concentrated in ‘salting-out’ reagent or phase transition temperature adjustment reagent (L-4) in a mixing device (Mix #1). Said mixing of L-4 and L-1 may result in an endothermic liquid-liquid phase transition into a multi-liquid phase mixture. L-4 may dissolves in the aqueous component of L-1, which may result in Organic Composition #1 becoming at least partially insoluble and / or forming a separate liquid phase in a liquid-liquid phase transition. A resulting multi-liquid phase mixture (LL-2) may comprise a mostly Organic Composition #1 liquid phase and a mostly aqueous dilute ‘salting-out’ reagent liquid phase or mostly phase transition temperature adjustment reagent liquid phase. The previously described liquid-liquid phase transition may be endothermic and may result in the temperature of LL-2 being less than the mean temperature of L-1 and L-4. In some embodiments, step 1A and step 2A may be combined. For example, in some embodiments, Mix #1 may be combined with the Enthalpy Source Heat Exchanger.

[0294] 2A—Heat Absorbing Heat Exchange: LL-2 may be heat exchanged (Enthalpy Source Heat Exchanger) with a heat source or an application requiring cooling or an enthalpy source or a combination thereof. LL-2 may absorb heat from or ‘cool’ said heat source or an application requiring cooling or an enthalpy source or a combination thereof, while said heat source or an application requiring cooling or an enthalpy source or a combination thereof may be cooled or supply heat to LL-2. Depending on the liquid state of LL-2, the temperature of LL-2, the temperature of the Enthalpy Heat Source Heat Exchanger, and phase transition properties of LL-2, LL-2 may absorb heat in the Enthalpy Heat Source Heat Exchanger due to an enthalpy of liquid-liquid phase transition, or specific heat capacity due to an enthalpy of phase transition, or specific heat capacity or a combination thereof. LL-2 may exit the Enthalpy Source Heat Exchanger at a greater enthalpy or temperature or a combination thereof state and / or may comprise at least a portion a multi-liquid phase solution (LL-3).

[0295] 3A—Liquid-Liquid Separation: LL-3 may be separated into two separate liquid streams using a liquid-liquid separation device (LLS-1). One of the two liquid phases may comprise a mostly organic liquid phase (L-3), such as mostly Organic Composition #1. One of the liquid phases may comprise mostly aqueous dilute ‘salting-out’ reagent or mostly phase transition temperature adjustment reagent solution (L-2).

[0296] 4A—Forward Osmosis Concentrating: Mostly aqueous dilute ‘salting-out’ reagent or mostly phase transition temperature adjustment reagent solution (L-2) may be fed into a forward osmosis or osmotically assisted reverse osmosis or a combination thereof system (FO #1). L-2 may function as a feed solution, while L-5, which may comprise Liquid B or brine or high osmotic pressure solution, may function as a draw solution. A portion of water or other permeable solvent in L-2 may permeate from L-2 to L-5 across a semi-permeable membrane, while ‘salting-out’ reagent or phase transition temperature adjustment reagent in L-2 may be rejected by said membrane. FO #1 may concentrate L-2 into a retentate solution comprising a concentrated solution of ‘salting-out’ reagent or phase transition temperature adjustment reagent (L-4). FO #1 may dilute L-5 into a diluted solution (L-6), which may have been diluted by FO permeate, which may comprise water and / or other solvent permeate.

[0297] 5A—FO Mixing Reagents to form Exothermic Phase Transition: L-3, which may comprise a liquid phase comprising mostly organic Composition #1, may comprise a draw solution in a forward osmosis, or osmotically assisted reverse osmosis, or combination thereof process (FO #2). A solution comprising mostly water, L-7, may comprise a feed solution. L-3 may draw water or other permeable solvent from L-7 across a membrane, while said membrane may reject non-permeable residual reagents. During FO #2, L-3 may be diluted to form LL-1 or L-1, which may comprise an exothermic liquid-liquid phase transition. During FO #2, non-permeable reagents in L-7 may be concentrated to form retentate L-8. The present step may enable water to be transferred to the Refrigeration Cycle Portion while preventing the contamination of the Refrigeration Cycle Portion with potential contaminants in L-7. In the present embodiment, it may be desirable to combine step 5A and step 6A. For example, FO #2 may be integrated with the Enthalpy Sink Heat Exchanger, which may enable L-3 to be cooled at or below its liquid-liquid phase transition temperature range to enable its operation as a draw solution.

[0298] 6A—Heat Releasing Heat Exchange: LL-1 may be heat exchanged with an application requiring heating, a heat sink, or a combination thereof using a heat exchanger (Enthalpy Sink Heat Exchanger). LL-1 may release heat to said application requiring heating, a heat sink, or a combination thereof, while said application requiring heating, a heat sink, or a combination thereof may cool LL-1. Depending on the liquid state of LL-1, the temperature of LL-1, the temperature of the Enthalpy Heat Sink Heat Exchanger, and phase transition properties of LL-1, LL-1 may release heat in the Enthalpy Heat Sink Heat Exchanger due to an enthalpy of liquid-liquid phase transition, or specific heat capacity due to an enthalpy of phase transition, or specific heat capacity or a combination thereof. LL-1 may exit the Enthalpy Sink Heat Exchanger at a lower enthalpy or temperature or a combination thereof state and may comprise at least a portion a single liquid phase combined solution (L-1).FIG. 17:Refrigeration Cycle Portion:1A—Mixing Reagents to Form Endothermic Phase Transition: A solution comprising mostly single liquid phase combined solution (L-2) may be mixed with a solution concentrated in ‘salting-out’ reagent or phase transition temperature adjustment reagent (L-4) in a mixing device (Mix #2). Said mixing of L-4 and L-2 may result in an endothermic liquid-liquid phase transition into a multi-liquid phase mixture. L-4 may dissolve in the aqueous component of L-2, which may result in Organic Composition #1 becoming at least partially insoluble and / or forming a separate liquid phase in a liquid-liquid phase transition. A resulting multi-liquid phase mixture (LL-1) may comprise a mostly Organic Composition #1 liquid phase and a aqueous dilute ‘salting-out’ reagent or mostly phase transition temperature adjustment reagent liquid phase. The previously described liquid-liquid phase transition may be endothermic and may result in the temperature of LL-1 being less than the mean temperature of L-2 and L-4. In some embodiments, step 1A and step 2A may be combined. For example, in some embodiments, Mix #2 may be combined with Heat Exchanger #1.

[0300] 2A—Heat Absorbing Heat Exchange: LL-1 may be heat exchanged (Heat Exchanger #1) with a heat source or an application requiring cooling or an enthalpy source or a combination thereof. LL-1 may absorb heat from or ‘cool’ said heat source or an application requiring cooling or an enthalpy source or a combination thereof, while said heat source or an application requiring cooling or an enthalpy source or a combination thereof may be cooled or supply heat to LL-1. Depending on the liquid state of LL-1, the temperature of LL-1, the temperature of Heat Exchanger #1, and phase transition properties of LL-1, LL-1 may absorb heat in Heat Exchanger #1 due to an enthalpy of liquid-liquid phase transition, or specific heat capacity due to an enthalpy of phase transition, or specific heat capacity or a combination thereof. LL-1 may exit Heat Exchanger #1 at a greater enthalpy or temperature or a combination thereof state and / or may comprise at least a portion a multi-liquid phase solution (LL-2).

[0301] 3A—Liquid-Liquid Separation: LL-2 may be separated into two separate liquid streams using a liquid-liquid separation device (LLS-1). One of the two liquid phases may comprise a mostly organic liquid phase (L-5), such as mostly Organic Composition #1. One of the liquid phases may comprise mostly aqueous dilute ‘salting-out’ reagent or phase transition temperature adjustment reagent solution (L-3).

[0302] 4A—Forward Osmosis Concentrating: Mostly aqueous dilute ‘salting-out’ reagent or mostly phase transition temperature adjustment reagent solution (L-3) may be fed into a forward osmosis or osmotically assisted reverse osmosis or a combination thereof system (FO). L-3 may function as a feed solution, while L-10, which may Liquid B, or brine, or high osmotic pressure solution, may function as a draw solution. A portion of water or other permeable solvent in L-3 may permeate from L-3 to L-10 across a semi-permeable membrane, while ‘salting-out’ reagent or phase transition temperature adjustment reagent in L-3 may be rejected by said membrane. FO may concentrate L-3 into a retentate solution comprising a concentrated solution of salting-out’ reagent or phase transition temperature adjustment reagent (L-4). FO may dilute L-10 into a diluted solution (L-11), which may have been diluted by FO permeate, which may comprise water and / or other solvent permeate.

[0303] 5A—Heat Exchange to Heat L-5 and L-9 into ‘Warm’ Temperature Zone: ‘Cold’ liquid phase comprising mostly Organic Composition #1 (L-5) and a ‘cold’ liquid phase comprising mostly water or other solvent (L-9) may be heat exchanged (Heat Exchanger #2) with ‘warm’ mostly single liquid phase combined solution (L-1), which may result in ‘warm’ L-5 (L-6) and warm L-9 (L-7) and ‘cold’ L-1 (L-2). L-5 and L-9 may be non-contiguously separate liquid streams during Heat Exchanger #2 to, for example, prevent dissolution of L-5 into L-9 before or during Heat Exchanger #2. L-9 may be purified to remove potential contaminants from the Regeneration Portion before or during Heat Exchanger #2 or Mix #1. Water from L-9 may be exchanged or added to L-5 by means a ‘FO #2’ system, such as an FO #2 shown in FIG. 5 and / or FIG. 8.

[0304] 6A—Mixing Reagents to Form Exothermic Phase Transition: L-6 may be mixed with L-7 in a mixing device, Mix #1, forming L-8. L-7 may be purified to remove residual organic Composition #2 and / or other potential contaminants from the Regeneration Portion before or during Mix #1. Depending on the liquid-liquid phase transition temperature range, the temperature of L-6 and L-7, and the enthalpy of the liquid-liquid phase transition, L-8 may comprise a multi-liquid phase mixture, or a multi-liquid phase mixture with some L-6 dissolved in L-7, or a single liquid phase combined solution.

[0305] 7A—Heat Releasing Heat Exchange: L-8 may be heat exchanged with an application requiring heating, a heat sink, or a combination thereof using a heat exchanger (Heat Exchanger #3). L-8 may release heat to said application requiring heating, a heat sink, or a combination thereof, while said application requiring heating, a heat sink, or a combination thereof may cool L-8. Depending on the liquid state of L-8, the temperature of L-8, the temperature of the Heat Exchanger #3, and phase transition properties of L-8, L-8 may release heat in the Heat Exchanger #3 due to an enthalpy of liquid-liquid phase transition, or specific heat capacity due to an enthalpy of phase transition, or specific heat capacity or a combination thereof. L-8 may exit Heat Exchanger #3 at a lower enthalpy or temperature or a combination thereof state and may comprise at least a portion a single liquid phase combined solution (L-1).

[0306] 8A—Heat Exchange to ‘Cool’ L-1 into ‘Cold’ Temperature Zone: ‘Warm’ mostly single liquid phase combined solution (L-1) may be heat exchanged (Heat Exchanger #2) with a ‘cold’ liquid phase comprising mostly Organic Composition #1 (L-5) and a ‘cold’ liquid phase comprising mostly water or other solvent (L-14), which may result in ‘warm’ L-5 (L-6) and warm L-9 (L-7) and ‘cold’ L-1 (L-2). L-5 and L-9 may be non-contiguously separate liquid streams during Heat Exchanger #2 to, for example, prevent dissolution of L-5 into L-9 before or during Heat Exchanger #2. L-9 may be purified to remove potential contaminants from the Regeneration Portion before or during Heat Exchanger #2 or Mix #1.Example Figure KeysExample Figure Key FIG. 9Label inFIG.DescriptionL-1L-1 may comprise a solution comprising a combination of OrganicComposition #1 and aqueous liquid phase. L-1 may comprise at least aportion a single liquid phase combined solution. L-1 may comprise LL-1,except after heat removal from LL-1 in, for example, the Enthalpy Heat SinkHeat Exchanger. Heat removed in the Enthalpy Heat Sink HeatExchanger may include, but is not limited to, heat from enthalpy of liquid-liquid phase transition and / or heat from specific heat capacity. L-1 is anoutput of the Enthalpy Sink Heat Exchanger.L-4L-4 may comprise a concentrated solution of ‘salting-out reagent’ or‘concentrate’ or ‘retentate’. L-4 may also comprise some OrganicComposition #1 which may be due to, including, but not limited to, residualfrom L-3 and / or an incomplete separation in LLS-1 and / or residualOrganic Composition #1 dissolved in L-2. L-4 may be generated by ‘FO’.Mix #1Mix #1 may involve mixing or combining L-1 and L-4 to form a multi-liquidphase solution, LL-2. Said mixing may result in a liquid-liquid phasetransition, which may possess an enthalpy of phase transition. Said enthalpyof phase transition may be endothermic or exothermic, although may beendothermic in the present embodiment.LL-2LL-2 may comprise a multi-liquid phase mixture, which may have resultedfrom the mixing of L-1 and L-4. LL-2 may possess a lesser temperatureand / or lesser enthalpy than L-4 and L-1. LL-2 may possess said lessertemperature, due to, for example, an endothermic liquid-liquid phasetransition in Mix #1. LL-2 may possess a latent endothermic enthalpy ofphase transition, which may absorb heat in the Enthalpy Source HeatExchanger. LL-2 may possess a substantially lower temperature than, forexample, ‘Return #2’, and the heat capacity of this substantially lowertemperature may be exploited in the Enthalpy Source Heat Exchanger tocool Return #2 to form Supply #2.EnthalpyThe Enthalpy Source Heat Exchanger may transfer or exchange heat fromSource Heatone or more heat or enthalpy sources to the refrigeration cycle. If theExchangerrefrigeration cycle is being employed as a chiller or air conditioner orcooling device, Return #2 may comprise the load or application requiringcooling, and the Enthalpy Source Heat Exchanger may be employed toenable the refrigeration cycle to absorb heat from the load or ‘cool’ the load.If the refrigeration cycle is being employed as a heat pump or heating device,Return #2 may comprise the enthalpy or heat source, and the EnthalpySource Heat Exchanger may be employed to enable the refrigeration cycle toabsorb heat from this enthalpy or heat source. The Enthalpy Source HeatExchanger transfers heat from Return #2 to LL-2, which may result inSupply #2 (which may possess a cooler temperature or lower enthalpy thanReturn #2) and LL-3 (which may possess a higher temperature or greaterenthalpy than LL-2).LL-3LL-3 may comprise a multi-liquid phase mixture, which may have resultedfrom LL-2 absorbing heat while heat exchanging in the Enthalpy SourceHeat Exchanger. LL-3 may possess a greater temperature or greaterenthalpy or both than LL-2.LLS-1LLS-1 may comprise a liquid-liquid separation device. LLS-1 may separateLL-3 into constituent liquid phases, which may comprise L-2 and L-3.L-2L-2 may comprise a dilute solution of ‘salting-out reagent’. L-2 maycomprise one of the liquid phases separated by LLS-1 from multi-liquidphase mixture LL-3.FO‘FO’ may comprise a forward osmosis or an osmotically assisted reverseosmosis or combination thereof process. ‘FO’ may involve a feed solutioncomprising L-2, which may be concentrated into a concentrate or retentate,L-4. ‘FO’ may involve a draw solution comprising ‘OrganicComposition #2’ (L-9) which, during Forward Osmosis, may be diluted bythe water and / or other liquid flux through the forward osmosis membrane,which may result in a diluted draw solution (L-5).L-3L-3 may comprise a solution comprising mostly ‘Organic Composition #1’.L-3 may comprise one of the liquid phases separated by LLS-1 from multi-liquid phase mixture LL-3.Mix #2Mix #2 may involve mixing or combining L-3 and L-10 to form a multi-liquid phase solution, LL-1, or at least a portion single liquid phasecombined solution, LL-1, or a single liquid phase combined solution, LL-1.L-3 and L-10 may Mix in Mix #2 to form an exothermic or endothermicliquid-liquid phase transition, although in the present embodiment, theliquid-liquid phase transition may form an exothermic phase transition.LL-1LL-1 may comprise a mixture or combination of L-3 and L-10. Dependingon the temperature of L-3 and L-10, LL-1 may combine to form a singleliquid phase combined solution, at least a portion of a single liquid phasecombined solution, or a multi-liquid phase mixture. For example, if L-3 andL-10 combine at a temperature less than their liquid-liquid phase transitiontemperature by a temperature difference greater than the adiabatictemperature change of their enthalpy of phase transition, the LL-1 maycomprise a single liquid phase combined solution at a greater temperaturethan L-3 and / or L-10. For example, if L-3 and L-10 combine at atemperature less than their liquid-liquid phase transition temperature by atemperature difference less than the adiabatic temperature change of theirenthalpy of phase transition, the LL-1 may comprise a portion, but notentirely, a single liquid phase combined solution at a greater temperaturethan L-3 and / or L-10. For example, if L-3 and L-10 combine at atemperature equal to or greater than their liquid-liquid phase transitiontemperature, the LL-1 may comprise a multi-liquid phase mixture.Enthalpy SinkThe Enthalpy Sink Heat Exchanger may transfer or exchange heat from theHeatrefrigeration cycle to one or more heat sinks. If the refrigeration cycle isExchangerbeing employed as a chiller or air conditioner or cooling device, Supply #1may comprise the heat sink or evaporative cooling water supply or air orother heat sink, and the Enthalpy Sink Heat Exchanger may be enable therefrigeration cycle to release or discharge heat into the heat sink. If therefrigeration cycle is being employed as a heat pump or heating device,Supply #1 may comprise the load or application requiring heating, and theEnthalpy Sink Heat Exchanger may enable the refrigeration cycle to supplyheat to this load or application requiring heating. The Enthalpy Sink HeatExchanger transfers heat from LL-1 to Supply #1, which may result inReturn #1 (which may possess a hotter temperature or greater enthalpy thanSupply #1) and L-1 (which may possess a lesser temperature or lesserenthalpy than LL-1).L-5L-5 may comprise a diluted draw solution. L-5 may result from aconcentrated draw solution comprising Organic Composition #2 (L-9)drawing water or other solvent from L-2 through a membrane in ‘FO’. L-5may comprise Organic Composition #2 with significantly more water orother solvent dissolved than L-9. L-5 may be at a temperature significantlyless than the liquid-liquid phase transition temperature range of L-5.L-6L-6 comprises L-5 after heat exchange with L-7 and L-8 in HeatExchanger #3, which may result in L-6 being at a greater temperature thanL-5. L-6 may be at a temperature close to the liquid-liquid phase transitiontemperature range of L-6.HeatHeat Exchanger #3 may comprise a heat exchanger which transfers heatExchanger #3from the components of the dilute draw solution (L-5) followingregeneration and liquid-liquid separation (L-7 and L-8) to L-5. HeatExchanger #3 may pre-heat L-5, forming L-6, which may minimize thermalenergy consumption. Heat Exchanger #3 may enable L-9 and L-10 to be ator near the temperature of the refrigeration cycle, preventing or minimizingheat transfer from the Regeneration Portion into the Refrigeration CyclePortion and minimizing energetic losses. Heat Exchanger #3 may minimizeenergy consumption in the Thermal Source or overall regeneration portion ofthe process by minimizing the relative proportion of heat required forheating the liquid to the liquid-liquid phase transition temperature andmaximizing the relative proportion of heat employed to power or absorbedby the liquid-liquid phase transition from L-6 to LL-4. Heat Exchanger #3may enable L-7 and L-8 to be cooled while preventing L-7 and L-8 fromdissolving in each other, by, for example, ensuring L-7 and L-8 are non-contiguously separate during cooling.ThermalThermal Source may comprise a heat exchanger to supply heat to L-6 aboveSourcethe liquid-liquid phase transition temperature of L-6. Thermal Source heatsup L-6 to at or above its liquid-liquid phase transition temperature range.L-6 may absorb said heat and may undergo an endothermic liquid-liquidphase transition into a multi-liquid phase mixture, LL-4.LL-4LL-4 may comprise L-6 following an endothermic phase transition inThermal Source, due to, for example, heat supplied in Thermal Source.LL-4 may comprising a multi-liquid phase mixture with two or more liquidphases. One of the liquid phases may comprise a solution comprising mostlyOrganic Composition #2. One of the liquid phases may comprise a solutioncomprising mostly water or other solvent or a combination thereof.LLS-2LLS-2 may comprise a liquid-liquid separation device. LLS-2 may separateLL-4 into its constituent liquid phases, which may comprise a solutioncomprising mostly Organic Composition #2 (L-7) and / or a solutioncomprising mostly water or other solvent or a combination thereof (L-8).LLS-2 separates LL-4 into L-7 and L-8. L-7 and L-8 may comprise non-contiguously separated streams before Heat Exchanger #3. It may bedesirable for L-7 and L-8 to be non-contiguously separated streams beforeHeat Exchanger #3 to prevent them from dissolving in each other (whichmay occur if mixed in Heat Exchanger #3, because Heat Exchanger #3 maycool the L-7 and L-8 to less than their liquid-liquid phase transitiontemperature range.L-7L-7 may comprise a liquid phase separated from multi-liquid phase mixture,LL-4 by liquid-liquid separation device, LLS-2. L-7 may comprise asolution comprising mostly ‘Organic Composition #2’. Before HeatExchanger #3, L-7 may be at a temperature near, at, or above the liquid-liquid phase transition temperature range of L-6.L-8L-8 may comprise a liquid phase separated from multi-liquid phase mixture,LL-4 by liquid-liquid separation device, LLS-2. L-8 may comprise asolution comprising mostly water or other solvent or a combination thereof.L-8 may be at a temperature near, at, or above the liquid-liquid phasetransition temperature range of L-6.L-9L-9 may comprise L-7 after heat exchanging with L-5 in Heat Exchanger #3.L-9 may be at a substantially lesser temperature than L-7. L-9 may comprisea solution comprising mostly ‘Organic Composition #2’. L-9 may comprisea draw solution in ‘FO’.L-10L-10 may comprise L-8 after heat exchanging with L-5 in HeatExchanger #3. L-10 may be at a substantially lesser temperature than L-8.L-10 may comprise a solution comprising mostly water or other solvent or acombination thereof. L-10 may comprise regenerated water or other solventor a combination thereof which may have been previously drawn from orremoved from the Refrigeration Cycle Portion in FO.Supply #1Supply #1 may comprise a cooler temperature or lower enthalpy or both heattransfer fluid or material than Return #1. Supply #1 may comprise anapplication requiring heating or a heat sink or an enthalpy sink or acombination thereof, for example, before absorbing heat in a heat exchange.Return #1Return #1 may comprise a warmer temperature or greater enthalpy or bothheat transfer fluid or material than Supply #1. Return #1 may comprise anapplication requiring heating or a heat sink or an enthalpy sink or acombination thereof, for example, after absorbing heat in a heat exchange.Supply #2Supply #2 may comprise a cooler temperature or lower enthalpy or both heattransfer fluid or material than Return #2. Supply #2 may comprise anapplication requiring cooling or a heat source or an enthalpy source or acombination thereof, for example, after discharging heat in a heat exchange.Return #2Return #2 may comprise a warmer temperature or greater enthalpy or bothheat transfer fluid or material than Supply #2. Return #2 may comprise anapplication requiring cooling or a heat source or an enthalpy source or acombination thereof, for example, before discharging heat in a heatexchange.Example Figure Key for FIG. 10Label inFIG.DescriptionL-1L-1 may comprise a solution comprising a combination of OrganicComposition #1 and aqueous liquid phase. L-1 may comprise at least aportion a single liquid phase combined solution. L-1 may comprise LL-1,except after heat removal from LL-1 in, for example, the Enthalpy Heat SinkHeat Exchanger. Heat removed in the Enthalpy Heat Sink HeatExchanger may include, but is not limited to, heat from enthalpy of liquid-liquid phase transition and / or heat from specific heat capacity. L-1 is anoutput of the Enthalpy Sink Heat Exchanger.L-4L-4 may comprise a concentrated solution of ‘salting-out reagent’ or‘concentrate’ or ‘retentate’. The concentrate may be generated by forwardosmosis, ‘FO’.Mix #1Mix #1 may involve mixing or combining L-1 and L-4 to form a multi-liquidphase solution, LL-2. Said mixing may result in a liquid-liquid phasetransition, which may possess an enthalpy of phase transition. Said enthalpyof phase transition may be endothermic or exothermic, although may beendothermic in the present embodiment.LL-2LL-2 may comprise a multi-liquid phase mixture, which may have resultedfrom the mixing of L-1 and L-4. LL-2 may possess a lesser temperatureand / or lesser enthalpy than L-4 and L-1. LL-2 may possess said lessertemperature, due to, for example, an endothermic liquid-liquid phasetransition in Mix #1. LL-2 may possess a latent endothermic enthalpy ofphase transition, which may absorb heat in the Enthalpy Source HeatExchanger. LL-2 may possess a substantially lower temperature than, forexample, ‘Return #2’, and the heat capacity of this substantially lowertemperature may be exploited in the Enthalpy Source Heat Exchanger tocool Return #2 to form Supply #2.EnthalpyThe Enthalpy Source Heat Exchanger may transfer or exchange heat fromSource Heatone or more heat or enthalpy sources to the refrigeration cycle. If theExchangerrefrigeration cycle is being employed as a chiller or air conditioner orcooling device, Return #2 may comprise the load or application requiringcooling, and the Enthalpy Source Heat Exchanger may be employed toenable the refrigeration cycle to absorb heat from the load or ‘cool’ the load.If the refrigeration cycle is being employed as a heat pump or heating device,Return #2 may comprise the enthalpy or heat source, and the EnthalpySource Heat Exchanger may be employed to enable the refrigeration cycle toabsorb heat from this enthalpy or heat source. The Enthalpy Source HeatExchanger transfers heat from Return #2 to LL-2, which may result inSupply #2 (which may possess a cooler temperature or lower enthalpy thanReturn #2) and LL-3 (which may possess a higher temperature or greaterenthalpy than LL-2).LL-3LL-3 may comprise a multi-liquid phase mixture, which may have resultedfrom LL-2 absorbing heat while heat exchanging in the Enthalpy SourceHeat Exchanger. LL-3 may possess a greater temperature or greaterenthalpy or both than LL-2.LLS-1LLS-1 may comprise a liquid-liquid separation device. LLS-1 may separateLL-3 into its constituent liquid phases, which may comprise L-2 and L-3.L-2L-2 may comprise a dilute solution of ‘salting-out reagent’. L-2 maycomprise one of the liquid phases separated by LLS-1 from multi-liquidphase mixture LL-3.FO‘FO’ may comprise a forward osmosis or an osmotically assisted reverseosmosis or combination thereof process. ‘FO’ may involve a feed solutioncomprising L-2, which may be concentrated into a concentrate or retentate,L-4. ‘FO’ may involve a draw solution comprising ‘OrganicComposition #2’ (L-10) which, during Forward Osmosis, may be diluted bythe water and / or other liquid flux through a forward osmosis membrane,which may result in a diluted draw solution (L-5).L-3L-3 may comprise a solution comprising mostly ‘Organic Composition #1’.L-3 may comprise one of the liquid phases separated by LLS-1 from multi-liquid phase mixture LL-3.Mix #2Mix #2 may involve mixing or combining L-3 and L-13 to form a multi-liquid phase solution, LL-1, or at least a portion single liquid phasecombined solution, LL-1, or a single liquid phase combined solution, LL-1.L-3 and L-13 may Mix in Mix #2 to form an exothermic or endothermicliquid-liquid phase transition, although in the present embodiment, theliquid-liquid phase transition may form an exothermic phase transition.LL-1LL-1 may comprise a mixture or combination of L-3 and L-13. Dependingon the temperature of L-3 and L-13, LL-1 may combine to form a singleliquid phase combined solution, at least a portion of a single liquid phasecombined solution, or a multi-liquid phase mixture. For example, if L-3 andL-13 combine at a temperature less than their liquid-liquid phase transitiontemperature by a temperature difference greater than the adiabatictemperature change of their enthalpy of phase transition, the LL-1 maycomprise a single liquid phase combined solution at a greater temperaturethan L-3 and / or L-13. For example, if L-3 and L-13 combine at atemperature less than their liquid-liquid phase transition temperature by atemperature difference less than the adiabatic temperature change of theirenthalpy of phase transition, the LL-1 may comprise a portion, but notentirely, a single liquid phase combined solution at a greater temperaturethan L-3 and / or L-13. For example, if L-3 and L-13 combine at atemperature equal to or greater than their liquid-liquid phase transitiontemperature, the LL-1 may comprise a multi-liquid phase mixture.Enthalpy SinkThe Enthalpy Sink Heat Exchanger may transfer or exchange heat from theHeatrefrigeration cycle to one or more heat sinks. If the refrigeration cycle isExchangerbeing employed as a chiller or air conditioner or cooling device, Supply #1may comprise the heat sink or evaporative cooling water supply or air orother heat sink, and the Enthalpy Sink Heat Exchanger may be enable therefrigeration cycle to release or discharge heat into the heat sink. If therefrigeration cycle is being employed as a heat pump or heating device,Supply #1 may comprise the load or application requiring heating, and theEnthalpy Sink Heat Exchanger may enable the refrigeration cycle to supplyheat to this load or application requiring heating. The Enthalpy Sink HeatExchanger transfers heat from LL-1 to Supply #1, which may result inReturn #1 (which may possess a hotter temperature or greater enthalpy thanSupply #1) and L-1 (which may possess a lesser temperature or lesserenthalpy than LL-1).L-5L-5 may comprise a diluted draw solution. L-5 may result from aconcentrated draw solution comprising Organic Composition #2 (L-10)drawing water or other solvent from L-2 through a membrane in ‘FO’. L-5may comprise Organic Composition #2 with significantly more water orother solvent dissolved than L-10. L-5 may be at a temperature significantlyless than the liquid-liquid phase transition temperature range of L-5.Mix #3Mix #3 may involve mixing or combining L-5 and L-12 to form a combinedsolution (L-6). Mix #3 may involve integrating reverse osmosis retentate(L-12) into the diluted draw solution (L-5) before the draw solutionregeneration. L-12 may comprise residual Organic Composition #2 in L-11,which may have been separated or recovered by RO.L-6L-6 may comprise a combined solution of L-5 and L-12. L-6 may be at atemperature significantly less than the liquid-liquid phase transitiontemperature range of L-6.HeatHeat Exchanger #3 may comprise a heat exchanger which transfers heatExchanger #3from the components of the dilute draw solution following regeneration andliquid-liquid separation (L-8 and L-9) to L-6. Heat Exchanger #3 may pre-heat L-6, forming L-7, which may minimize thermal energy consumption.Heat Exchanger #3 may enable L-10 and L-11 to be at or near thetemperature of the refrigeration cycle, preventing or minimizing heat transferfrom the Regeneration Portion into the Refrigeration Cycle Portion andminimizing energetic losses.L-7L-7 comprises L-6 after heat exchange with L-8 and L-9 in HeatExchanger #3, which may result in L-7 being at a greater temperature thanL-6. L-7 may be at a temperature close to the liquid-liquid phase transitiontemperature range of L-7.ThermalThermal Source may comprise a heat exchanger to supply heat to L-7 near,Sourceat, or above the liquid-liquid phase transition temperature range of L-7.Thermal Source may heat up L-7 to at or above its liquid-liquid phasetransition temperature range. L-7 may absorb said heat and may undergo anendothermic liquid-liquid phase transition into a multi-liquid phase mixture,LL-4.LL-4LL-4 may comprise L-7 following an endothermic phase transition inThermal Source, due to, for example, heat supplied in Thermal Source.LL-4 may comprising a multi-liquid phase mixture with two or more liquidphases. One of the liquid phases may comprise a solution comprising mostlyOrganic Composition #2. One of the liquid phases may comprise a solutioncomprising mostly water or other solvent or a combination thereof.LLS-2LLS-2 may comprise a liquid-liquid separation device. LLS-2 may separateLL-4 into its constituent liquid phases, which may comprise a solutioncomprising mostly Organic Composition #2 (L-8) and / or a solutioncomprising mostly water or other solvent or a combination thereof (L-9).LLS-2 separates LL-4 into L-8 and L-9. L-8 and L-9 may comprise non-contiguously separated streams before Heat Exchanger #3. It may bedesirable for L-8 and L-9 to be non-contiguously separated streams beforeHeat Exchanger #3 to prevent them from dissolving in each other (whichmay occur if mixed in Heat Exchanger #3, because Heat Exchanger #3 maycool the L-8 and L-9 to a temperature less than their liquid-liquid phasetransition temperature range).L-8L-8 may comprise a liquid phase separated from multi-liquid phase mixture,LL-4 by liquid-liquid separation device, LLS-2. L-8 may comprise asolution comprising mostly ‘Organic Composition #2’. Before HeatExchanger #3, L-8 may be at a temperature near, at, or above the liquid-liquid phase transition temperature range of L-7.L-9L-9 may comprise a liquid phase separated from multi-liquid phase mixture,LL-4 by liquid-liquid separation device, LLS-2. L-9 may comprise asolution comprising mostly water or other solvent or a combination thereof.L-9 may be at a temperature near, at, or above the liquid-liquid phasetransition temperature range of L-7.L-10L-10 may comprise L-8 after heat exchanging with L-6 in HeatExchanger #3. L-10 may be at a substantially lesser temperature than L-8.L-10 may comprise a solution comprising mostly ‘Organic Composition #2’.L-10 may comprise a draw solution in ‘FO’L-11L-11 may comprise L-9 after heat exchanging with L-6 in HeatExchanger #3. L-11 may be at a substantially lesser temperature than L-9.L-11 may comprise a solution comprising mostly water or other solvent or acombination thereof. L-11 may comprise regenerated water or other solventor a combination thereof which may have been previously drawn from orremoved from the Refrigeration Cycle Portion in FO. L-11 may containresidual Organic Composition #2, which may be removed or recovered in,for example, ‘RO’, before returning said regenerated water to theRefrigeration Cycle Portion.RORO may comprise reverse osmosis or nanofiltration or other membrane-based process or separation process or a combination thereof. RO mayinvolve separating residual Organic Composition #2 from L-11. Separatingresidual Organic Composition #2 may prevent contamination of theRefrigeration Cycle Portion with Organic Composition #2. RO may separateL-11 into a concentrate or retentate stream, which may comprise a portionOrganic Composition #2 (L-12), and a permeate stream, which maycomprise a mostly water or other solvent (L-13). It may be desirable for therecovery ratio or recovery rate, or the percentage of the mass of L-11 whichis in the permeate, to be greater than or equal to, including, but not limitedto, one or more or a combination of the following: 10%, or 20%, or 30%, or40%, or 50%, or 60%, or 70%, or 80%, or 90%, or 95%.L-12L-12 may comprise retentate or concentrate from RO. L-12 may comprise asolution with residual Organic Composition #2 separated from L-11.L-13L-13 may comprise permeate from RO. L-13 may comprise mostly water orother solvent. L-13 may comprise water or other solvent originallytransferred from the Refrigeration Cycle Portion to the Regeneration Portionduring FO. L-13 may comprise regenerated water or other solvent returnedto the Refrigeration Cycle Portion from the Regeneration Portion. L-13 maybe mixed with L-3 in Mix #2.Supply #1Supply #1 may comprise a cooler temperature or lower enthalpy or both heattransfer fluid or material than Return #1. Supply #1 may comprise anapplication requiring heating or a heat sink or an enthalpy sink or acombination thereof, for example, before absorbing heat in a heat exchange.Return #1Return #1 may comprise a warmer temperature or greater enthalpy or bothheat transfer fluid or material than Supply #1. Return #1 may comprise anapplication requiring heating or a heat sink or an enthalpy sink or acombination thereof, for example, after absorbing heat in a heat exchange.Supply #2Supply #2 may comprise a cooler temperature or lower enthalpy or both heattransfer fluid or material than Return #2. Supply #2 may comprise anapplication requiring cooling or a heat source or an enthalpy source or acombination thereof, for example, after discharging heat in a heat exchange.Return #2Return #2 may comprise a warmer temperature or greater enthalpy or bothheat transfer fluid or material than Supply #2. Return #2 may comprise anapplication requiring cooling or a heat source or an enthalpy source or acombination thereof, for example, before discharging heat in a heatexchange.Example Figure Key for FIG. 13Label inFIG.DescriptionL-1L-1 may comprise a solution comprising a combination of OrganicComposition #1 and aqueous liquid phase. L-1 may comprise at least aportion a single liquid phase combined solution. L-1 may comprise LL-1,except after heat removal from LL-1 in, for example, the Enthalpy Heat SinkHeat Exchanger. Heat removed in the Enthalpy Heat Sink HeatExchanger may include, but is not limited to, heat from enthalpy of liquid-liquid phase transition and / or heat from specific heat capacity. L-1 is anoutput of the Enthalpy Sink Heat Exchanger.L-4L-4 may comprise a concentrated solution of ‘salting-out reagent’ or‘concentrate’ or ‘retentate’. The concentrate may be generated by forwardosmosis, ‘FO #1’Mix #1Mix #1 may involve mixing or combining L-1 and L-4 to form a multi-liquidphase solution, LL-2. Said mixing may result in a liquid-liquid phasetransition, which may possess an enthalpy of phase transition. Said enthalpyof phase transition may be endothermic or exothermic, although may beendothermic in the present embodiment.LL-2LL-2 may comprise a multi-liquid phase mixture, which may have resultedfrom the mixing of L-1 and L-4. LL-2 may possess a lesser temperatureand / or lesser enthalpy than L-4 and L-1. LL-2 may possess said lessertemperature, due to, for example, an endothermic liquid-liquid phasetransition in Mix #1. LL-2 may possess a latent endothermic enthalpy ofphase transition, which may absorb heat in the Enthalpy Source HeatExchanger. LL-2 may possess a substantially lower temperature than, forexample, ‘Return #2’, and the heat capacity of this substantially lowertemperature may be exploited in the Enthalpy Source Heat Exchanger tocool Return #2 to form Supply #2.EnthalpyThe Enthalpy Source Heat Exchanger may transfer or exchange heat fromSource Heatone or more heat or enthalpy sources to the refrigeration cycle. If theExchangerrefrigeration cycle is being employed as a chiller or air conditioner orcooling device, Return #2 may comprise the load or application requiringcooling, and the Enthalpy Source Heat Exchanger may be employed toenable the refrigeration cycle to absorb heat from the load or ‘cool’ the load.If the refrigeration cycle is being employed as a heat pump or heating device,Return #2 may comprise the enthalpy or heat source, and the EnthalpySource Heat Exchanger may be employed to enable the refrigeration cycle toabsorb heat from this enthalpy or heat source. The Enthalpy Source HeatExchanger transfers heat from Return #2 to LL-2, which may result inSupply #2 (which may possess a cooler temperature or lower enthalpy thanReturn #2) and LL-3 (which may possess a higher temperature or greaterenthalpy than LL-2).LL-3LL-3 may comprise a multi-liquid phase mixture, which may have resultedfrom LL-2 absorbing heat while heat exchanging in the Enthalpy SourceHeat Exchanger. LL-3 may possess a greater temperature or greaterenthalpy or both than LL-2.LLS-1LLS-1 may comprise a liquid-liquid separation device. LLS-1 may separateLL-3 into its constituent liquid phases, which may comprise L-2 and L-3.L-2L-2 may comprise a dilute solution of ‘salting-out reagent’. L-2 maycomprise one of the liquid phases separated by LLS-1 from multi-liquidphase mixture LL-3.FO #1‘FO #1’ may comprise a forward osmosis or an osmotically assisted reverseosmosis or combination thereof process. ‘FO #1’ may involve a feedsolution comprising L-2, which may be concentrated into a concentrate orretentate, L-4. ‘FO #1’ may involve a draw solution comprising ‘OrganicComposition #2’ (L-10) which, during Forward Osmosis, may be diluted bythe water and / or other liquid flux through the forward osmosis membrane,which may result in a diluted draw solution (L-5).L-3L-3 may comprise a solution comprising mostly ‘Organic Composition #1’.L-3 may comprise one of the liquid phases separated by LLS-1 from multi-liquid phase mixture LL-3.LL-1LL-1 may comprise a diluted solution of L-3 or a multi-liquid phase mixtureor both. For example, L-3 may have been employed as a draw solution inFO #2. Water or other solvent from L-11 may have permeated one or moremembranes in FO #2, which may result in a diluted solution of L-3. L-3may be cooled using, for example, a heat sink or the enthalpy sink heatexchanger before or during FO #2, to, for example, maximize the solubilityof water or osmotic pressure of L-3 or both. FO #2 may be combined withthe enthalpy source heat exchanger.Enthalpy SinkThe Enthalpy Sink Heat Exchanger may transfer or exchange heat from theHeatrefrigeration cycle to one or more heat sinks. If the refrigeration cycle isExchangerbeing employed as a chiller or air conditioner or cooling device, Supply #1may comprise the heat sink or evaporative cooling water supply or air orother heat sink, and the Enthalpy Sink Heat Exchanger may be enable therefrigeration cycle to release or discharge heat into the heat sink. If therefrigeration cycle is being employed as a heat pump or heating device,Supply #1 may comprise the load or application requiring heating, and theEnthalpy Sink Heat Exchanger may enable the refrigeration cycle to supplyheat to this load or application requiring heating. The Enthalpy Sink HeatExchanger transfers heat from LL-1 to Supply #1, which may result inReturn #1 (which may possess a hotter temperature or greater enthalpy thanSupply #1) and L-1 (which may possess a lesser temperature or lesserenthalpy than LL-1).L-5L-5 may comprise a diluted draw solution. L-5 may result from aconcentrated draw solution comprising Organic Composition #2 (L-10)drawing water or other solvent from L-2 through a membrane in ‘FO’. L-5may comprise Organic Composition #2 with significantly more water orother solvent dissolved than L-10. L-5 may be at a temperature significantlyless than the liquid-liquid phase transition temperature range of L-5.Mix #3Mix #3 may involve mixing or combining L-5 and L-12 to form a combinedsolution (L-6). Mix #3 may involve integrating forward osmosis orosmotically assisted reverse osmosis (FO #2) retentate (L-12) into the diluteddraw solution (L-5) before the draw solution regeneration. L-12 maycomprise residual Organic Composition #2 in L-11, which may have beenseparated or recovered by FO or osmotically assisted RO (FO #2).L-6L-6 may comprise a combined solution of L-5 and L-12. L-6 may be at atemperature significantly less than the liquid-liquid phase transitiontemperature range of L-6.HeatHeat Exchanger #3 may comprise a heat exchanger which transfers heatExchanger #3from the components of the dilute draw solution following regeneration andliquid-liquid separation (L-8 and L-9) to L-6. Heat Exchanger #3 may pre-heat L-6, forming L-7, which may minimize thermal energy consumption.Heat Exchanger #3 may enable L-10 and L-11 to be at or near thetemperature of the refrigeration cycle, preventing or minimizing heat transferfrom the Regeneration Portion into the Refrigeration Cycle Portion andminimizing energetic losses.L-7L-7 comprises L-6 after heat exchange with L-8 and L-9 in HeatExchanger #3, which may result in L-7 being at a greater temperature thanL-6. L-7 may be at a temperature close to the liquid-liquid phase transitiontemperature range of L-7.ThermalThermal Source may comprise a heat exchanger to supply heat to L-7 near,Sourceat, or above the liquid-liquid phase transition temperature range of L-7.Thermal Source may heat up L-7 to at or above its liquid-liquid phasetransition temperature range. L-7 may absorb said heat and may undergo anendothermic liquid-liquid phase transition into a multi-liquid phase mixture,LL-4.LL-4LL-4 may comprise L-7 following an endothermic phase transition inThermal Source, due to, for example, heat supplied in Thermal Source.LL-4 may comprising a multi-liquid phase mixture with two or more liquidphases. One of the liquid phases may comprise a solution comprising mostlyOrganic Composition #2. One of the liquid phases may comprise a solutioncomprising mostly water or other solvent or a combination thereof.LLS-2LLS-2 may comprise a liquid-liquid separation device. LLS-2 may separateLL-4 into its constituent liquid phases, which may comprise a solutioncomprising mostly Organic Composition #2 (L-8) and / or a solutioncomprising mostly water or other solvent or a combination thereof (L-9).LLS-2 separates LL-4 into L-8 and L-9. L-8 and L-9 may comprise non-contiguously separated streams before Heat Exchanger #3. It may bedesirable for L-8 and L-9 to be non-contiguously separated streams beforeHeat Exchanger #3 to prevent them from dissolving in each other (whichmay occur if mixed in Heat Exchanger #3, because Heat Exchanger #3 maycool the L-8 and L-9 to a temperature less than their liquid-liquid phasetransition temperature range).L-8L-8 may comprise a liquid phase separated from multi-liquid phase mixture,LL-4 by liquid-liquid separation device, LLS-2. L-8 may comprise asolution comprising mostly ‘Organic Composition #2’. Before HeatExchanger #3, L-8 may be at a temperature near, at, or above the liquid-liquid phase transition temperature range of L-7.L-9L-9 may comprise a liquid phase separated from multi-liquid phase mixture,LL-4 by liquid-liquid separation device, LLS-2. L-9 may comprise asolution comprising mostly water or other solvent or a combination thereof.L-9 may be at a temperature near, at, or above the liquid-liquid phasetransition temperature range of L-7.L-10L-10 may comprise L-8 after heat exchanging with L-6 in HeatExchanger #3. L-10 may be at a substantially lesser temperature than L-8.L-10 may comprise a solution comprising mostly ‘Organic Composition #2’.L-10 may comprise a draw solution in ‘FO’.L-11L-11 may comprise L-9 after heat exchanging with L-6 in HeatExchanger #3. L-11 may be at a substantially lesser temperature than L-9.L-11 may comprise a solution comprising mostly water or other solvent or acombination thereof. L-11 may comprise regenerated water or other solventor a combination thereof which may have been previously drawn from orremoved from the Refrigeration Cycle Portion in FO #1. L-11 may containresidual Organic Composition #2, which may be removed or recovered in,for example, ‘FO #2’. Water in L-11 may be returned to the RefrigerationCycle Portion by FO #2, wherein water may transfer through a membranefrom L-11 to L-3, which may result in a retentate (L-12) and diluted L-3(LL-1).FO #2FO #2 may comprise a forward osmosis or osmotically assisted reverseosmosis process. FO #2 may involve passing L-11 across a membrane andL-3 across the opposite side of a membrane. Due to osmotic pressure orhydraulic pressure or both, water or other solvent may pass through themembrane from L-11 to L-3, which may result in diluted L-3 or a multi-liquid phase mixture or both (LL-1) and concentrated L-11 residual reagents(L-12). FO #2 may enable water or other solvent from L-11 to be transferredfrom L-11 to L-3 while preventing the transfer of non-water or non-solventresidual reagents from L-11 or the Regeneration Portion into L-3 or theRefrigeration Cycle portion. Advantageously, FO #2 may enable at least aportion of the energy for returning water to the Refrigeration Cycle portionfrom the Regeneration portion, while minimizing contamination of theRefrigeration Cycle portion, to be provided by internal osmotic pressuredifferences rather than electricity or other potentially more costly energysource. FO #2 may be integrated or combined with the Enthalpy Sink HeatExchanger. For example, a portion of or all the Enthalpy Sink HeatExchanger may be placed before or during FO #2.FO #2 may involve separating residual Organic Composition #2 from L-11.Separating residual Organic Composition #2 may prevent contamination ofthe Refrigeration Cycle Portion with Organic Composition #2. It may bedesirable for the recovery ratio or recovery rate, or the percentage of L-11which is in LL-1, to be greater than or equal to, including, but not limited to,one or more or a combination of the following: 10%, or 20%, or 30%, or40%, or 50%, or 60%, or 70%, or 80%, or 90%, or 95%.FO #2 may involve mixing or combining L-3 and L-11 to form a multi-liquid phase solution, LL-1, or at least a portion single liquid phasecombined solution, LL-1, or a single liquid phase combined solution, LL-1.A portion of L-3 and L-11 may combine in FO #2 to form an exothermic orendothermic liquid-liquid phase transition, although in the presentembodiment, the liquid-liquid phase transition may form an exothermicphase transition.L-12L-12 may comprise retentate or concentrate from FO #2. L-12 maycomprise a solution with residual Organic Composition #2 separated fromL-11.Supply #1Supply #1 may comprise a cooler temperature or lower enthalpy or both heattransfer fluid or material than Return #1. Supply #1 may comprise anapplication requiring heating or a heat sink or an enthalpy sink or acombination thereof, for example, before absorbing heat in a heat exchange.Return #1Return #1 may comprise a warmer temperature or greater enthalpy or bothheat transfer fluid or material than Supply #1. Return #1 may comprise anapplication requiring heating or a heat sink or an enthalpy sink or acombination thereof, for example, after absorbing heat in a heat exchange.Supply #2Supply #2 may comprise a cooler temperature or lower enthalpy or both heattransfer fluid or material than Return #2. Supply #2 may comprise anapplication requiring cooling or a heat source or an enthalpy source or acombination thereof, for example, after discharging heat in a heat exchange.Return #2Return #2 may comprise a warmer temperature or greater enthalpy or bothheat transfer fluid or material than Supply #2. Return #2 may comprise anapplication requiring cooling or a heat source or an enthalpy source or acombination thereof, for example, before discharging heat in a heatexchange.Example Figure Key for FIG. 11Label inFIG.DescriptionL-1L-1 may comprise a solution comprising a combination of OrganicComposition #1 and aqueous liquid phase. L-1 may comprise at least aportion a single liquid phase combined solution. L-1 may comprise L-8,except after heat removal from L-8 in, for example, the Heat Exchanger #3.Heat removed in the Heat Exchanger #3 may include, but is not limited to,heat from enthalpy of liquid-liquid phase transition and / or heat fromspecific heat capacity. L-1 is an output of Heat Exchanger #3.HeatHeat Exchanger #2 may involve a heat exchange between ‘warm’ L-1 andExchanger #2‘cold’ L-12 and L-5, which may result in ‘cold’ L-1 and ‘warm’ L-12 andL-5. L-12 and L-5 may be heat exchanged with L-1 in Heat Exchanger #2 asnon-contiguously separate liquid phases to, for example, prevent L-12 andL-5 from dissolving in each other and / or releasing an enthalpy of phasetransition during Heat Exchanger #2. Heat Exchanger #2 may enable twoseparate temperature zones within the Refrigeration Cycle portion of theprocess. For example, L-6, L-7, Mix #1, L-8, Heat Exchanger #3, and L-1may comprise a first temperature zone, while L-2, Mix #2, LL-1, HeatExchanger #1, LL-2. LLS-1, L-3, L-4, and L-5 may comprise a secondtemperature zone which may be at a significantly different temperature ortemperature range than the first temperature zone. Said significantlydifferent temperature may comprise a temperature difference greater than theadiabatic temperature change of the enthalpy of the liquid-liquid phasetransition. Said temperature zones may enable the refrigeration cycle tomove heat or pump heat across a temperature difference greater than theadiabatic temperature change of the enthalpy of liquid-liquid phasetransition.L-2L-2 may comprise L-1 after heat exchange in Heat Exchanger #2. L-2 maybe at a significantly different temperature than L-1, such as, for example, atemperature difference greater than the adiabatic temperature change of theliquid-liquid phase transition of Organic Composition #1 and water.Mix #2Mix #1 may involve mixing or combining L-2 and L-4 to form a multi-liquidphase solution, LL-1. Said mixing may result in a liquid-liquid phasetransition, which may possess an enthalpy of phase transition. Said enthalpyof phase transition may be endothermic or exothermic, although may beendothermic in the present embodiment.L-4L-4 may comprise a concentrated solution of ‘salting-out reagent’ or‘concentrate’ or ‘retentate’. L-4 may also comprise some OrganicComposition #1 which may be due to, including, but not limited to, residualfrom L-3 and / or an incomplete separation in LLS-1 and / or residualOrganic Composition #1 dissolved in L-3. The concentrate may begenerated by forward osmosis, ‘FO’.LL-1LL-1 may comprise a multi-liquid phase mixture, which may have resultedfrom the mixing of L-2 and L-4 in Mix #2. LL-1 may possess a lessertemperature and / or lesser enthalpy than L-4 and L-2. LL-1 may possess saidlesser temperature, due to, for example, an endothermic liquid-liquid phasetransition in Mix #2. LL-1 may possess a latent endothermic enthalpy ofphase transition, which may absorb heat in Heat Exchanger #1. LL-1 maypossess a lesser temperature than LL-2, which may enable the absorption ofheat in Heat Exchanger #1 due to specific heat capacity.HeatHeat Exchanger #1 may comprise a heat exchanger between LL-1 and anExchanger #1application requiring cooling or a heat source or enthalpy source. LL-1 mayabsorb heat in a heat exchange with an application requiring cooling or aheat source or enthalpy source, which may result in a higher temperatureand / or enthalpy LL-1 (for example: LL-2) and a lower temperature and / orless enthalpy application requiring cooling or heat source or enthalpy source.LL-2LL-2 may comprise the same overall composition as LL-1, except at a highertemperature and / or greater enthalpy. LL-2 may comprise LL-1 after heatexchanging in Heat Exchanger #1. LL-2 may comprise at least a portion amulti-liquid phase mixture. It may be desirable for at least one liquid phaseof said multi-liquid phase mixture to comprise mostly OrganicComposition #1. It may be desirable for at least one liquid phase of saidmulti-liquid phase mixture to comprise mostly water or a dilute aqueoussolution of ‘salting-out’ reagent.LLS-1LLS-1 may comprise a liquid-liquid separation device. LLS-1 may separateLL-2 into constituent liquid phases, which may comprise L-3 and L-5.L-3L-3 may comprise a dilute solution of ‘salting-out reagent’. L-3 maycomprise an aqueous solution. L-3 may comprise one of the liquid phasesseparated by LLS-1 from multi-liquid phase mixture LL-2. L-3 maycomprise residual Organic Composition #1, which may be due to, forexample, an incomplete separation in LLS-1 and / or residual OrganicComposition #1 dissolved in L-3.L-5L-5 may comprise a solution comprising mostly ‘Organic Composition #1’.L-5 may comprise one of the liquid phases separated by LLS-1 from multi-liquid phase mixture LL-2. L-5 may comprise residual water and / or ‘salting-out’ reagent, which may be due to, for example, an incomplete separation inLLS-1 and / or residual water and / or ‘salting-out’ reagent dissolved in L-5.FO‘FO’ may comprise a forward osmosis or an osmotically assisted reverseosmosis or combination thereof process. ‘FO’ may involve a feed solutioncomprising L-3, which may be concentrated into a concentrate or retentate,L-4. ‘FO’ may involve a draw solution comprising ‘OrganicComposition #2’ (L-13) which, during Forward Osmosis, may be diluted bywater and / or other liquid flux through the forward osmosis membrane,which may result in a diluted draw solution (L-14).L-6L-6 may comprise L-5 after heat exchange in Heat Exchanger #2. L-6 maybe at a significantly different temperature than L-5, such as, for example, atemperature difference greater than the adiabatic temperature change of theliquid-liquid phase transition of Organic Composition #1 and water. L-6may be non-contiguously separate from L-7.L-7L-7 may comprise L-12 after heat exchange in Heat Exchanger #2. L-7 maybe at a significantly different temperature than L-12, such as, for example, atemperature difference greater than the adiabatic temperature change of theliquid-liquid phase transition of Organic Composition #1 and water. L-7may be non-contiguously separate from L-6.Mix #1Mix #1 may involve mixing or combining L-6 and L-7 to form, including,but not limited to, one or more or a combination of the following: a multi-liquid phase solution, L-8, or at least a portion single liquid phase combinedsolution, L-8, or a single liquid phase combined solution, L-8. L-6 and L-7may Mix in Mix #1 to form an exothermic or endothermic liquid-liquidphase transition, although the present embodiment may form an exothermicphase transition. It may be desirable for the adiabatic temperature change ofsaid enthalpy of said liquid-liquid phase transition to be greater than theapproach temperature and / or heat exchanger Delta-T of Heat Exchanger #2.L-8L-8 may comprise a combination of L-6 and L-7. L-8 may compriseincluding, but not limited to, one or more or a combination of the following:a multi-liquid phase solution, or at least a portion single liquid phasecombined solution, or a single liquid phase combined solution. L-8 may beat a greater temperature and / or greater enthalpy than L-1.HeatHeat Exchanger #3 may involve heat exchanging L-8 with an applicationExchanger #3requiring heating or a heat sink or a cold source, which may result in a lessertemperature and / or lesser enthalpy L-8 (for example: L-1) and a greatertemperature and / or greater enthalpy application requiring heating or a heatsink or a cold source.L-9L-9 may comprise L-14 after heat exchange with L-10 and L-11 in HeatExchanger #4, which may result in L-9 being at a greater temperature thanL-14. L-9 may be at a temperature close to the liquid-liquid phase transitiontemperature range of L-9.ThermalThermal Source may comprise a heating source or a cooling source. If theSourceRegeneration Portion comprises a LCST, Thermal Source may comprise aheating source or enthalpy source or heat addition heat exchange. If theRegeneration Portion comprises a UCST, Thermal Source may comprise acooling source or heat sink or heat removal heat exchange.LL-3LL-3 may comprise L-9 following an endothermic phase transition inThermal Source, due to, for example, heat supplied in Thermal Source.LL-3 may comprise a multi-liquid phase mixture with two or more liquidphases. One of the liquid phases may comprise a solution comprising mostlyOrganic Composition #2. One of the liquid phases may comprise a solutioncomprising mostly water or other solvent or a combination thereof.LLS-2LLS-2 may comprise a liquid-liquid separation device. LLS-2 may separateLL-3 into its constituent liquid phases, which may comprise a solutioncomprising mostly Organic Composition #2 (L-11) and / or a solutioncomprising mostly water or other solvent or a combination thereof (L-10).LLS-2 separates LL-3 into L-10 and L-11. L-10 and L-11 may comprisenon-contiguously separated streams before Heat Exchanger #4. It may bedesirable for L-10 and L-11 to be non-contiguously separated streams beforeHeat Exchanger #4 to, for example, prevent L-10 and L-11 from dissolvingin each other (which may occur if mixed in Heat Exchanger #4, becauseHeat Exchanger #4 may cool L-10 and L-11 to less than their liquid-liquidphase transition temperature range).L-10L-10 may comprise a liquid phase separated from multi-liquid phasemixture, LL-3, by a liquid-liquid separation device, LLS-2. L-10 maycomprise a solution comprising mostly water or other solvent or acombination thereof. L-10 may be at a temperature near, at, or above theliquid-liquid phase transition temperature range of L-9.L-11L-11 may comprise a liquid phase separated from multi-liquid phasemixture, LL-3 by a liquid-liquid separation device, LLS-2. L-11 maycomprise a solution comprising mostly ‘Organic Composition #2’. BeforeHeat Exchanger #4, L-11 may be at a temperature near, at, or above theliquid-liquid phase transition temperature range of L-9.HeatHeat Exchanger #4 may comprise a heat exchanger which transfers heatExchanger #4from the components of the dilute draw solution (L-14) followingregeneration and liquid-liquid separation (L-10 and L-11) to L-14. HeatExchanger #4 may pre-heat L-14, forming L-9, which may minimize thermalenergy consumption. Heat Exchanger #4 may enable L-12 and L-13 to be ator near the temperature of the refrigeration cycle, preventing or minimizingheat transfer from the Regeneration Portion into the Refrigeration CyclePortion and minimizing energetic losses. Heat Exchanger #4 may minimizeenergy consumption in the Thermal Source or overall regeneration portion ofthe process by minimizing the relative proportion of heat required forheating the liquid to the liquid-liquid phase transition temperature andmaximizing the relative proportion of heat employed to power or absorbedby the liquid-liquid phase transition from L-9 to LL-3. Heat Exchanger #4may enable L-10 and L-11 to be cooled while preventing L-10 and L-11from dissolving in each other, by, for example, ensuring L-10 and L-11 arenon-contiguously separate during cooling.L-12L-12 may comprise mostly water and / or other solvent which may have atsome point passed through a membrane during ‘FO’ from the RefrigerationCycle Portion of the process to the Regeneration Portion of the process.L-12 may comprise the returning of said water and / or other solvent to theRefrigeration Cycle Portion following regeneration of said water and / orother solvent in the Regeneration Portion. L-12 may contain residualOrganic Composition #2, which may be, if desired, partially or completelyremoved to, for example, prevent contamination of the Refrigeration CyclePortion with Organic Composition #2. L-12 (or L-7) may serve a functionalrole as the water and / or other solvent which may be mixed with L-6 to forma heat of phase transition, such as an exothermic enthalpy of mixing. Saidexothermic enthalpy of phase transition may comprise at least a portion ofthe heat pumped or moved from Heat Exchanger #1 to Heat Exchanger #3.L-13L-13 may comprise L-11 after heat exchanging with L-14 in HeatExchanger #4. L-13 may be at a substantially lesser temperature than L-11.L-13 may comprise a solution comprising mostly ‘Organic Composition #2’.L-13 may comprise a draw solution in ‘FO’.L-14L-14 may comprise a diluted draw solution. L-14 may result from aconcentrated draw solution comprising Organic Composition #2 (L-14)drawing water or other solvent from L-3 through a membrane in ‘FO’. L-14may comprise Organic Composition #2 with significantly more water orother solvent dissolved than L-13. L-14 may be at a temperaturesignificantly less than a liquid-liquid phase transition temperature range ofL-14.Example Figure Key for FIG. 12Label inFIG.DescriptionL-1L-1 may comprise a solution comprising a combination of OrganicComposition #1 and aqueous liquid phase. L-1 may comprise at least aportion a single liquid phase combined solution. L-1 may comprise L-8,except after heat removal from L-8 in, for example, the Heat Exchanger #3.Heat removed in Heat Exchanger #3 may include, but is not limited to, heatfrom enthalpy of liquid-liquid phase transition and / or heat from specificheat capacity. L-1 may be an output of Heat Exchanger #3.HeatHeat Exchanger #2 may involve a heat exchange between ‘warm’ L-1 andExchanger #2‘cold’ L-14 and L-5, which may result in ‘cold’ L-1 and ‘warm’ L-14 andL-5 (L-7 and L-6, respectively). L-14 and L-5 may be heat exchanged withL-1 in Heat Exchanger #2 as non-contiguously separate liquid phases to, forexample, prevent L-14 and L-5 from dissolving in each other and / orreleasing an enthalpy of phase transition during Heat Exchanger #2. HeatExchanger #2 may enable two separate temperature zones within theRefrigeration Cycle portion of the process. For example, L-6, L-7, Mix #1,L-8, Heat Exchanger #3, and L-1 may comprise a first temperature zone,while L-2, Mix #2, LL-1, Heat Exchanger #1, LL-2. LLS-1, L-3, L-4, andL-5 may comprise a second temperature zone which may be at asignificantly different temperature or temperature range than the firsttemperature zone. Said significantly different temperature may comprise atemperature difference greater than the adiabatic temperature change of theenthalpy of the liquid-liquid phase transition. Said temperature zones mayenable the refrigeration cycle to move heat or pump heat across atemperature difference greater than the adiabatic temperature change of theenthalpy of liquid-liquid phase transition.L-2L-2 may comprise L-1 after heat exchange in Heat Exchanger #2. L-2 maybe at a significantly different temperature than L-1, such as, for example, atemperature difference greater than the adiabatic temperature change of theliquid-liquid phase transition of Organic Composition #1 and water.Mix #2Mix #1 may involve mixing or combining L-2 and L-4 to form a multi-liquidphase solution, LL-1. Said mixing may result in a liquid-liquid phasetransition, which may possess an enthalpy of phase transition. Said enthalpyof phase transition may be endothermic or exothermic, although may beendothermic in the present embodiment.L-4L-4 may comprise a concentrated solution of ‘salting-out reagent’ or‘concentrate’ or ‘retentate’. L-4 may further comprise some OrganicComposition #1 which may be due to, including, but not limited to, residualfrom L-3 and / or an incomplete separation in LLS-1 and / or residualOrganic Composition #1 dissolved in L-3. The concentrate may begenerated by forward osmosis, ‘FO’.LL-1LL-1 may comprise a multi-liquid phase mixture, which may have resultedfrom the mixing of L-2 and L-4 in Mix #2. LL-1 may possess a lessertemperature and / or lesser enthalpy than L-4 and L-2. LL-1 may possess saidlesser temperature, due to, for example, an endothermic liquid-liquid phasetransition in Mix #2. LL-1 may possess a latent endothermic enthalpy ofphase transition, which may absorb heat in Heat Exchanger #1. LL-1 maypossess a lesser temperature than LL-2, which may enable the absorption ofheat in Heat Exchanger #1 due to specific heat capacity.HeatHeat Exchanger #1 may comprise a heat exchanger between LL-1 and anExchanger #1application requiring cooling or a heat source or enthalpy source. LL-1 mayabsorb heat in a heat exchange with an application requiring cooling or aheat source or enthalpy source, which may result in a higher temperatureand / or enthalpy LL-1 (for example: LL-2) and a lower temperature and / orless enthalpy application requiring cooling or heat source or enthalpy source.LL-2LL-2 may comprise the same overall composition as LL-1, except at a highertemperature and / or greater enthalpy. LL-2 may comprise LL-1 after heatexchanging in Heat Exchanger #1. LL-2 may comprise at least a portion amulti-liquid phase mixture. It may be desirable for at least one liquid phaseof said multi-liquid phase mixture to comprise mostly OrganicComposition #1. It may be desirable for at least one liquid phase of saidmulti-liquid phase mixture to comprise mostly water or a dilute aqueoussolution of ‘salting-out’ reagent.LLS-1LLS-1 may comprise a liquid-liquid separation device. LLS-1 may separateLL-2 into constituent liquid phases, which may comprise L-3 and L-5.L-3L-3 may comprise a dilute solution of ‘salting-out reagent’. L-3 maycomprise an aqueous solution or mostly water or other solvent solution. L-3may comprise one of the liquid phases separated by LLS-1 from multi-liquidphase mixture LL-2. L-3 may comprise residual Organic Composition #1,which may be due to, for example, an incomplete separation in LLS-1and / or residual Organic Composition #1 dissolved in L-3.L-5L-5 may comprise a solution comprising mostly ‘Organic Composition #1’.L-5 may comprise one of the liquid phases separated by LLS-1 from multi-liquid phase mixture LL-2. L-5 may further comprise residual water and / or‘salting-out’ reagent, which may be due to, for example, an incompleteseparation in LLS-1 and / or residual water and / or ‘salting-out’ reagentdissolved in L-5.FO‘FO’ may comprise a forward osmosis or an osmotically assisted reverseosmosis or combination thereof process. ‘FO’ may involve a feed solutioncomprising L-3, which may be concentrated into a concentrate or retentate,L-4. ‘FO’ may involve a draw solution comprising ‘OrganicComposition #2’ (L-15) which, during Forward Osmosis, may be diluted bywater and / or other liquid flux through the forward osmosis membrane,which may result in a diluted draw solution (L-16).L-6L-6 may comprise L-5 after heat exchange in Heat Exchanger #2. L-6 maybe at a significantly different temperature than L-5, such as, for example, atemperature difference greater than the adiabatic temperature change of theliquid-liquid phase transition of Organic Composition #1 and water. L-6may be non-contiguously separate from L-7.L-7L-7 may comprise L-14 after heat exchange in Heat Exchanger #2. L-7 maybe at a significantly different temperature than L-12, such as, for example, atemperature difference greater than the adiabatic temperature change of theliquid-liquid phase transition of Organic Composition #1 and water. L-7may be non-contiguously separate from L-6.Mix #1Mix #1 may involve mixing or combining L-6 and L-7 to form, including,but not limited to, one or more or a combination of the following: a multi-liquid phase solution, L-8, or at least a portion single liquid phase combinedsolution, L-8, or a single liquid phase combined solution, L-8. L-6 and L-7may Mix in Mix #1 to form an exothermic or endothermic liquid-liquidphase transition, although the present embodiment may form an exothermicphase transition. It may be desirable for the adiabatic temperature change ofsaid enthalpy of said liquid-liquid phase transition to be greater than theapproach temperature and / or heat exchanger Delta-T of Heat Exchanger #2.L-8L-8 may comprise a combination of L-6 and L-7. L-8 may compriseincluding, but not limited to, one or more or a combination of the following:a multi-liquid phase solution, or at least a portion single liquid phasecombined solution, or a single liquid phase combined solution. L-8 may beat a greater temperature and / or greater enthalpy than L-1.HeatHeat Exchanger #3 may involve heat exchanging L-8 with an applicationExchanger #3requiring heating or a heat sink or a cold source, which may result in a lessertemperature and / or lesser enthalpy L-8 (for example: L-1) and a greatertemperature and / or greater enthalpy application requiring heating or a heatsink or a cold source.L-9L-9 may comprise L-17 after heat exchange with L-10 and L-11 in HeatExchanger #4, which may result in L-9 being at a greater temperature thanL-17. L-9 may be at a temperature close to the liquid-liquid phase transitiontemperature range of L-9.ThermalThermal Source may comprise a heating source or a cooling source. If theSourceRegeneration Portion comprises a LCST, Thermal Source may comprise aheating source or enthalpy source or heat addition heat exchange. If theRegeneration Portion comprises a UCST, Thermal Source may comprise acooling source or heat sink or heat removal heat exchange.LL-3LL-3 may comprise L-9 following an endothermic phase transition inThermal Source, due to, for example, heat supplied in Thermal Source.LL-3 may comprise a multi-liquid phase mixture with two or more liquidphases. One of the liquid phases may comprise a solution comprising mostlyOrganic Composition #2. One of the liquid phases may comprise a solutioncomprising mostly water or other solvent or a combination thereof.LLS-2LLS-2 may comprise a liquid-liquid separation device. LLS-2 may separateLL-3 into its constituent liquid phases, which may comprise a solutioncomprising mostly Organic Composition #2 (L-11) and / or a solutioncomprising mostly water or other solvent or a combination thereof (L-10).LLS-2 separates LL-3 into L-10 and L-11. L-10 and L-11 may comprisenon-contiguously separated streams before Heat Exchanger #4. It may bedesirable for L-10 and L-11 to be non-contiguously separated streams beforeHeat Exchanger #4 to, for example, prevent L-10 and L-11 from dissolvingin each other (which may occur if mixed in Heat Exchanger #4, becauseHeat Exchanger #4 may cool L-10 and L-11 to less than their liquid-liquidphase transition temperature range).L-10L-10 may comprise a liquid phase separated from multi-liquid phasemixture, LL-3, by a liquid-liquid separation device, LLS-2. L-10 maycomprise a solution comprising mostly water or other solvent or acombination thereof. L-10 may be at a temperature near, at, or above theliquid-liquid phase transition temperature range of L-9.L-11L-11 may comprise a liquid phase separated from multi-liquid phasemixture, LL-3 by a liquid-liquid separation device, LLS-2. L-11 maycomprise a solution comprising mostly ‘Organic Composition #2’. BeforeHeat Exchanger #4, L-11 may be at a temperature near, at, or above theliquid-liquid phase transition temperature range of L-9.HeatHeat Exchanger #4 may comprise a heat exchanger which transfers heatExchanger #4from the components of the dilute draw solution (L-17) followingregeneration and liquid-liquid separation (L-10 and L-11) to L-17. HeatExchanger #4 may pre-heat L-17, forming L-9, which may minimize thermalenergy consumption. Heat Exchanger #4 may enable L-12 and L-15 to be ator near the temperature of the refrigeration cycle, preventing or minimizingheat transfer from the Regeneration Portion into the Refrigeration CyclePortion and minimizing energetic losses. Heat Exchanger #4 may minimizeenergy consumption in the Thermal Source or overall Regeneration Portionof the process by minimizing the relative proportion of heat employed forheating the liquid to the liquid-liquid phase transition temperature andmaximizing the relative proportion of heat employed to power or absorbedby the liquid-liquid phase transition from L-9 to LL-3. Heat Exchanger #4may enable L-10 and L-11 to be cooled while preventing L-10 and L-11from dissolving in each other, by, for example, ensuring L-10 and L-11 arenon-contiguously separate during cooling.L-12L-12 may comprise mostly water and / or other solvent which may have atsome point passed through a membrane during ‘FO’ from the RefrigerationCycle Portion of the process to the Regeneration Portion of the process.L-12 may contain residual Organic Composition #2, which may be, ifdesired, partially or completely removed using, for example, ‘RO’, to, forexample, prevent contamination of the Refrigeration Cycle Portion withOrganic Composition #2. L-12 may comprise a feed solution to ‘RO’.RORO may comprise reverse osmosis or nanofiltration or other membrane-based process or separation process or a combination thereof. RO mayinvolve separating residual Organic Composition #2 from L-12. Separatingresidual Organic Composition #2 may prevent contamination of theRefrigeration Cycle Portion with Organic Composition #2. RO may separateL-12 into a concentrate or retentate stream, which may comprise a portionOrganic Composition #2 (L-13), and a permeate stream, which maycomprise a mostly water or other solvent (L-14). It may be desirable for therecovery ratio or recovery rate, or the percentage of the mass of L-12 whichis in the permeate, to be greater than or equal to, including, but not limitedto, one or more or a combination of the following: 10%, or 20%, or 30%, or40%, or 50%, or 60%, or 70%, or 80%, or 90%, or 95%.L-13L-13 may comprise retentate or concentrate from RO. L-13 may comprise asolution with residual Organic Composition #2 separated from L-12.L-14L-14 may comprise permeate from RO. L-14 may comprise mostly water orother solvent. L-14 may comprise a lesser concentration of OrganicComposition #2 than L-12. L-14 may comprise water or other solventoriginally transferred from the Refrigeration Cycle Portion to theRegeneration Portion during FO. L-14 may comprise regenerated water orother solvent returned to the Refrigeration Cycle Portion from theRegeneration Portion. L-14 (or L-7) may serve a functional role as the waterand / or other solvent which may be mixed with L-6 to form a heat of phasetransition, such as an exothermic enthalpy of mixing. Said exothermicenthalpy of phase transition may comprise at least a portion of the heatpumped or moved from Heat Exchanger #1 to Heat Exchanger #3.L-15L-15 may comprise L-11 after heat exchanging with L-17 in HeatExchanger #4. L-15 may be at a substantially lesser temperature than L-11.L-15 may comprise a solution comprising mostly ‘Organic Composition #2’.L-15 may comprise a draw solution in ‘FO’.L-16L-16 may comprise a diluted draw solution. L-16 may result from aconcentrated draw solution comprising Organic Composition #2 (L-15)drawing water or other solvent from L-3 through a membrane in ‘FO’. L-16may comprise Organic Composition #2 with significantly more water orother solvent dissolved than L-15. L-16 may be at a temperaturesignificantly less than a liquid-liquid phase transition temperature range ofL-16.Mix #3Mix #3 may involve mixing or combining L-13 and L-16 to form acombined solution (L-17). Mix #3 may involve integrating reverse osmosisretentate (L-13) into the diluted draw solution (L-16) before the drawsolution regeneration. L-13 may comprise residual Organic Composition #2in L-12, which may have been separated or recovered by RO.L-17L-17 may comprise a combined solution of L-13 and L-16. L-17 may be at atemperature significantly less than the liquid-liquid phase transitiontemperature range of L-17. L-17 may possess a lesser mass concentration ofresidual Organic Composition #2 and a greater mass concentration of wateror other solvent than L-16. L-17 may possess more favorable liquid-liquidphase transition properties than L-16.Example Figure Key FIG. 14Label inFIG.DescriptionL-1L-1 may comprise a solution comprising a combination of OrganicComposition #1 and aqueous liquid phase. L-1 may comprise at least aportion a single liquid phase combined solution. L-1 may comprise LL-1,except after heat removal from LL-1 in, for example, the Enthalpy Heat SinkHeat Exchanger. Heat removed in the Enthalpy Heat Sink HeatExchanger may include, but is not limited to, heat from enthalpy of liquid-liquid phase transition and / or heat from specific heat capacity. L-1 is anoutput of the Enthalpy Sink Heat Exchanger.L-4L-4 may comprise a concentrated solution of ‘salting-out reagent’ or‘concentrate’ or ‘retentate’. L-4 may also comprise some OrganicComposition #1 which may be due to, including, but not limited to, residualfrom L-3 and / or an incomplete separation in LLS-1 and / or residualOrganic Composition #1 dissolved in L-2. L-4 may be generated by ‘FO’.Mix #1Mix #1 may involve mixing or combining L-1 and L-4 to form a multi-liquidphase solution, LL-2. Said mixing may result in a liquid-liquid phasetransition, which may possess an enthalpy of phase transition. Said enthalpyof phase transition may be endothermic or exothermic, although may beendothermic in the present embodiment.LL-2LL-2 may comprise a multi-liquid phase mixture, which may have resultedfrom the mixing of L-1 and L-4. LL-2 may possess a lesser temperatureand / or lesser enthalpy than L-4 and L-1. LL-2 may possess said lessertemperature, due to, for example, an endothermic liquid-liquid phasetransition in Mix #1. LL-2 may possess a latent endothermic enthalpy ofphase transition, which may absorb heat in the Enthalpy Source HeatExchanger. LL-2 may possess a substantially lower temperature than, forexample, ‘Return #2’, and the heat capacity of this substantially lowertemperature may be exploited in the Enthalpy Source Heat Exchanger tocool Return #2 to form Supply #2.EnthalpyThe Enthalpy Source Heat Exchanger may transfer or exchange heat fromSource Heatone or more heat or enthalpy sources to the refrigeration cycle. If theExchangerrefrigeration cycle is being employed as a chiller or air conditioner orcooling device, Return #2 may comprise the load or application requiringcooling, and the Enthalpy Source Heat Exchanger may be employed toenable the refrigeration cycle to absorb heat from the load or ‘cool’ the load.If the refrigeration cycle is being employed as a heat pump or heating device,Return #2 may comprise the enthalpy or heat source, and the EnthalpySource Heat Exchanger may be employed to enable the refrigeration cycle toabsorb heat from this enthalpy or heat source. The Enthalpy Source HeatExchanger transfers heat from Return #2 to LL-2, which may result inSupply #2 (which may possess a cooler temperature or lower enthalpy thanReturn #2) and LL-3 (which may possess a higher temperature or greaterenthalpy than LL-2).LL-3LL-3 may comprise a multi-liquid phase mixture, which may have resultedfrom LL-2 absorbing heat while heat exchanging in the Enthalpy SourceHeat Exchanger. LL-3 may possess a greater temperature or greaterenthalpy or both than LL-2.LLS-1LLS-1 may comprise a liquid-liquid separation device. LLS-1 may separateLL-3 into constituent liquid phases, which may comprise L-2 and L-3.L-2L-2 may comprise a dilute solution of ‘salting-out reagent’. L-2 maycomprise one of the liquid phases separated by LLS-1 from multi-liquidphase mixture LL-3. L-2 may comprise a feed solution into ‘FO’.L-5L-5 may comprise a draw solution in ‘FO’. L-5 may comprise aconcentrated brine or other solution with a large osmotic pressure. L-5 maydesirably have an osmotic pressure greater than L-2 or L-4. Alternatively,L-5 may have an osmotic pressure near, at, or less than the osmotic pressureof L-4, and FO may comprise an osmotically assisted reverse osmosissystem. L-5 may comprise, for example, including, but not limited to, one ormore or a combination of the following: sugar water, concentrate, juiceconcentrate, syrup concentrate, malt concentrate, beverage concentrate,seawater, brackish water, saline water, evaporation pond brine, brine fromhypersaline lake, brine from saline aquifer, saline brine from underground,reverse osmosis brine, evaporator brine, cryodesalination brine, or frackwater brine.FO‘FO’ may comprise a forward osmosis or an osmotically assisted reverseosmosis or combination thereof process. ‘FO’ may involve a feed solutioncomprising L-2, which may be concentrated into a concentrate or retentate,L-4. ‘FO’ may involve a draw solution comprising ‘Brine’ (L-5) which,during Forward Osmosis, may be diluted by the water and / or other liquidflux through a ‘FO’ membrane, which may result in a diluted draw solutionor ‘Dilute Brine’ (L-6).L-6L-6 may comprise diluted draw solution (for example: diluted L-5)following forward osmosis or osmotically assisted reverse osmosis in ‘FO’.L-6 may be returned to the original source of L-5. Alternatively, L-6 maycomprise a valuable byproduct, for example, which may include, but is notlimited to, one or more or a combination of the following: a feedstock for abeverage, or a feedstock for brewery, or feedstock to a fermentation process,or a drilling fluid feedstock, or a antifreeze solution. The water permeatinginto L-5 during ‘FO’ to form L-6 may comprise a similar or the same massof water added to the process in L-7.L-3L-3 may comprise a solution comprising mostly ‘Organic Composition #1’.L-3 may comprise one of the liquid phases separated by LLS-1 from multi-liquid phase mixture LL-3.L-7L-7 may comprise freshwater input. Freshwater input may undergotreatment to remove or minimize potential contaminants or foulants. Ifnecessary, said treatment may be conducted, for example, before Mix #2.Mix #2Mix #2 may involve mixing or combining L-3 and L-7 to form a multi-liquidphase solution, LL-1, or at least a portion single liquid phase combinedsolution, LL-1, or a single liquid phase combined solution, LL-1. L-3 andL-7 may Mix in Mix #2 to form an exothermic or endothermic liquid-liquidphase transition, although in the present embodiment, the liquid-liquid phasetransition may form an exothermic phase transition.LL-1LL-1 may comprise a mixture or combination of L-3 and L-7. Depending onthe temperature of L-3 and L-7, LL-1 may combine to form a single liquidphase combined solution, at least a portion of a single liquid phase combinedsolution, or a multi-liquid phase mixture. For example, if L-3 and L-7combine at a temperature less than their liquid-liquid phase transitiontemperature by a temperature difference greater than the adiabatictemperature change of their enthalpy of phase transition, the LL-1 maycomprise a single liquid phase combined solution at a greater temperaturethan L-3 and / or L-7. For example, if L-3 and L-7 combine at a temperatureless than their liquid-liquid phase transition temperature by a temperaturedifference less than the adiabatic temperature change of their enthalpy ofphase transition, the LL-1 may comprise a portion, but not entirely, a singleliquid phase combined solution at a greater temperature than L-3 and / orL-7. For example, if L-3 and L-7 combine at a temperature equal to orgreater than their liquid-liquid phase transition temperature, the LL-1 maycomprise a multi-liquid phase mixture.Enthalpy SinkThe Enthalpy Sink Heat Exchanger may transfer or exchange heat from theHeatrefrigeration cycle to one or more heat sinks. If the refrigeration cycle isExchangerbeing employed as a chiller or air conditioner or cooling device, Supply #1may comprise the heat sink or evaporative cooling water supply or air orother heat sink, and the Enthalpy Sink Heat Exchanger may be enable therefrigeration cycle to release or discharge heat into the heat sink. If therefrigeration cycle is being employed as a heat pump or heating device,Supply #1 may comprise the load or application requiring heating, and theEnthalpy Sink Heat Exchanger may enable the refrigeration cycle to supplyheat to this load or application requiring heating. The Enthalpy Sink HeatExchanger transfers heat from LL-1 to Supply #1, which may result inReturn #1 (which may possess a hotter temperature or greater enthalpy thanSupply #1) and L-1 (which may possess a lesser temperature or lesserenthalpy than LL-1).Supply #1Supply #1 may comprise a cooler temperature or lower enthalpy or both heattransfer fluid or material than Return #1. Supply #1 may comprise anapplication requiring heating or a heat sink or an enthalpy sink or acombination thereof, for example, before absorbing heat in a heat exchange.Return #1Return #1 may comprise a warmer temperature or greater enthalpy or bothheat transfer fluid or material than Supply #1. Return #1 may comprise anapplication requiring heating or a heat sink or an enthalpy sink or acombination thereof, for example, after absorbing heat in a heat exchange.Supply #2Supply #2 may comprise a cooler temperature or lower enthalpy or both heattransfer fluid or material than Return #2. Supply #2 may comprise anapplication requiring cooling or a heat source or an enthalpy source or acombination thereof, for example, after discharging heat in a heat exchange.Return #2Return #2 may comprise a warmer temperature or greater enthalpy or bothheat transfer fluid or material than Supply #2. Return #2 may comprise anapplication requiring cooling or a heat source or an enthalpy source or acombination thereof, for example, before discharging heat in a heatexchange.Example Figure Key FIG. 15Label inFIG.DescriptionL-1L-1 may comprise a solution comprising a combination of OrganicComposition #1 and aqueous liquid phase. L-1 may comprise at least aportion a single liquid phase combined solution. L-1 may comprise LL-1,except after heat removal from LL-1 in, for example, the Enthalpy Heat SinkHeat Exchanger. Heat removed in the Enthalpy Heat Sink HeatExchanger may include, but is not limited to, heat from enthalpy of liquid-liquid phase transition and / or heat from specific heat capacity. L-1 is anoutput of the Enthalpy Sink Heat Exchanger.L-4L-4 may comprise a concentrated solution of ‘salting-out reagent’ or‘concentrate’ or ‘retentate’. L-4 may also comprise some OrganicComposition #1 which may be due to, including, but not limited to, residualfrom L-3 and / or an incomplete separation in LLS-1 and / or residualOrganic Composition #1 dissolved in L-2. L-4 may be generated by ‘FO’.Mix #1Mix #1 may involve mixing or combining L-1 and L-4 to form a multi-liquidphase solution, LL-2. Said mixing may result in a liquid-liquid phasetransition, which may possess an enthalpy of phase transition. Said enthalpyof phase transition may be endothermic or exothermic, although may beendothermic in the present embodiment.LL-2LL-2 may comprise a multi-liquid phase mixture, which may have resultedfrom the mixing of L-1 and L-4. LL-2 may possess a lesser temperatureand / or lesser enthalpy than L-4 and L-1. LL-2 may possess said lessertemperature, due to, for example, an endothermic liquid-liquid phasetransition in Mix #1. LL-2 may possess a latent endothermic enthalpy ofphase transition, which may absorb heat in the Enthalpy Source HeatExchanger. LL-2 may possess a substantially lower temperature than, forexample, ‘Return #2’, and the heat capacity of this substantially lowertemperature may be exploited in the Enthalpy Source Heat Exchanger tocool Return #2 to form Supply #2.EnthalpyThe Enthalpy Source Heat Exchanger may transfer or exchange heat fromSource Heatone or more heat or enthalpy sources to the refrigeration cycle. If theExchangerrefrigeration cycle is being employed as a chiller or air conditioner orcooling device, Return #2 may comprise the load or application requiringcooling, and the Enthalpy Source Heat Exchanger may be employed toenable the refrigeration cycle to absorb heat from the load or ‘cool’ the load.If the refrigeration cycle is being employed as a heat pump or heating device,Return #2 may comprise the enthalpy or heat source, and the EnthalpySource Heat Exchanger may be employed to enable the refrigeration cycle toabsorb heat from this enthalpy or heat source. The Enthalpy Source HeatExchanger transfers heat from Return #2 to LL-2, which may result inSupply #2 (which may possess a cooler temperature or lower enthalpy thanReturn #2) and LL-3 (which may possess a higher temperature or greaterenthalpy than LL-2).LL-3LL-3 may comprise a multi-liquid phase mixture, which may have resultedfrom LL-2 absorbing heat while heat exchanging in the Enthalpy SourceHeat Exchanger. LL-3 may possess a greater temperature or greaterenthalpy or both than LL-2.LLS-1LLS-1 may comprise a liquid-liquid separation device. LLS-1 may separateLL-3 into constituent liquid phases, which may comprise L-2 and L-3.L-2L-2 may comprise a dilute solution of ‘salting-out reagent’. L-2 maycomprise one of the liquid phases separated by LLS-1 from multi-liquidphase mixture LL-3. L-2 may comprise a feed solution into ‘FO’.L-5Liquid B or L-5 may comprise a draw solution in ‘FO’. L-5 may comprise asolution with a large osmotic pressure. L-5 may desirably have an osmoticpressure greater than L-2 or L-4. Alternatively, L-5 may have an osmoticpressure near, at, or less than the osmotic pressure of L-4, and FO maycomprise an osmotically assisted reverse osmosis system. L-5 maycomprise, for example, including, but not limited to, one or more or acombination of the following: sugar water, concentrate, juice concentrate,syrup concentrate, malt concentrate, beverage concentrate, seawater,brackish water, saline water, evaporation pond brine, brine from hypersalinelake, brine from saline aquifer, saline brine from underground, or frack waterbrine.FO‘FO’ may comprise a forward osmosis or an osmotically assisted reverseosmosis or combination thereof process. ‘FO’ may involve a feed solutioncomprising L-2, which may be concentrated into a concentrate or retentate,L-4. ‘FO’ may involve a draw solution comprising ‘Liquid B’ (L-5) which,during Forward Osmosis, may be diluted by the water and / or other liquidflux through a ‘FO’ membrane, which may result in a diluted draw solutionor ‘Dilute Liquid B’ (L-6).L-6Dilute Liquid B or L-6 may comprise diluted draw solution (for example:diluted L-5) following forward osmosis or osmotically assisted reverseosmosis in ‘FO’. L-6 may be returned to the original source of L-5.Alternatively, L-6 may comprise a valuable byproduct, for example, whichmay include, but is not limited to, one or more or a combination of thefollowing: a feedstock for a beverage, or a feedstock for brewery, orfeedstock to a fermentation process, or a drilling fluid feedstock, or aantifreeze solution. The water permeating into L-5 during ‘FO’ to form L-6may comprise a similar or the same mass of water added to the process inL-7.L-3L-3 may comprise a solution comprising mostly ‘Organic Composition #1’.L-3 may comprise one of the liquid phases separated by LLS-1 from multi-liquid phase mixture LL-3.L-7Liquid A or L-7 may comprise solvent or membrane permeable solventinput, which may include, but is not limited to, water, ammonia, organicsolvent, inorganic solvent, or a combination thereof. Liquid A or L-7 inputmay undergo treatment to remove or minimize potential contaminants orfoulants. If necessary, said treatment may be conducted, for example, beforeMix #2.Mix #2Mix #2 may involve mixing or combining L-3 and L-7 to form a multi-liquidphase solution, LL-1, or at least a portion single liquid phase combinedsolution, LL-1, or a single liquid phase combined solution, LL-1. L-3 andL-7 may Mix in Mix #2 to form an exothermic or endothermic liquid-liquidphase transition, although in the present embodiment, the liquid-liquid phasetransition may form an exothermic phase transition.LL-1LL-1 may comprise a mixture or combination of L-3 and L-7. Depending onthe temperature of L-3 and L-7, LL-1 may combine to form a single liquidphase combined solution, at least a portion of a single liquid phase combinedsolution, or a multi-liquid phase mixture. For example, if L-3 and L-7combine at a temperature less than their liquid-liquid phase transitiontemperature by a temperature difference greater than the adiabatictemperature change of their enthalpy of phase transition, the LL-1 maycomprise a single liquid phase combined solution at a greater temperaturethan L-3 and / or L-7. For example, if L-3 and L-7 combine at a temperatureless than their liquid-liquid phase transition temperature by a temperaturedifference less than the adiabatic temperature change of their enthalpy ofphase transition, the LL-1 may comprise a portion, but not entirely, a singleliquid phase combined solution at a greater temperature than L-3 and / orL-7. For example, if L-3 and L-7 combine at a temperature equal to orgreater than their liquid-liquid phase transition temperature, the LL-1 maycomprise a multi-liquid phase mixture.Enthalpy SinkThe Enthalpy Sink Heat Exchanger may transfer or exchange heat from theHeatrefrigeration cycle to one or more heat sinks. If the refrigeration cycle isExchangerbeing employed as a chiller or air conditioner or cooling device, Supply #1may comprise the heat sink or wet surface air heat exchanger or evaporativecooling water supply or air or other heat sink, and the Enthalpy Sink HeatExchanger may be enable the refrigeration cycle to release or discharge heatinto the heat sink. If the refrigeration cycle is being employed as a heatpump or heating device, Supply #1 may comprise the load or applicationrequiring heating, and the Enthalpy Sink Heat Exchanger may enable therefrigeration cycle to supply heat to this load or application requiringheating. The Enthalpy Sink Heat Exchanger transfers heat from LL-1 toSupply #1, which may result in Return #1 (which may possess a hottertemperature or greater enthalpy than Supply #1) and L-1 (which may possessa lesser temperature or lesser enthalpy than LL-1).Supply #1Supply #1 may comprise a cooler temperature or lower enthalpy or both heattransfer fluid or material than Return #1. Supply #1 may comprise anapplication requiring heating or a heat sink or an enthalpy sink or acombination thereof, for example, before absorbing heat in a heat exchange.Return #1Return #1 may comprise a warmer temperature or greater enthalpy or bothheat transfer fluid or material than Supply #1. Return #1 may comprise anapplication requiring heating or a heat sink or an enthalpy sink or acombination thereof, for example, after absorbing heat in a heat exchange.Supply #2Supply #2 may comprise a cooler temperature or lower enthalpy or both heattransfer fluid or material than Return #2. Supply #2 may comprise anapplication requiring cooling or a heat source or an enthalpy source or acombination thereof, for example, after discharging heat in a heat exchange.Return #2Return #2 may comprise a warmer temperature or greater enthalpy or bothheat transfer fluid or material than Supply #2. Return #2 may comprise anapplication requiring cooling or a heat source or an enthalpy source or acombination thereof, for example, before discharging heat in a heatexchange.Example Figure Key FIG. 16Label inFIG.DescriptionL-1L-1 may comprise a solution comprising a combination of OrganicComposition #1 and aqueous liquid phase. L-1 may comprise at least aportion a single liquid phase combined solution. L-1 may comprise LL-1,except after heat removal from LL-1 in, for example, the Enthalpy Heat SinkHeat Exchanger. Heat removed in the Enthalpy Heat Sink HeatExchanger may include, but is not limited to, heat from enthalpy of liquid-liquid phase transition and / or heat from specific heat capacity. L-1 is anoutput of the Enthalpy Sink Heat Exchanger.L-4L-4 may comprise a concentrated solution of ‘salting-out reagent’ or‘concentrate’ or ‘retentate’. L-4 may also comprise some OrganicComposition #1 which may be due to, including, but not limited to, residualfrom L-3 and / or an incomplete separation in LLS-1 and / or residualOrganic Composition #1 dissolved in L-2. L-4 may be generated by‘FO #1’Mix #1Mix #1 may involve mixing or combining L-1 and L-4 to form a multi-liquidphase solution, LL-2. Said mixing may result in a liquid-liquid phasetransition, which may possess an enthalpy of phase transition. Said enthalpyof phase transition may be endothermic or exothermic, although may beendothermic in the present embodiment.LL-2LL-2 may comprise a multi-liquid phase mixture, which may have resultedfrom the mixing of L-1 and L-4. LL-2 may possess a lesser temperatureand / or lesser enthalpy than L-4 and L-1. LL-2 may possess said lessertemperature, due to, for example, an endothermic liquid-liquid phasetransition in Mix #1. LL-2 may possess a latent endothermic enthalpy ofphase transition, which may absorb heat in the Enthalpy Source HeatExchanger. LL-2 may possess a substantially lower temperature than, forexample, ‘Return #2’, and the heat capacity of this substantially lowertemperature may be exploited in the Enthalpy Source Heat Exchanger tocool Return #2 to form Supply #2.EnthalpyThe Enthalpy Source Heat Exchanger may transfer or exchange heat fromSource Heatone or more heat or enthalpy sources to the refrigeration cycle. If theExchangerrefrigeration cycle is being employed as a chiller or air conditioner orcooling device, Return #2 may comprise the load or application requiringcooling, and the Enthalpy Source Heat Exchanger may be employed toenable the refrigeration cycle to absorb heat from the load or ‘cool’ the load.If the refrigeration cycle is being employed as a heat pump or heating device,Return #2 may comprise the enthalpy or heat source, and the EnthalpySource Heat Exchanger may be employed to enable the refrigeration cycle toabsorb heat from this enthalpy or heat source. The Enthalpy Source HeatExchanger transfers heat from Return #2 to LL-2, which may result inSupply #2 (which may possess a cooler temperature or lower enthalpy thanReturn #2) and LL-3 (which may possess a higher temperature or greaterenthalpy than LL-2).LL-3LL-3 may comprise a multi-liquid phase mixture, which may have resultedfrom LL-2 absorbing heat while heat exchanging in the Enthalpy SourceHeat Exchanger. LL-3 may possess a greater temperature or greaterenthalpy or both than LL-2.LLS-1LLS-1 may comprise a liquid-liquid separation device. LLS-1 may separateLL-3 into constituent liquid phases, which may comprise L-2 and L-3.L-2L-2 may comprise a dilute solution of ‘salting-out reagent’. L-2 maycomprise one of the liquid phases separated by LLS-1 from multi-liquidphase mixture LL-3. L-2 may comprise a feed solution into ‘FO #1’.L-5Liquid B or L-5 may comprise a draw solution in ‘FO #1’. L-5 maycomprise a solution with a large osmotic pressure. L-5 may desirably havean osmotic pressure greater than L-2 or L-4. Alternatively, L-5 may have anosmotic pressure near, at, or less than the osmotic pressure of L-4, andFO #1 may comprise an osmotically assisted reverse osmosis system. L-5may comprise, for example, including, but not limited to, one or more or acombination of the following: sugar water, concentrate, juice concentrate,syrup concentrate, malt concentrate, beverage concentrate, seawater,brackish water, saline water, evaporation pond brine, brine from hypersalinelake, brine from saline aquifer, saline brine from underground, or frack waterbrine.FO #1‘FO #1’ may comprise a forward osmosis or an osmotically assisted reverseosmosis or combination thereof process. ‘FO #1’ may involve a feedsolution comprising L-2, which may be concentrated into a concentrate orretentate, L-4. ‘FO #1’ may involve a draw solution comprising ‘Brine’(L-5) which, during Forward Osmosis, may be diluted by the water and / orother liquid flux through a ‘FO #1’ membrane, which may result in a diluteddraw solution or ‘Dilute Brine’ (L-6).L-6Dilute Liquid B or L-6 may comprise diluted draw solution (for example:diluted L-5) following forward osmosis or osmotically assisted reverseosmosis in ‘FO #1’. L-6 may be returned to the original source of L-5.Alternatively, L-6 may comprise a valuable byproduct, for example, whichmay include, but is not limited to, one or more or a combination of thefollowing: a feedstock for a beverage, or a feedstock for brewery, orfeedstock to a fermentation process, or a drilling fluid feedstock, or aantifreeze solution. The water permeating into L-5 during ‘FO #1’ to formL-6 may comprise a similar or the same mass of water added to the processin L-7.L-3L-3 may comprise a solution comprising mostly ‘Organic Composition #1’.L-3 may comprise one of the liquid phases separated by LLS-1 from multi-liquid phase mixture LL-3.L-7Liquid A or L-7 may comprise solvent or membrane permeable solventinput, which may include, but is not limited to, water, ammonia, organicsolvent, inorganic solvent, or a combination thereof. Liquid A or L-7 maycomprise freshwater or brackish water or seawater or wastewater or waterwith impurities.FO #2FO #2 may comprise a forward osmosis or osmotically assisted reverseosmosis process. FO #2 may involve passing L-7 across a membrane andL-3 across the opposite side of a membrane. Due to osmotic pressure orhydraulic pressure or both, water or other solvent may pass through themembrane from L-7 to L-3, which may result in diluted L-3 or a multi-liquidphase mixture or both (LL-1) and concentrated L-7 residual reagents (L-8).FO #2 may enable water or other solvent from L-7 to be transferred from L-7to L-3 while preventing the transfer of non-water or non-solvent residualreagents from L-7. FO #2 may be integrated or combined with the EnthalpySink Heat Exchanger. For example, a portion of or all the Enthalpy SinkHeat Exchanger may be placed before or during FO #2. FO #2 may be, ifdesired, cooled or heated during operation.FO #2 may involve preventing contaminants in L-7 from entering therefrigeration cycle. It may be desirable for the recovery ratio or recoveryrate, or the percentage of L-7 which is in LL-1, to be greater than or equal to,including, but not limited to, one or more or a combination of the following:10%, or 20%, or 30%, or 40%, or 50%, or 60%, or 70%, or 80%, or 90%, or95%.FO #2 may involve mixing or combining L-3 and L-7 to form a multi-liquidphase solution, LL-1, or at least a portion single liquid phase combinedsolution, LL-1, or a single liquid phase combined solution, LL-1. A portionof L-3 and L-7 may combine in FO #2 to form an exothermic or endothermicliquid-liquid phase transition, although in the present embodiment, theliquid-liquid phase transition may form an exothermic phase transition.L-8L-8 or Retentate Liquid A may comprise the retentate from FO #2. L-8 orRetentate Liquid A may comprise a more concentrated solution of non-wateror non-solvent reagents or reagents which may be impermeable to amembrane in FO #2.LL-1LL-1 may comprise a mixture or combination of L-3 and L-7 permeate fromFO #2. Depending on the temperature of L-3 and L-7, LL-1 may combine toform a single liquid phase combined solution, at least a portion of a singleliquid phase combined solution, or a multi-liquid phase mixture. Forexample, if L-3 and L-7 combine at a temperature less than their liquid-liquid phase transition temperature by a temperature difference greater thanthe adiabatic temperature change of their enthalpy of phase transition, theLL-1 may comprise a single liquid phase combined solution at a greatertemperature than L-3 and / or L-7. For example, if L-3 and L-7 combine at atemperature less than their liquid-liquid phase transition temperature by atemperature difference less than the adiabatic temperature change of theirenthalpy of phase transition, the LL-1 may comprise a portion, but notentirely, a single liquid phase combined solution at a greater temperaturethan L-3 and / or L-7. For example, if L-3 and L-7 combine at a temperatureequal to or greater than their liquid-liquid phase transition temperature, theLL-1 may comprise a multi-liquid phase mixture.Enthalpy SinkThe Enthalpy Sink Heat Exchanger may transfer or exchange heat from theHeatrefrigeration cycle to one or more heat sinks. If the refrigeration cycle isExchangerbeing employed as a chiller or air conditioner or cooling device, Supply #1may comprise the heat sink or wet surface air heat exchanger or evaporativecooling water supply or air or other heat sink, and the Enthalpy Sink HeatExchanger may be enable the refrigeration cycle to release or discharge heatinto the heat sink. If the refrigeration cycle is being employed as a heatpump or heating device, Supply #1 may comprise the load or applicationrequiring heating, and the Enthalpy Sink Heat Exchanger may enable therefrigeration cycle to supply heat to this load or application requiringheating. The Enthalpy Sink Heat Exchanger transfers heat from LL-1 toSupply #1, which may result in Return #1 (which may possess a hottertemperature or greater enthalpy than Supply #1) and L-1 (which may possessa lesser temperature or lesser enthalpy than LL-1).Supply #1Supply #1 may comprise a cooler temperature or lower enthalpy or both heattransfer fluid or material than Return #1. Supply #1 may comprise anapplication requiring heating or a heat sink or an enthalpy sink or acombination thereof, for example, before absorbing heat in a heat exchange.Return #1Return #1 may comprise a warmer temperature or greater enthalpy or bothheat transfer fluid or material than Supply #1. Return #1 may comprise anapplication requiring heating or a heat sink or an enthalpy sink or acombination thereof, for example, after absorbing heat in a heat exchange.Supply #2Supply #2 may comprise a cooler temperature or lower enthalpy or both heattransfer fluid or material than Return #2. Supply #2 may comprise anapplication requiring cooling or a heat source or an enthalpy source or acombination thereof, for example, after discharging heat in a heat exchange.Return #2Return #2 may comprise a warmer temperature or greater enthalpy or bothheat transfer fluid or material than Supply #2. Return #2 may comprise anapplication requiring cooling or a heat source or an enthalpy source or acombination thereof, for example, before discharging heat in a heatexchange.Example Figure Key for FIG. 17Label inFIG.DescriptionL-1L-1 may comprise a solution comprising a combination of OrganicComposition #1 and aqueous liquid phase. L-1 may comprise at least aportion a single liquid phase combined solution. L-1 may comprise L-8,except after heat removal from L-8 in, for example, the Heat Exchanger #3.Heat removed in the Heat Exchanger #3 may include, but is not limited to,heat from enthalpy of liquid-liquid phase transition and / or heat fromspecific heat capacity. L-1 is an output of Heat Exchanger #3.HeatHeat Exchanger #2 may involve a heat exchange between ‘warm’ L-1 andExchanger #2‘cold’ L-9 and L-5, which may result in ‘cold’ L-1 and ‘warm’ L-9 (L-7) and‘warm’ L-5 (L-6). L-9 and L-5 may be heat exchanged with L-1 in HeatExchanger #2 as non-contiguously separate liquid phases to, for example,prevent L-9 and L-5 from dissolving in each other and / or releasing anenthalpy of phase transition during Heat Exchanger #2. Heat Exchanger #2may enable two separate temperature zones within the Refrigeration Cycleportion of the process. For example, L-6, L-7, Mix #1, L-8, HeatExchanger #3, and L-1 may comprise a first temperature zone, while L-2,Mix #2, LL-1, Heat Exchanger #1, LL-2. LLS-1, L-3, L-4, L-5, and L-9may comprise a second temperature zone which may be at a significantlydifferent temperature or temperature range than the first temperature zone.Said significantly different temperature may comprise a temperaturedifference greater than the adiabatic temperature change of the enthalpy ofthe liquid-liquid phase transition. Said temperature zones may enable therefrigeration cycle to move heat or pump heat across a temperaturedifference greater than the adiabatic temperature change of the enthalpy ofliquid-liquid phase transition.L-2L-2 may comprise L-1 after heat exchange in Heat Exchanger #2. L-2 maybe at a significantly different temperature than L-1, such as, for example, atemperature difference greater than the adiabatic temperature change of theliquid-liquid phase transition of Organic Composition #1 and water.Mix #2Mix #1 may involve mixing or combining L-2 and L-4 to form a multi-liquidphase solution, LL-1. Said mixing may result in a liquid-liquid phasetransition, which may possess an enthalpy of phase transition. Said enthalpyof phase transition may be endothermic or exothermic, although may beendothermic in the present embodiment.L-4L-4 may comprise a concentrated solution of ‘salting-out reagent’ or‘concentrate’ or ‘retentate’. L-4 may also comprise some OrganicComposition #1 which may be due to, including, but not limited to, residualfrom L-3 and / or an incomplete separation in LLS-1 and / or residualOrganic Composition #1 dissolved in L-3. The concentrate may begenerated by forward osmosis, ‘FO’.LL-1LL-1 may comprise a multi-liquid phase mixture, which may have resultedfrom the mixing of L-2 and L-4 in Mix #2. LL-1 may possess a lessertemperature and / or lesser enthalpy than L-4 and L-2. LL-1 may possess saidlesser temperature, due to, for example, an endothermic liquid-liquid phasetransition in Mix #2. LL-1 may possess a latent endothermic enthalpy ofphase transition, which may absorb heat in Heat Exchanger #1. LL-1 maypossess a lesser temperature than LL-2, which may enable the absorption ofheat in Heat Exchanger #1 due to specific heat capacity.HeatHeat Exchanger #1 may comprise a heat exchanger between LL-1 and anExchanger #1application requiring cooling or a heat source or enthalpy source. LL-1 mayabsorb heat in a heat exchange with an application requiring cooling or aheat source or enthalpy source, which may result in a higher temperatureand / or enthalpy LL-1 (for example: LL-2) and a lower temperature and / orless enthalpy application requiring cooling or heat source or enthalpy source.LL-2LL-2 may comprise the same overall composition as LL-1, except at a highertemperature and / or greater enthalpy. LL-2 may comprise LL-1 after heatexchanging in Heat Exchanger #1. LL-2 may comprise at least a portion amulti-liquid phase mixture. It may be desirable for at least one liquid phaseof said multi-liquid phase mixture to comprise mostly OrganicComposition #1. It may be desirable for at least one liquid phase of saidmulti-liquid phase mixture to comprise mostly water or a dilute aqueoussolution of ‘salting-out’ reagent.LLS-1LLS-1 may comprise a liquid-liquid separation device. LLS-1 may separateLL-2 into constituent liquid phases, which may comprise L-3 and L-5.L-3L-3 may comprise a dilute solution of ‘salting-out reagent’. L-3 maycomprise an aqueous solution. L-3 may comprise one of the liquid phasesseparated by LLS-1 from multi-liquid phase mixture LL-2. L-3 maycomprise residual Organic Composition #1, which may be due to, forexample, an incomplete separation in LLS-1 and / or residual OrganicComposition #1 dissolved in L-3.L-5L-5 may comprise a solution comprising mostly ‘Organic Composition #1’.L-5 may comprise one of the liquid phases separated by LLS-1 from multi-liquid phase mixture LL-2. L-5 may comprise residual water and / or ‘salting-out’ reagent, which may be due to, for example, an incomplete separation inLLS-1 and / or residual water and / or ‘salting-out’ reagent dissolved in L-5.FO‘FO’ may comprise a forward osmosis or an osmotically assisted reverseosmosis or combination thereof process. ‘FO’ may involve a feed solutioncomprising L-3, which may be concentrated into a concentrate or retentate,L-4. ‘FO’ may involve a draw solution comprising ‘Liquid B’ (L-10) which,during Forward Osmosis, may be diluted by the water and / or other liquidflux through a ‘FO’ membrane, which may result in a diluted draw solutionor ‘Dilute Liquid B’ (L-11).L-6L-6 may comprise L-5 after heat exchange in Heat Exchanger #2. L-6 maybe at a significantly different temperature than L-5, such as, for example, atemperature difference greater than the adiabatic temperature change of theliquid-liquid phase transition of Organic Composition #1 and water. L-6may be non-contiguously separate from L-7.L-7L-7 may comprise L-9 after heat exchange in Heat Exchanger #2. L-7 maybe at a significantly different temperature than L-9, such as, for example, atemperature difference greater than the adiabatic temperature change of theliquid-liquid phase transition of Organic Composition #1 and water. L-7may be non-contiguously separate from L-6.Mix #1Mix #1 may involve mixing or combining L-6 and L-7 to form, including,but not limited to, one or more or a combination of the following: a multi-liquid phase solution, L-8, or at least a portion single liquid phase combinedsolution, L-8, or a single liquid phase combined solution, L-8. L-6 and L-7may Mix in Mix #1 to form an exothermic or endothermic liquid-liquidphase transition, although the present embodiment may form an exothermicphase transition. It may be desirable for the adiabatic temperature change ofsaid enthalpy of said liquid-liquid phase transition to be greater than theapproach temperature and / or heat exchanger Delta-T of Heat Exchanger #2.L-8L-8 may comprise a combination of L-6 and L-7. L-8 may compriseincluding, but not limited to, one or more or a combination of the following:a multi-liquid phase solution, or at least a portion single liquid phasecombined solution, or a single liquid phase combined solution. L-8 may beat a greater temperature and / or greater enthalpy than L-1.HeatHeat Exchanger #3 may involve heat exchanging L-8 with an applicationExchanger #3requiring heating or a heat sink or a cold source, which may result in a lessertemperature and / or lesser enthalpy L-8 (for example: L-1) and a greatertemperature and / or greater enthalpy application requiring heating or a heatsink or a cold source.L-9Liquid A or L-9 may comprise solvent or membrane permeable solventinput, which may include, but is not limited to, water, ammonia, organicsolvent, inorganic solvent, or a combination thereof. Liquid A or L-7 inputmay undergo treatment to remove or minimize potential contaminants orfoulants. If necessary, said treatment may be conducted, for example, beforeMix #2.L-10Liquid B or L-10 may comprise a draw solution in ‘FO’. L-10 maycomprise a solution with a large osmotic pressure. L-10 may desirably havean osmotic pressure greater than L-2 or L-4. Alternatively, L-10 may havean osmotic pressure near, at, or less than the osmotic pressure of L-4, andFO may comprise an osmotically assisted reverse osmosis system. L-10 maycomprise, for example, including, but not limited to, one or more or acombination of the following: sugar water, concentrate, juice concentrate,syrup concentrate, malt concentrate, beverage concentrate, seawater,brackish water, saline water, evaporation pond brine, brine from hypersalinelake, brine from saline aquifer, saline brine from underground, or frack waterbrine.L-11Dilute Liquid B or L-11 may comprise diluted draw solution (for example:diluted L-5) following forward osmosis or osmotically assisted reverseosmosis in ‘FO’. L-11 may be returned to the original source of L-10.Alternatively, L-11 may comprise a valuable byproduct, for example, whichmay include, but is not limited to, one or more or a combination of thefollowing: a feedstock for a beverage, or a feedstock for brewery, orfeedstock to a fermentation process, or a drilling fluid feedstock, or aantifreeze solution. The water permeating into L-10 during ‘FO’ to formL-11 may comprise a similar or the same mass of water added to the processfrom L-9.Example CompositionsExample Organic Composition #1 may include, but is not limited to, one or more or a combination of the following:Glycol ethersGlycol ether polymersPolyethylene Glycol Dimethyl EtherPolyethylene Glycol Monomethyl EtherGlycol PolymersPolypropylene GlycolPolyethylene GlycolPolymers Combining PEG and PPG

[0316] PEG-PPG-PEG

[0317] PPG-PEG-PPG

[0318] ‘Rand’ Polymers

[0319] Ionic Liquids

[0320] Ethers

[0321] Glycol Ethers

[0322] Butoxyethanol

[0323] Diethylene Glycol Hexyl Ether

[0324] Organic reagents

[0325] Organic reagents which are liquid at or near room temperature

[0326] Reagents which possess a liquid-liquid phase transition in water

[0327] Reagents which possess a liquid-liquid phase transition in a solvent

[0328] Example Organic Composition #2 may include, but is not limited to, one or more or a combination of the following:

[0329] Glycol ethers

[0330] Glycol ether polymers

[0331] Polyethylene Glycol Dimethyl Ether

[0332] Polyethylene Glycol Monomethyl Ether

[0333] Glycol Polymers

[0334] Polypropylene Glycol

[0335] Polyethylene Glycol

[0336] Polymers Combining PEG and PPG

[0337] PEG-PPG-PEG

[0338] PPG-PEG-PPG

[0339] ‘Rand’ Polymers

[0340] Ionic Liquids

[0341] Ethers

[0342] Glycol Ethers

[0343] Butoxyethanol

[0344] Diethylene Glycol Hexyl Ether

[0345] Organic reagents

[0346] Organic reagents which are liquid at or near room temperature

[0347] Reagents which possess a liquid-liquid phase transition in water

[0348] Salt brine solutions

[0349] Antifreeze solutions

[0350] Draw solutions described herein

[0351] Externally regenerated draw solutions

[0352] Greater osmotic pressure solution

[0353] Naturally occurring greater osmotic pressure solution

[0354] Reagents which possess a liquid-liquid phase transition in a solvent

[0355] Example Salts or Salting-Out Reagents: ionic compounds, organic compounds, ammonium sulfate, potassium sulfate, dipotassium phosphate, tripotassium phosphate, monopotassium phosphate, calcium chloride, sodium chloride, glycerol, PEGs, PEG ethers, ammonia, carbon dioxide, potassium carbonate, sodium sulfate, ammonium nitrate, ammonium carbonate, ammonium bicarbonate, ammonium sesquicarbonate, ammonium carbamate, or a combination thereof.Notes

[0356] Note: It may be desirable for Organic Composition #2 to possess a greater osmotic pressure or a greater phase transition temperature or a combination thereof compared to Organic Composition #1.

[0357] Note: It may be desirable for Organic Composition #2 to possess a greater osmotic pressure or a greater phase transition temperature or a combination thereof in a solution with water compared to Organic Composition #1.

[0358] Note: It may be desirable for the adiabatic temperature change of the liquid-liquid phase transition to be greater than the approach temperature difference or required heat transfer delta-T or both of, for example, ‘Heat Exchanger #2’ in, for example, FIGS. 11 and 12. It may be desirable for the enthalpy of phase transition in ‘Mix #2’ in FIGS. 11 and 12 to possess an adiabatic temperature change greater than the approach temperature difference or required heat transfer delta-T or both of, for example, ‘Heat Exchanger #2’.

[0359] Note: In some embodiments, Organic Composition #1 may be the same composition as Organic Composition #2.

[0360] Note: Favorable Properties for Liquid-Liquid Phase Transition may include, but are not limited to, one or more or a combination of the following properties: liquid-liquid phase transition temperature range, liquid-liquid phase transition temperature, composition of the constituent liquid phases, water concentration in mostly non-water liquid phase, residual non-water reagent concentration in mostly water liquid phase, enthalpy of liquid-liquid phase transition, toxicity, volatility, flammability, cost, corrosion inhibitors, degradation inhibitors, antiscalants, anti-foulants, anti-biofoulants, oxygen scavengers, pH buffers, density, hydrophobicity, hydrophilicity, surface tension, self-attraction forces, repelling forces, coalescing properties, viscosity, density, density difference between liquid phases, hydrophobicity, hydrophilicity, surface tension, self-attraction forces, repelling forces, coalescing properties, viscosity, or a combination thereof.

[0361] Note: Liquid-liquid phase transition facilitator reagents or liquid-liquid phase transition separation facilitator reagents or salting-out reagents or phase transition temperature adjustment reagents may include, but are not limited to, salts, or inorganics, or organics, or other reagents which may improve one or more or a combination of properties which enable or facilitate liquid-liquid phase transition. Said properties may include, but are not limited to, liquid-liquid phase transition temperature range, liquid-liquid phase transition temperature, composition of the constituent liquid phases, water concentration in mostly non-water liquid phase, residual non-water reagent concentration in mostly water liquid phase, enthalpy of liquid-liquid phase transition, toxicity, volatility, flammability, cost, corrosion inhibitors, degradation inhibitors, antiscalants, anti-foulants, anti-biofoulants, oxygen scavengers, pH buffers, density, hydrophobicity, hydrophilicity, surface tension, self-attraction forces, repelling forces, coalescing properties, viscosity, or a combination thereof.

[0362] Note: Liquid-liquid phase separation facilitator reagents or liquid-liquid phase transition facilitator reagents or salting-out reagents or phase transition temperature adjustment reagents may include, but are not limited to, salts, or inorganics, or organics, or other reagents which may improve one or more or a combination of properties which enable or facilitate liquid-liquid phase separation. Said properties may include, but are not limited to, density, hydrophobicity, hydrophilicity, surface tension, self-attraction forces, repelling forces, coalescing properties, viscosity, or a combination thereof.

[0363] Note: By using FO, the present invention can employ a wider range of organic Composition #1 reagents, including organic Composition #1 which require significantly greater salt concentrations / salt osmotic pressure to be ‘salted out’ or undergo a phase transition temperature adjustment which results in a multi-liquid phase mixture or greater phase separation. Benefits may include, but are not limited to, refrigeration cycles producing or pumping heat across larger temperature differences and / or greater Enthalpy of mixing or enthalpy of phase transition organic Composition #1 reagents and / or greater heat pumping capacity per a unit of liquid flow rate or a combination thereof.

[0364] Note: Liquid streams in the present invention may be stored in liquid storage vessel(s). For example, one or more liquid streams in the present invention may be stored in liquid storage vessels to enable desynchronized operation of different sections of the process. For example, one or more Regeneration Portion streams may be stored in liquid storage tanks to enable the Refrigeration Cycle Portion to operate while the Regeneration Portion may not be operating. For example, one or more Regeneration Portion streams may be stored in liquid storage tanks to enable the Refrigeration Cycle Portion to temporarily or instantaneously or both operate at higher output or capacity than the rate which it is regenerating in the regeneration portion. For example, one or more Refrigeration Cycle Portion streams may be stored in liquid storage tanks to enable the Regeneration Portion to operate while the Regeneration Portion may not be operating.

[0365] Note: Before or while starting operation where the hot and cold temperature zones are the same temperature, it may be desirable to employ an external source of heat or cold to cool and / or heat the respective regions to near the temperatures desired for the temperature zones. When the refrigeration cycle operates after the temperatures in the temperature zones have been adjusted to the desired temperatures, the refrigeration cycle may sustain said the temperature of said temperature zones while pumping heat. Alternatively, or additionally, the desired temperature zones may be generated by temporarily not or minimally or insufficiently supplying heat to an enthalpy source heat exchanger, or temporarily not or minimally or insufficiently supplying heat to an enthalpy sink heat exchanger, or a combination thereof. The duration of said ‘temporary’ may be until one or more desired temperature zones are achieved.

[0366] Note: The present invention may enable the generation of useful energy or work (e.g. cooling or heating) from the enthalpy of mixing of high osmotic pressure solutions and low osmotic pressure solutions. For example, the present invention may enable the powering of a refrigeration cycle for heating or cooling using seawater as a draw solution and freshwater as an input stream. For example, the present invention may enable the powering of a refrigeration cycle for heating or cooling from the enthalpy of mixing of high osmotic pressure solutions and low osmotic pressure solutions without the need to first convert the enthalpy of mixing of said high osmotic pressure solution and low osmotic pressure solution into electricity or mechanical work.

[0367] Note: In some saline lakes or hypersaline lakes, water levels are receding due to droughts, diversions of water flow, or other potential causes. The present invention enables water to be added to these saline lakes or hypersaline lakes, while, in the process, generating useful or valuable heating or cooling. For example, water levels in the Dead Sea have been declining for many years, causing environmental and economic challenges. The Israeli and Jordanian governments have made proposals to ship water from desalination plants, Mediterranean water, Red Sea Water, Sea of Galilee Water, or other water sources to the Dead Sea and add said water to address the Dead Seas declining water levels. With the present invention, said water can be added to the Dead Sea, and, in the process of added or introducing or contacting or mixing said water, supply / power the cooling or heating needs of nearby resorts, buildings, industry, and / or other applications requiring cooling or heating.

[0368] Note: Phase transition temperature may be adjusted by adjusting properties other than or in addition to concentration adjustment. For example, phase transition temperature may be adjusted by adjusting magnetic properties, especially if reagents with magnetically influenced solubility properties or phase transition properties are employed. For example, phase transition temperature may be adjusted by adjusting the presence of light or certain wavelengths of liquid or a combination thereof, especially if reagents with light-influenced solubility properties or phase transition properties are employed.

[0369] Example Liquid-Liquid Phase Transitioning Reagents include, but are not limited to, one or more or a combination of the following:

[0370] Glycol ethers

[0371] Glycol ether polymers

[0372] Polyethylene Glycol Dimethyl Ether

[0373] Polyethylene Glycol Monomethyl Ether

[0374] Glycol Polymers

[0375] Polypropylene Glycol

[0376] Polyethylene Glycol

[0377] Polymers Combining PEG and PPG

[0378] PEG-PPG-PEG

[0379] PPG-PEG-PPG

[0380] ‘Rand’ Polymers

[0381] Ionic Liquids

[0382] Ethers

[0383] Glycol Ethers

[0384] Butoxyethanol

[0385] Diethylene Glycol Hexyl Ether

[0386] Reagents with a liquid-liquid phase transition in water

[0387] Reagents with a liquid-liquid phase transition in a solventSummary DescriptionSummary of Liquid Phase Only Refrigeration Cycle:

[0388] The present embodiment pertains to a configuration of a ‘liquid-phase only’ refrigeration cycle.

[0389] The present embodiment operates using a liquid solution which exhibits a liquid-liquid phase transition. A solution liquid-liquid phase transitions from a combined single liquid phase to a two liquid phase mixture above a liquid-liquid phase transition temperature. Below said liquid-liquid phase transition temperature, a two liquid phase mixture reversibly liquid-liquid phase transitions into a combined single liquid phase solution. When a solution liquid-liquid phase transitions from a single liquid phase to two liquid phases, the solution absorbs heat (i.e. an endothermic phase transition). When a solution liquid-liquid phase transitions from a two liquid phases to one liquid phase, the solution releases heat (i.e. an exothermic phase transition). The amount of heat absorbed by an endothermic liquid-liquid phase transition may be the same as the amount of heat released by an exothermic liquid-liquid phase transition with the same solution and temperature ranges. The amount of heat absorbed or released during a liquid-liquid phase transition is referred to herein as ‘the enthalpy of phase transition’ or ‘enthalpy of liquid-liquid phase transition’.

[0390] A liquid-liquid phase transitioning solution may comprise an organic component (also described as organic reagent or organic) and an aqueous component. When a solution comprises a single liquid phase combined solution, the organic component may dissolved in the aqueous component. When a solution comprises a two liquid phase mixture, an organic component and an aqueous component may be separate liquid phases, respectively.

[0391] A liquid-liquid phase transition temperature range may be adjusted by adjusting the concentration of salt in the solution. Increasing the concentration of salt may decrease a liquid-liquid phase transition temperature range. Above a certain concentration of salt (depending on the type of salt, the composition of the organic component, and the concentration of the organic component), an organic component may become nearly or completely insoluble or may form a separate liquid phase (e.g. may be salted out). A liquid phase only refrigeration cycle may work by adjusting the concentration of a salt or other reagent with similar phase transition temperature adjustment or ‘salting-out’ properties or characteristics such that an exothermic liquid-liquid phase transition is engineered to occur at a greater temperature and an endothermic liquid-liquid phase transition is engineered to occur at a lesser temperature.Brief Description of the Figures

[0392] FIG. 23: FIG. 23 shows a liquid phase only refrigeration cycle functioning as a heat transfer liquid for a conventional vapor compression refrigeration cycle chiller (only the evaporator side of a conventional vapor compression refrigeration cycle is shown—shown as LV-1 and V-1). Unlike chilled water heat transfer, the liquid phase only refrigeration cycle acts as a second refrigeration cycle, providing an additional cooling compared to a heat transfer liquid without the liquid phase only refrigeration cycle. The objective is to reduce the energy consumption of or stress on the conventional vapor compression refrigeration cycle by enabling it to generate a smaller temperature difference for the same cooling (for every 1° F. or 0.56° K reduction in temperature difference in a vapor compression refrigeration cycle, the energy efficiency of the vapor compression refrigeration cycle increases by 2%).

[0393] FIG. 24: Same as FIG. 24, except with example stream temperatures shown. Unlike chilled water heat transfer, the liquid phase only refrigeration cycle acts as a second refrigeration cycle, providing an additional 7.5° K of cooling compared to a heat transfer liquid without the liquid phase only refrigeration cycle, which translates into a 27% increase in energy efficiency for the vapor compression refrigeration cycle (for every 1° F. or 0.56° K reduction in temperature difference in a vapor compression refrigeration cycle, the energy efficiency of the vapor compression refrigeration cycle increases by 2%).

[0394] FIG. 25: A figure of a conventional chilled water loop achieving the same temperatures as FIG. 24. In FIG. 25, to achieve a Supply #2 temperature of 7.5° C., the vapor compression refrigeration cycle evaporator temperature (LV-1 and V-1) needs to be −0.5° C., or 7.5° K less than the temperature in FIG. 24, which translates into significantly greater electricity consumption / lower energy efficiency / lower Coefficient of Performance than the embodiments shown in FIG. 23 and FIG. 24.FIGS. 23 and 24 Summary:

[0395] FIG. 23 and FIG. 24 show a liquid-liquid phase transition refrigeration cycle acting as a second refrigeration cycle and a substitute for a heat transfer liquid (e.g. replacement of water). The purposes of the liquid phase only refrigeration cycle in FIGS. 23 and 24 may be to:

[0396] Increasing the energy efficiency of a vapor compression refrigeration cycle in a chiller by integrating a more energy efficient refrigeration cycle (the liquid phase only refrigeration cycle)

[0397] Supplying cooling as a non-volatile liquid

[0398] Supplying cooling with less liquid flow rate or greater energy density

[0399] In FIGS. 23 and 24, the liquid-liquid phase transition refrigeration cycle is employed to absorb heat from the ‘Load / Heat Source Heat Exchanger’ at a lower temperature (cooling Return #2 to produce Supply #2) and pump / release this heat in the ‘Heat Sink Heat Exchanger’ (supplying heat to Supply #1 to produce Return 2). In FIGS. 23 and 24, the ‘Load / Heat SourceHeatExchanger’ is cooling Return #2, which may comprise a gas requiring cooling. For example, ‘Heat Sink Heat Exchanger’ may comprise a liquid to air heat exchanger, such as an air handler unit in a building. In FIGS. 23 and 24, the ‘Heat Sink Heat Exchanger’ may comprise a Direct Expansion (DX) heat exchanger, which heat exchanges a liquid gas phase transition refrigerant (i.e. LV-1 and L-1) with a liquid (i.e. LL-1 and L-1).Figure KeyLabel inFIG.Example Figure Key for FIG. 23 and FIG. 24LL-1LL-1 comprises a two liquid phase mixture comprising a mixture of organicliquid phase (L-3) and freshwater permeate (L-5). LL-1 may be at its liquid-liquid phase transition temperature and may remain a two liquid phase mixtureuntil it is cooled in the heat sink heat exchanger.Stream Summary:Two liquid phase mixture, 10° C., less than 1 PPT salt conc.,6.22 Liters Per Minute (LPM)Heat SinkThe Heat Sink Heat Exchanger cools LL-1 by heat exchanging it with a heatHeatsink. During cooling inside the Heat Sink Heat Exchanger, LL-1 liquid-liquidExchangerphase transitions into a single liquid phase combined solution. In FIG. 1 andFIG. 2, the Heat Sink Heat Exchanger comprises a direct expansion (DX) heatexchanger, because the side of the heat exchanger connected to the vaporcompression refrigeration cycle (acting as the vapor compression refrigerationcycle's evaporator) involves vaporizing refrigerant from a liquid into a gas.L-1L-1 comprises mostly a single liquid phase combined solution. L-1 comprisesthe same overall composition as LL-1, except L-1 has undergone an exothermicliquid-liquid phase transition from two liquid phases to a single liquid phase dueto cooling in the Heat Sink Heat Exchanger.Stream Summary:Single liquid phase combined solution, 10° C., less than 1 PPT salt conc.,5.83 Liters Per Minute (LPM)L-4L-4 comprises reverse osmosis retentate. L-4 comprises a relativelyconcentrated salt solution.Stream Summary:Aqueous salt solution, 10° C., 52.26 grams per liter Dipotassium Phosphate,1.94 Liters Per Minute (LPM)Mix #1Mix #1 may be a mixing device which combines L-1 and L-4 to form a multi-liquid phase mixture, LL-2. During mixing of L-1 and L-4, L-4 dissolves in theaqueous component of L-1, ‘kicking-out’ or ‘salting-out’ most of the organicliquid phase. The liquid-liquid phase transition of this ‘salting-out’ of theorganic phase may be an endothermic liquid-liquid phase transition. In thepresent example flowsheet, the enthalpy of phase transition of this liquid-liquidphase transition may absorb 27 kJ of heat per kg of total solution. In the presentexample flowsheet, the baseline specific heat capacity of the liquid (without thespecific heat capacity enhancement due to a liquid-liquid phase transition) is 3.6J / g ° C. Based on the previously described values, LL-2 possesses a temperature7.5° C. less than the mean temperature of L-1 and L-4.LL-2LL-2 comprises a two liquid phase mixture comprising a mixture of organicliquid phase and dilute aqueous salt solution liquid phase following anendothermic liquid-liquid phase transition in Mix #1. LL-2 may be above itsliquid-liquid phase transition temperature. In the present example flowsheet,LL-2 may remain a multi-liquid phase solution through heat exchanging in theLoad / Heat Source Heat Exchanger.LL-2 may comprise a multi-liquid phase mixture if L-3 and L-5 are mixed near,at, or above its liquid-liquid phase transition temperature range in Mix #2 (whichis shown in). LL-2 may comprise a multi-liquid phase mixture with partialdissolution of L-3 in L-5 if L-3 and L-5 are mixed at a temperature at or lessthan their liquid-liquid phase transition temperature range. LL-2 may comprisea single liquid phase combined solution if L-3 and L-5 are mixed at atemperature less than their liquid-liquid phase transition temperature range bymore than the adiabatic temperature change of their enthalpy of liquid-liquidphase transition.Stream Summary:Two liquid phase mixture comprising a mostly organic liquid phase and a mostlyaqueous salt solution liquid phase, 2.5° C., 17.42 grams per liter DipotassiumPhosphate in aqueous liquid phase,7.78 Liters Per Minute (LPM)Load / HeatThe Load / Heat Source Heat Exchanger heat exchanges LL-2 with G-1, coolingSourceG-1 to form G-2 and heating LL-2 to form LL-3. In FIGS. 1 and 2, TheHeatLoad / Heat Source Heat Exchanger comprises a liquid-gas heat exchanger,Exchangerwhich may be, for example, an air handler heat Exchanger in a HVAC system.LL-3LL-3 comprises a two liquid phase mixture comprising a mixture of organicliquid phase and dilute aqueous salt solution liquid phase following heatexchanging / providing ‘cooling’ in the Load / Heat Source Heat Exchanger.LL-2 may be above its liquid-liquid phase transition temperature.LL-3 Stream Summary:Two liquid phase mixture comprising a mostly organic liquid phase and a mostlyaqueous salt solution liquid phase, 10° C., 17.42 grams per liter DipotassiumPhosphate in aqueous liquid phase,7.78 Liters Per Minute (LPM)LLS-1LLS-1 comprises a liquid-liquid separation device, such as a decanter. LLS-1separates LL-3 into two separate liquid streams, L-2 and L-3, which maycomprise the constituent liquid phases of LL-3.L-2L-2 comprises a relatively dilute aqueous salt solution, which may have beenone of the liquid phases separated from LL-3 in LLS-1. L-2 comprises the feedsolution for ‘RO’.Stream Summary:Aqueous salt solution, 10° C., 17.42 grams per liter Dipotassium Phosphate,5.83 Liters Per Minute (LPM)RO‘RO’ comprises a reverse osmosis unit. ‘RO’ converts a feed solution (L-2) intoa retentate stream (L-4) and a permeate stream (L-5).L-5L-5 comprises a freshwater permeate stream produced by ‘RO’ from feedsolution L-2.Stream Summary:Water, 10° C., less than 1 PPT salt conc.,3.89 Liters Per Minute (LPM)L-3L-3 comprises a mostly organic liquid phase, which may have been one of theliquid phases separated from LL-3 in LLS-1.Organic liquid phase, 10° C., less than 1 PPT salt conc.,1.94 Liters Per Minute (LPM)Mix #2Mix #2 may be a mixing device which combines L-3 and L-5 to form a multi-liquid phase mixture or single liquid phase solution or both, LL-2.LV-1LV-1 is part of a vapor compression refrigeration cycle heat exchanging with the(Supply #1)liquid phase only refrigeration cycle in the ‘Heat Sink Heat Exchanger’. LV-1comprises a refrigerant at a liquid state or a liquid-vapor Mix state before itenters the ‘Heat Sink Heat Exchanger’, where it will absorb heat whileexpanding / evaporating.V-1V-1 is part of a vapor compression refrigeration cycle heat exchanging with the(Return #1)liquid phase only refrigeration cycle in the ‘Heat Sink Heat Exchanger’. V-1comprises refrigerant at a vapor state following absorbing heat viaexpansion / evaporation in the ‘Heat Sink Heat Exchanger’.G-1G-1 comprises a warm air stream requiring cooling entering the ‘Load / Heat(Return #2)Source Heat Exchanger’. G-1 may be cooled during a heat exchange with the‘Load / Heat Source Heat Exchanger’, forming G-2.G-2G-2 comprises a cool air stream exiting the ‘Load / Heat Source Heat(Supply #2)Exchanger’.FIG. 23 and FIG. 24 Step-by-Step Description:

[0400] Heat Absorbing Liquid-Liquid Phase Transition: A combined single liquid phase solution comprising organic and freshwater (L-1) is mixed with a concentrated salt water retentate stream (L-4) in a mixing device (Mix #1). L-4 dissolves in the aqueous component of L-1, resulting in most of the organic component of L-1 forming a separate liquid phase in a liquid-liquid phase transition. The resulting multi-liquid phase mixture (LL-2) may comprise a mostly organic liquid phase and a mostly dilute salt water aqueous phase. The previously described liquid-liquid phase transition may be endothermic and may resulting in the temperature of LL-2 being significantly lower than the mean temperature of L-1 and L-4.

[0401] Absorbing Heat from ‘Load’ in Heat Exchanger: LL-2 is heat exchanged to cool a thermal load. For example, LL-2 is heat exchanged with warm air (G-1) in a liquid-gas heat exchanger (‘Load / Heat Source Heat Exchanger’), which results in cooled air (G-2) and warmer multi-liquid phase mixture (LL-3).

[0402] Liquid-Liquid Separation: LL-3 is separated into two separate liquid streams using a liquid-liquid separation device (LLS-1), such as a decanter. One of the two liquid phases may comprise a mostly organic liquid phase (L-3). One of the liquid phases may comprise mostly aqueous dilute salt solution (L-2).

[0403] Reverse Osmosis Separation: L-2 is fed into a reverse osmosis unit as a feed solution. L-2 is separated into a retentate stream comprising a concentrated salt solution (L-4) and a mostly freshwater permeate stream (L-5).

[0404] Mixing Freshwater and Organic Liquid Phases: L-5 is mixed with L-3 using a mixing device (Mix #2), forming LL-1. Because L-5 is almost salt-free, the liquid-liquid phase transition temperature of the solution is significantly greater than in LL-3. Depending on the liquid-liquid phase transition temperature range, the temperature of L-5 and L-3, and the enthalpy of the liquid-liquid phase transition, LL-1 may be a multi-liquid phase mixture, or a multi-liquid phase mixture with some L-3 dissolved in L-5, or a single liquid phase combined solution. In FIG. 24, the LL-1 comprises a multi-liquid phase mixture.

[0405] Releasing Heat to Heat Sink in Heat Exchanger: LL-1 is heat exchanged in the ‘Heat Sink Heat Exchanger’ to release heat into a heat sink. In FIG. 24, LL-1 releases heat while being cooled due to a liquid-liquid phase transition from a multi-liquid phase mixture to a single liquid phase solution. In FIG. 24, LL-1 is heat exchanged with a refrigerant at a liquid state or liquid-vapor state in the ‘Heat Sink Heat Exchanger’, resulting in a single liquid phase combined solution (L-1) and a refrigerant at a vapor state (V-1).Notes

[0406] Note: Enthalpy of Phase transition of the example liquid-liquid phase transition provided by FIG. 24 may be 27 kJ / kg.

[0407] Note: Baseline specific heat capacity of the example liquid-liquid phase transition composition in FIG. 24 (specific heat capacity of the liquid without the enthalpy of phase transition of the water+organic) is 3.6 J / g° C., which is used to determine the adiabatic temperature change due to the liquid-liquid phase transition.

[0408] Note: Liquid storage may be employed to store the liquid streams. This may enable the reverse osmosis unit or a vapor compression refrigeration cycle or both to continue running to recharge the storage tanks even when cooling is not required. Similarly, the storage tanks may provide cooling while the reverse osmosis unit, or a vapor compression refrigeration cycle or both is / are off.

[0409] Note: In a heat pump configuration, the ‘Heat Sink Heat Exchanger’ may comprise the heat exchanger heat exchanging with the ‘load’.

[0410] Note: Pumps and / or energy recovery devices may not be shown in the figures, although may be included in any reaL-life construction of the systems shown in FIG. 23 and FIG. 24.

[0411] Note: The present figures show a refrigeration cycle in a specific use case. The refrigeration cycle may be employed in other use cases or temperature ranges than those shown or described herein.Organic Solvent Nanofiltration Refrigeration Cycle Example Embodiments

[0412] Summary of Example Embodiments: The present invention may comprise a liquid-phase heat pump, refrigeration cycle, or a heat / ‘cool’ transfer process. The present invention may enable a refrigeration cycle or heat pump by, for example, enabling an endothermic liquid phase transition to occur at a relatively lower temperature and an exothermic phase transition to occur at a relatively higher temperature. The present invention may enable heat transfer with a liquid—liquid enthalpy of phase transition or an adjustable liquid-liquid enthalpy of phase transition. The temperature at which a portion or most of the enthalpy of phase transition occurs may be adjustable, by, for example, adjusting the concentration or composition of the working fluids using, for example, one or more devices for concentration or composition adjustment. Changes or adjustment in the composition and / or system conditions of working fluids in the present invention may enable a change in phase transition temperature or phase transition conditions.

[0413] An Example LCST Embodiment for a refrigeration cycle may comprise:

[0414] Heat Exchanger

[0415] Liquid-Liquid Separation

[0416] Nanofiltration (for example: may be organic solvent nanofiltration) or Reverse Osmosis or Forward Osmosis or Osmotically Assisted Nanofiltration

[0417] Mixing

[0418] Heat Exchanger

[0419] Triggering / initiating an endothermic phase transition through the addition of a permeate stream to a combined solution. Said endothermic phase transition may be triggered through adding a permeate stream, which may comprise mostly ‘small molecular weight reagent’, to a single liquid phase mixture, which may result in an endothermic phase transition, which may result in the formation of a multi-liquid phase mixture.

[0420] An Example UCST Embodiment for a refrigeration cycle process may comprise:

[0421] Heat Exchanger:

[0422] Liquid-Liquid Separation:

[0423] Nanofiltration (for example: may be organic solvent nanofiltration):

[0424] Mixing

[0425] Heat Exchanger

[0426] Triggering / initiating an endothermic phase transition through the addition of a permeate stream to a combined solution. Said endothermic phase transition may be triggered through adding a permeate stream, which may comprise mostly ‘small molecular weight reagent’, to a single liquid phase mixture, which may result in an endothermic phase transition, which may result in the formation of a multi-liquid phase mixture.

[0427] To adjust phase transition temperature range or enable a liquid-liquid phase transition or initiate a liquid-liquid phase transition or a combination thereof, one or more of the following may be employed:

[0428] Membrane Based Process

[0429] Vaporization (for example: may be distillation, membrane distillation, evaporation)

[0430] Precipitation

[0431] Gas Pressurization

[0432] Gas Depressurization

[0433] System Pressurization

[0434] System Depressurization

[0435] Mechanical Pressurization

[0436] Mechanical Depressurization

[0437] Addition of Permeate

[0438] Addition of Condensate

[0439] Addition of Concentrate

[0440] Addition of Precipitate

[0441] Addition of a Regenerable or Regenerated Composition or Reagent

[0442] Process reagents may be stored and / or dispatchable and / or rapidly dispatchable, enabling, for example, cooling or heating to be desynchronized from when electricity or heat or other energy source is consumed to power process. For example, one or more reagents may be stored in a tank, and rapidly dispatched when liquid-liquid phase transition temperature range adjustment is needed. For example, the rate of regeneration of one or more reagents may be slower than the rate which the system can instantaneous dispatch said one or more reagents.Example Embodiment for Phase Transition Temperature Adjustment which may Contain Multiple Concentration Adjustable Reagents in Either or Both or One or More or a Combination of Liquid Phases:

[0443] In some embodiments, the LCST or UCST liquid may phase transition into a non-aqueous phase or organic phase and a mostly water phase or an aqueous phase. Two or more liquid phases may be reversibly transformed into a single liquid phase solution. The temperature of phase transition may be adjusted using, for example reversible adjustments in concentration, or composition, or system conditions or temperature. Said non-aqueous phase may be organic or inorganic or a combination of organics and inorganics and may comprise a mixture of reagents of different molecular weights.

[0444] For example, said non-aqueous phase may comprise a mixture or solution of a reagent with high solubility in water or a defined aqueous solution, and a reagent with relatively lower solubility in water or a defined aqueous solution or limited solubility in water or a defined aqueous solution. The reagent with high solubility in water may be defined as a reagent which is one or more or a combination of the following: fully miscible in water, fully miscible in water over a greater range of temperatures, soluble in water over a greater range of temperatures, soluble in water over a desired range of temperatures, soluble in a defined aqueous solution, soluble in a defined aqueous solution over a greater range of temperatures, or soluble in a defined aqueous solution over a desired range of temperatures. A defined aqueous solution may be defined as an aqueous solution with a specified solute or solutes and / or a specified range of concentrations of a solute or solutions. A defined aqueous solution may comprise an aqueous solution or a solution comprising mostly water or a solution comprising a greater concentration of water than another solution, or a solution comprising a greater concentration of water than said reagent with lower solubility in water or a solution comprising a greater concentration of water than said reagent with high solubility in water. A reagent with relatively lower solubility in water (or a defined aqueous solution) may be defined as a reagent which is one or more or a combination of the following: partially miscible in water, miscible in water over a smaller range of temperatures, soluble in water over a smaller range of temperatures, less soluble or limited solubility in water over a desired range of temperatures, insoluble or low or limited solubility in a defined aqueous solution, soluble in a defined aqueous solution over a smaller range of temperatures, or less soluble or limited solubility in a defined aqueous solution over a desired range of temperatures. It may be advantageous for the low solubility reagent and high solubility reagent to be mutually soluble or miscible in each other.

[0445] Phase transition temperature may be adjusted by adjusting the relative concentration of one or more reagents. For example, it may be desirable for the reagent with high solubility in water and the reagent with low solubility in water to be of different molecular weights or have different vapor pressures or have other different intrinsic properties, which may enable, for example, concentration adjustment, and / or a concentration adjustment resulting phase transition temperature adjustment, when desired. For example, if the reagent with high solubility in water and the reagent with low solubility in water are of different molecular weights, their relative concentration may be adjusted using, for example, organic solvent nanofiltration. For example, if the reagent with high solubility in water and the reagent with low solubility in water are of volatilities or vapor pressures, their relative concentration may be adjusted using, for example, a liquid-vapor or vapor-liquid phase transition method, such as distillation. Experimentally, the inventor has demonstrated, for example, that increasing the relative concentration of high solubility reagent compared to low solubility reagent in some LCST liquid compositions increases the LCST. Experimentally, the inventor has demonstrated, for example, reducing the relative concentration of high solubility reagent compared to low solubility reagent in some LCST liquid compositions decreases the LCST. Similarly, adjusting the relative concentration of reagents in the aqueous liquid phase may enable liquid-liquid phase transition temperature range temperature adjustment. For example, if the aqueous phase contains a salt or an organic compound or an inorganic compound or a combination thereof, the concentration of said reagents and the phase transition temperature range may be adjusted using, for example, a membrane-based process, such as reverse osmosis, forward osmosis or membrane distillation, or a liquid-vapor phase transition process, such as distillation or evaporation or pervaporation, or a precipitation based process or a combination thereof. Experimentally, the inventor has demonstrated, for example, that increasing the relative concentration of salt in the aqueous phase (if the aqueous phase contains salt) in some LCST liquid compositions decreases the LCST.

[0446] An example composition which employs a reagent with high water solubility and a reagent with low water solubility may comprise for example, one or more or a combination of the following:

[0447] A high water solubility reagent which may comprise a relatively larger molecular weight reagent or combination of reagents (for example, which may include, but is not limited to, one or more or a combination of the following: Polyethylene Glycol Dimethyl Ether 500, Polyethylene Glycol Dimethyl Ether 250, Polyethylene Glycol Monomethyl Ether 350, Polyethylene Glycol Monomethyl Ether 550)

[0448] A low water solubility reagent or solvent or a combination thereof which may comprise a relatively smaller molecular weight reagent or combination of reagents (for example, which may include, but is not limited to, one or more or a combination of the following: 2-Butoxyethanol, 2-Ethoxyethanol, Propylene Glycol n-Propyl Ether, Glycol Ether)

[0449] Salt or Salts (for example, may include, but is not limited to, sodium chloride, potassium chloride, calcium chloride, ammonium chloride, ammonium sulfate, sodium sulfate, potassium sulfate) or a Reagent with a high solubility in water and relatively low or limited solubility in one or more other reagents (for example, may include, but is not limited to, glycerol, urea, PEG 200, PEG 400, PEG 600, Dextrose, Maltodextrin)

[0450] Organic Solvent or a Reagent with a high solubility in the primarily organic phase and relatively low or limited solubility in the aqueous phase or aqueous phase reagents (for example, may include, but is not limited to, ethyl acetate, methyl acetate, propyl acetate, dimethyl ether, diethyl ether, dimethoxymethane, diethoxymethane, diethoxymethane, ethylene glycol diacetate, propylene glycol diacetate, Ethylene Glycol Diacetate Propylene Glycol Diacetate Dipropylene Glycol Dimethyl Ether (DPE) 2-Heptanone Propylene glycol monomethyl ether acetate Propylene Carbonate Cyclohexanone Dipropylene Glycol n-Butyl Ether (DPnB) Tri(propylene glycol) butyl ether, mixture of isomers (TPnB) Propylene glycol n-butyl ether (PnB) Dipropylene Glycol n-Propyl Ether (DPnP), n-butanol)

[0451] Water

[0452] Said composition may possess a LCST phase transition temperature range, at or above which the liquid may phase transition into two liquid phases which may comprise, for example, a primarily organic liquid phase and a primarily aqueous liquid phase. The primarily organic liquid phase may comprise a combination of high water solubility reagent and low water solubility reagent, and may contain minority concentrations of, for example, water and / or other aqueous liquid phase components. The primarily aqueous liquid phase may comprise a combination of water and salt or other reagent with high affinity for water relative to the primarily organic liquid phase, and may contain minority concentrations of, for example, high water solubility organic and / or low solubility organic. In said example composition, increasing the concentration of high water solubility reagent relative to low water solubility reagent may result in an increase in LCST and decreasing the concentration of high water solubility reagent relative to low water solubility reagent may result in a decrease in LCST. In said example composition, increasing the concentration of a salt or salts or a reagent with a high solubility in water and relatively low or limited solubility in the organic phase reagents may result in a decrease in LCST and decreasing the concentration of a salt or salts or a reagent with a high solubility in water and relatively low or limited solubility in the organic phase reagents may result in an increase in LCST.

[0453] Phase transition temperature may be adjusted by, for example, adjusting the relative concentration of one or more reagents by one or more or a combination of methods described herein. For example, with the example composition described in the present embodiment, the phase transition temperature may be adjusted by, for example, including, but not limited to, adjusting the relative concentration of the high water solubility reagent relative to the low water solubility reagent, adjusting the concentration of salt or reagent with high affinity for water relative to the organic phase, adjusting the concentration of water or a combination thereof.

[0454] The relative concentration of high solubility reagent to relatively low solubility reagent may be designed for specific concentration ranges depending on the method or methods employed for phase transition temperature adjustment. If the phase transition temperature is adjusted by adjusting the relative concentration of the high water solubility reagent relative to the low water solubility reagent, said concentration may adjusted by size based separation (such as, for example, a membrane based process) or a vapor-liquid or liquid-vapor phase transition concentration adjustment process. For size-based concentration adjustment process, it may be desirable for the large molecular weight reagent to be at a concentration sufficiently low relative to smaller molecular weight reagent such that it can be practically concentrated using the desired size based separation method. Size based separation methods, such as membrane-based processes for size based separation, may have limitations of the osmotic pressure and viscosity at which they can function. For example, with the example composition described, it may be desirable for the concentration of the larger molecular weight reagent to be less than 35 wt % based on the osmotic pressure limitations of 2017 organic solvent nanofiltration membranes. As technologies for organic solvent nanofiltration advance, the maximum concentration of a retentate in an organic solvent nanofiltration process may increase. Furthermore, other technologies or techniques, such as osmotically assisted nanofiltration, or osmotically assisted organic solvent nanofiltration, or ultra-high pressure nanofiltration, or forward osmosis, or DTRO, or other separation techniques, or a combination thereof may be employed. For vapor-liquid or liquid-vapor phase transition concentration adjustment processes, the concentration of the higher volatility or vapor pressure reagent relative to the lower volatility or vapor pressure reagent may employed in concentrating. For example, with a composition at least one reagent possessing volatility, distillation or pervaporation or evaporation or membrane distillation may be conducted to increase the concentration of, for example, the high water solubility reagent.

[0455] Phase transition temperature may be adjusted by adjusting the concentration of salt or reagent with high affinity for water relative to the organic phase. Concentration of said salt or reagent with high affinity for water relative to the organic phase may be adjusted using, for example, including, but not limited to, one or more or a combination of the following: membrane based process, size based separation process, a liquid-vapor based separation process, a vapor-liquid based separation process, precipitation or a combination thereof.

[0456] Phase transition temperature may be adjusted by adjusting the concentration of organic solvent or a reagent with a high solubility in the primarily organic phase and relatively low or limited solubility in the aqueous phase or aqueous phase reagents. Concentration of said reagent may be adjusted using, for example, including, but not limited to, one or more or a combination of the following: membrane based process, size based separation process, a liquid-vapor based separation process, a vapor-liquid based separation process, precipitation or a combination thereof.

[0457] In the case of the example composition, the high water solubility reagent and the low water solubility reagent may tend to ‘follow’ each other. The reagents ‘following’ each other may mean a significant portion or most of the high water solubility reagent and low water solubility reagent in the liquid system will be in the same liquid phase. For example, if two liquid phases form, a large portion of or most of the high water solubility reagent and low water solubility reagent may be present in the same liquid phase, which may comprise an organic liquid phase.

[0458] For example, the non-aqueous phase may comprise a mixture of a reagent with high water solubility and a reagent with low water solubility, and said high water solubility reagent may comprise a ‘large molecular weight reagent’ and said high water solubility reagent may comprise a ‘small molecular weight reagent’. In an example embodiment, an increase in concentration of said ‘large molecular weight reagent’ relative to said ‘small molecular weight reagent’ may result in, for example, including, but not limited to, one or more or a combination of the following: a relatively greater lower critical solution temperature (LCST), a relatively lower upper critical solution temperature (UCST), the ability to dissolve in an aqueous phase, the ability to dissolve in an associated aqueous phase, increased solubility in an aqueous phase, or the ability to dissolve in an associated aqueous phase.

[0459] Phase transitioning liquids may comprise entirely organic reagents or may entirely be non-aqueous. Temperature driven phase transition or concentration driven phase transitioning or both may occur due to formulations of different properties. For example, one liquid phase may comprise polar organic solvents while another aqueous phase may comprise non-polar solvents or less polar solvents or selectively polar solvents or a combination. Phase transitioning may be driven by intrinsic properties other than or in addition to polarity, for example, which may include organics with different functional groups or structures.

[0460] A simple example of an organic solvent only phase transitioning liquid may comprise for example:

[0461] Non-polar organic solvent (for example, which may include, but is not limited to: octane, heptane, hexane, butane, toluene, silicon oils, fluorocarbons, oils, mineral oil, hydrocarbon)

[0462] Polar organic solvent or non-water reagent which may independently have limited solubility or be non-soluble in said non-polar organic solvent (for example, which may include, but are not limited to: propylene carbonate, ethylene glycol, methanol, ethanol, isopropanol, acetone, ammonia, acetonitrile, DMSO, THF, butanol)

[0463] Organic Solvent with solubility in both polar and non-polar organic solvent (for example, which may include, but are not limited to: polyethylene glycol dimethyl ether, polyethylene glycol monomethyl ether, 2-butoxyethanol, glycol ethers, acetone, diglyme, methyl formate)

[0464] Advantageously, an organic-only phase transitioning liquid may be a liquid which can operate in environments where water or aqueous systems may be incompatible. For example, said organic-only phase transitioning liquid may be a dielectric liquid, enabling use with, for example, direct contact with electronic devices. Advantageously, an organic only phase transitioning liquid (which may possess, for example, a LCST or UCST or both or a more gradual phase transition, or a combination thereof) may enable significantly greater heat transfer rates and effective heat capacity relative to other dielectric fluids, while maintaining the benefits of a dielectric fluid. This may enable, for example, heat transfer rates approaching or near or at or greater than water or anti-freeze water, while employing a liquid with dielectric properties. This may enable enhanced performance or smaller size or lower cost or greater lifespan of, for example, high power electronics (for example, including, but not limited to, transmission stations, power converters, inverters, transformer stations, transformers) which require dielectric liquids for heat transfer fluids.

[0465] Phase transitioning may be driven by, for example, adjustments in concentration of one or more reagents, adjustments in temperature, or a combination thereof.

[0466] In some embodiments, the aqueous phase may not contain water or substantially less water. For example, the aqueous phase may also or alternatively refer to a 1) mostly inorganic liquid phase; or 2) a more polar liquid phase; or both. For example, the ‘aqueous phase’ or ‘inorganic phase’ or ‘polar phase’ may comprise mostly liquid ammonia or highly concentrated aqueous ammonia or highly concentrated amin...

Claims

1. A heat transfer fluid comprising:(a) an alkylene carbonate; and(b) at least one organic solvent selected from an alkylene glycol, or a glycol ether; andwherein the fluid is a dielectric liquid, comprises less than 30 weight percent of water, and has an effective heat capacity greater than water.

2. The heat transfer fluid of claim 1 wherein the alkylene carbonate is propylene carbonate or ethylene carbonate.

3. The heat transfer fluid of claim 1 wherein the alkylene glycol is ethylene glycol or propylene glycol.

4. The heat transfer fluid of claim 1 wherein the glycol ether is 2-butoxyethanol, ethylene glycol phenyl ether, propylene glycol phenyl ether, diethylene glycol n-butyl ether, triethylene glycol mono n-butyl ether, tripropylene glycol butyl ether, tripropylene glycol n-butyl ether, triethylene glycol mono methyl ether, triethylene glycol mono n-butyl ether, polyethylene glycol monomethyl ether, tripropylene glycol methyl ether, diethylene glycol hexyl ether, or polyethylene glycol dimethyl ether.

5. The heat transfer fluid of claim 1 whereinthe alkylene carbonate is propylene carbonate or ethylene carbonate; andthe at least one organic solvent is the alkylene glycol wherein the alkylene glycol is selected from ethylene glycol and propylene glycol.

6. The heat transfer fluid of claim 1 whereinthe alkylene carbonate is propylene carbonate or ethylene carbonate; andthe at least one organic solvent is the glycol ether wherein the glycol ether is selected from 2-butoxyethanol, ethylene glycol phenyl ether, propylene glycol phenyl ether, diethylene glycol n-butyl ether, triethylene glycol mono n-butyl ether, tripropylene glycol butyl ether, tripropylene glycol n-butyl ether, triethylene glycol mono methyl ether, triethylene glycol mono n-butyl ether, polyethylene glycol monomethyl ether, tripropylene glycol methyl ether, diethylene glycol hexyl ether, and polyethylene glycol dimethyl ether.

7. The heat transfer fluid of claim 1 wherein a liquid phase of the heat transfer fluid has an observed beat capacity that exceeds a calculated heat capacity based on the heat transfer fluid's composition.

8. A process for heat transfer comprising:forming a dielectric fluid comprising an alkylene carbonate and an organic solvent comprising a glycol ether;absorbing heat endothermically in a heat exchange;releasing heat exothermically in a second heat exchange;wherein the formed dielectric fluid comprises a liquid; andwherein a liquid phase of the formed dielectric fluid has an observed heat capacity that exceeds a calculated heat capacity based on the formed dielectric fluid's composition.

9. The process of claim 8 wherein the formed dielectric liquid exhibits a liquid-liquid phase transition temperature range.

10. The process of claim 9 wherein the process is operated in the temperature range of the liquid-liquid phase transition temperature range.

11. The process of claim 8 wherein the organic solvent further comprises an alkylene glycol.

12. The process of claim 8 wherein the organic solvent further comprises a non-polar organic solvent.

13. The process of claim 12 wherein the non-polar organic solvent is octane, heptane, hexane, butane, toluene, silicon oils, fluorocarbons, oils, mineral oil, or hydrocarbon.

14. The process of claim 8 wherein the formed dielectric fluid exhibits a gradual phase transition.

15. The process of claim 8 wherein the absorbed heat is from an electronic device.

16. The process of claim 15 wherein the electronic device comprises a battery, a computer, a server, a PC, an AI brain, an AI chip, a data center, a VTOL, a rail, a drone, HVAC, an industrial chiller, a printer, a transmission station, a power converter, an inverter, a transformer station, or a transformer.

17. The process of claim 8 wherein the formed dielectric fluid comprises less than 30 weight percent concentration of water, and has an effective heat capacity greater than water.

18. The process of claim 11 whereinthe alkylene carbonate is propylene carbonate or ethylene carbonate; andthe alkylene glycol is selected from ethylene glycol and propylene glycol.

19. The process of claim 8 whereinthe alkylene carbonate is propylene carbonate or ethylene carbonate; andthe glycol ether is selected from 2-butoxyethanol, ethylene glycol phenyl ether, propylene glycol phenyl ether, diethylene glycol n-butyl ether, triethylene glycol mono n-butyl ether, tripropylene glycol butyl ether, tripropylene glycol n-butyl ether, triethylene glycol mono methyl ether, triethylene glycol mono n-butyl ether, polyethylene glycol monomethyl ether, tripropylene glycol methyl ether, diethylene glycol hexyl ether, and polyethylene glycol dimethyl ether.

20. A process for heat transfer comprising:forming a dielectric fluid comprising an alkylene carbonate and an alkylene glycol;absorbing heat endothermically into the formed dielectric fluid in a heat exchange with an electronic device;releasing heat exothermically from the formed dielectric fluid in a second heat exchange;wherein the formed dielectric fluid comprises a liquid; andwherein a liquid phase of the formed dielectric fluid has an observed heat capacity that exceeds a calculated heat capacity based on the formed dielectric fluid's composition;wherein the alkylene carbonate is propylene carbonate or ethylene carbonate; andwherein the alkylene glycol is ethylene glycol, propylene glycol, 2-butoxyethanol, ethylene glycol phenyl ether, propylene glycol phenyl ether, diethylene glycol n-butyl ether, triethylene glycol mono n-butyl ether, tripropylene glycol butyl ether, tripropylene glycol n-butyl ether, triethylene glycol mono methyl ether, triethylene glycol mono n-butyl ether, polyethylene glycol monomethyl ether, tripropylene glycol methyl ether, diethylene glycol hexyl ether, or polyethylene glycol dimethyl ether.

21. The process of claim 20 wherein the electronic device comprises a battery, a computer, a server, a PC, an AI brain, an AI chip, a data center, a VTOL, a rail, a drone, HVAC, an industrial chiller, a printer, a transmission station, a power converter, an inverter, a transformer station, or a transformer.

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