Heat recovery system and distillation and dehydration method

Description

1 / 52 “HEAT RECOVERY SYSTEM AND DISTILLATION AND DEHYDRATION METHOD” Cross-References to Related Requests

[001] The present invention claims the benefit and priority to U.S. Provisional Patent Application No. 63 / 256,116 entitled “INTEGRATED HEAT-POWERED PROCESS AND SYSTEM FOR ORGANIC SOLVENT PRODUCTION USING VAPOR RECOMPRESSION” filed October 15, 2021, and to U.S. Provisional Patent Application No. 63 / 338,725 entitled “INTEGRATED HEAT-POWERED PROCESS AND SYSTEM FOR ORGANIC SOLVENT PRODUCTION USING VAPOR RECOMPRESSION” filed May 5, 2022, each of which is incorporated herein in its entirety. Background of the Invention

[002] To produce an organic solvent, such as fuel ethanol, water and fermentation solids must be removed. Typical processes utilize a series of distillation steps combined with a dehydration unit operation to achieve 99% by volume or higher organic solvent content, depending on specifications. To provide an integrated system that delivers low steam consumption in the production of organic solvents, different heat integration approaches have been implemented. These approaches include the use of a membrane for partial or total dehydration of a stream, such as a 120P or 190P stream, implementation of mechanical vapor recompression to further increase heat recovery from vapor streams, and other alternatives for heat integration in distillation, dehydration, and evaporation. Brief Description of the Invention

[003] The present invention provides new and innovative systems and methods for producing organic solvents (e.g., ethanol) that Petition 870260078936, dated 06 / 08 / 2026, page 11 / 84 2 / 52 utilize vapor recompression. The addition of vapor recompression allows for greater heat recovery within a stream, increasing the condensation temperature and pressure of that stream and subsequently using its latent heat to condense it.

[004] Additional features and advantages of the disclosed method and apparatus are described and will be evident from the following Detailed Description and Figures. The features and advantages described herein are not exhaustive and, in particular, many additional features and advantages will be apparent to a person skilled in the art by looking at the figures and description. Furthermore, it should be noted that the language used in the descriptive report has been selected primarily for readability and instruction purposes, and not to limit the scope of the inventive subject matter. Brief Description of the Figures

[005] Figure 1 illustrates an organic solvent production system with a separation system including an extraction column and a membrane that generates a retentate vapor that is condensed through a condenser, according to one aspect of the present invention.

[006] Figure 1A illustrates an organic solvent production system with a separation system including a single rectification / extraction column, according to one aspect of the present invention.

[007] Figure 2 illustrates an organic solvent production system with a separation system including an extraction column and a membrane that generates a retentate vapor that is condensed through one or more evaporators, according to one aspect of the present invention.

[008] Figure 3 illustrates an organic solvent production system with a separation system including both MSU dehydration and a membrane dehydration system, according to one aspect of the present invention. Petition 870260078936, dated 06 / 08 / 2026, page 12 / 84 3 / 52

[009] Figure 4 illustrates an organic solvent production system with a separation system including a vaporizer and a membrane, according to one aspect of the present invention.

[010] Figure 5 illustrates an organic solvent production system including an extraction column and an MSU, according to one aspect of the present invention.

[011] Figure 6 illustrates an organic solvent production system including a heat recovery system, according to one aspect of the present invention.

[012] Figure 7 illustrates an organic solvent production system including a heat recovery system, according to one aspect of the present invention.

[013] Figure 8 illustrates an organic solvent production system including a heat recovery system, according to one aspect of the present invention.

[014] Figure 9 illustrates an organic solvent production system including a heat recovery system, according to one aspect of the present invention.

[015] Figure 10 illustrates an organic solvent production system including a heat recovery system, according to one aspect of the present invention.

[016] Figure 11 illustrates an organic solvent production system including a heat recovery system, according to one aspect of the present invention.

[017] Figure 12 illustrates an organic solvent production system including a heat recovery system, according to one aspect of the present invention.

[018] Figure 13 illustrates a solvent production system. Petition 870260078936, dated 06 / 08 / 2026, page 13 / 84 4 / 52 organic including a heat recovery system, according to one aspect of the present invention.

[019] Figure 14 illustrates an organic solvent production system including a heat recovery system, according to one aspect of the present invention.

[020] Figure 15 illustrates a heat recovery system, according to one aspect of the present invention.

[021] Figure 16 is a flowchart of an exemplary method for operating an organic solvent production plant through an integrated heat process using vapor recompression, according to one aspect of the present invention. Detailed Description of the Invention

[022] The distillation and dehydration system provided is configured to produce an anhydrous organic solvent (e.g., >99% by vol.). The system provided is described below in connection with the production of anhydrous ethanol. Ethanol, however, is only one example and the following description applies equally to the production of other suitable organic solvents using the systems and methods provided. For example, such suitable organic solvents may include isobutanol, isopropanol, ketones, etc.

[023] Various purities of the organic solvent can be produced at different purity levels of the exemplary production system. As used herein in relation to the examples given for ethanol, 120 proof (120P), 190 proof (190P) and 200 proof (200P) are used for two purity levels for approximately at least 60% ethanol by volume, approximately at least 95% ethanol by volume and at least 99% ethanol by volume, respectively, but other purity levels may be specified for use according to the present invention.

[024] In addition, several materials can be referred to here as Petition 870260078936, dated 06 / 08 / 2026, page 14 / 84 5 / 52 “free” of other material (e.g., free of solids, free of solvent, free of water), indicating that the first material has been distilled, filtered, or otherwise separated to remove (or be freed from) at least a portion of the second material. For example, a base liquid containing fifty percent water and fifty percent an organic solvent (e.g., ethanol) may be subjected to a first distillation process to produce a first water-free stream of thirty percent water and seventy percent organic solvent, which may be subjected to a second distillation process to produce a second water-free stream of ten percent water and ninety percent organic solvent.In contrast, various materials may be referred to here as “enriched” with another material (e.g., solvent-enriched), indicating that the first material has been distilled, filtered, concentrated, or otherwise supplemented to increase the concentration of the second material. Using the previous examples, water-free streams may also be considered as solvent-enriched streams, and the remaining base material (from which the solvent-enriched streams were separated) may be considered as water-enriched streams compared to their respective inputs.

[025] The supplied system includes vapor recompression (e.g., a mechanical or thermal vapor recompression unit) to recover heat from a rectification-distillation section (e.g., a rectification / extraction column). The addition of vapor recompression allows for greater heat recovery within a stream, increasing the condensation temperature and pressure of that stream and subsequently using its latent heat to condense it. Vapor recompression units compress a vapor from a lower pressure to a higher pressure. Examples include motor-driven, electrically powered, and motor-driven compressors (both called MVRs or mechanical recompression units). Petition 870260078936, dated 06 / 08 / 2026, page 15 / 84 6 / 52 of steam), or thermal vapor recompression units that forgo electrical energy and instead use motive steam to drag and compress low-pressure vapor to a higher pressure (e.g., a steam jet pump). While the examples given here may cite one type of compressor using one type of energy source, different energy sources or compressor types may be used in a system design according to the system's operational constraints. The energy savings provided by adding a vapor recompression unit to an organic solvent plant can be substantial when compared to the energy required to produce the steam that will be used in the plant.

[026] Several components of the systems currently disclosed may be in fluid communication with each other, such as through piping. Two components in fluid communication with each other may be in direct fluid communication (for example, piping directly connects the two components) or may have intermediate components or processing between the two components, such as filters, pumps, heaters, odor removal vessels, etc.

[027] Figure 1 illustrates an example of an organic solvent production system (100), such as an ethanol production system. In at least some respects, the provided organic solvent production system (100) can be described as including five sections: (i) a feed extraction section, (ii) a rectification-distillation section, (iii) a compression section, (iv) a dehydration section, and (v) an evaporation section.

[028] In the feed extraction section, the feed, comprising a mixture of organic solvent, water and solids, may be directed to at least one distillation column (102a-b) (generally or collectively, distillation column (102) a beer column). By Petition 870260078936, dated 06 / 08 / 2026, page 16 / 84 7 / 52 For example, the feed can be directed to a first distillation column (102a) (BC 1), which thus forms a solids-free vaporous top stream and an organic solvent-free bottom stream. In some aspects, the system provided may include a second distillation column (102b) (BC 2), which requires splitting the feed into two portions by a divider (138) (e.g., a centrifuge, valve, Y-joint, etc.). In such aspects, the first portion can be directed to the first distillation column (102a) which thus forms a solids-free vaporous top stream and an organic solvent-free bottom stream. The second portion can be directed to the second distillation column (102b) which thus forms a solids-free vaporous top stream and an organic solvent-free bottom stream.In some respects, the first distillation column (102a) may operate at a different pressure (higher or lower) than the second distillation column (102b). In some respects, one or both portions may be preheated before reaching the respective distillation column (102) by a preheating heat exchanger (114e) (generally or collectively, heat exchanger (114)).

[029] In some respects, the first distillation column (102a) may be driven by process vapors through direct injection, such as vapors from one or more evaporators (130a-h) (generally or collectively, evaporators (130) or evaporator systems) in the evaporation section (132). In some respects, the first distillation column (102a) may be driven by vapors from process streams generated in vaporization vessels (104a-d) (generally or collectively, vaporization vessel (104)). In some respects, the first distillation column (102a) may be driven by instantaneous cooking vapors. For example, in the example illustrated in Figure 1, the first distillation column (102a) is driven by a combination of fourth-effect vapors and cooking vaporization. In other respects, the Petition 870260078936, dated 06 / 08 / 2026, page 17 / 84 8 / 52 The first distillation column (102a) may additionally or alternatively be driven by a beer column reboiler (106a-c) (generally or collectively, reboiler (106)), as illustrated for the second distillation column (102b) in Figure 1, with a combination of evaporator vapors, cooking vapors, vapors generated by vaporizing a portion of the organic solvent-free bottom stream from the second distillation column or other process streams.

[030] In some aspects having the second distillation column (102b), the second distillation column (102b) may be driven by process vapors through direct injection. In other aspects, the second distillation column (102b) may additionally or alternatively be driven by steam through a beer column reboiler (106). For example, in the illustrated aspect, the second distillation column (102b) is driven only by a beer column reboiler (106a). In some cases, the vapor condensate from the beer column reboiler (106a) is evaporated in a vaporization vessel (104). In such cases, the low-pressure steam generated by the vaporization vessel (104) can be used to power the reboiler (106b) of the side extraction column (110) in the rectification distillation section and / or heat an upper stream of the rectification column (108), or it can be used to heat any other suitable stream having a lower temperature.

[031] In at least some respects, the upper vapor stream from the first distillation column (102a) can be directed directly (i.e., without any intervening components) to the rectifying distillation section. For example, the upper vapor stream from the first distillation column (102a) can be directed directly to a rectifying column (108). In other words, the upper vapor stream from the first distillation column (102a) can be introduced into the rectifying column. Petition 870260078936, dated 06 / 08 / 2026, p. 18 / 84 9 / 52 (108) as a vapor without first being condensed. As described in more detail below in relation to the rectification-distillation section, the rectification-distillation section may include a rectification / extraction column (112) (Figure 1A) or, as shown in Figure 1, a rectification column (108) in fluid communication with a side extraction column (110). As such, references made to a rectification column (108) and / or a side extraction column (110) may alternatively be a rectification / extraction column (112).

[032] The vaporous upper stream of the second distillation column (102b) can be condensed. In some aspects, the vaporous upper stream of the second distillation column (102b) can be condensed through a condenser (140). In one example, the first distillation column (102a) can operate at a higher pressure than the second distillation column (102b) and the vaporous upper stream of the second distillation column (102b) can be condensed through a condenser (140). In other aspects, the vaporous upper stream of the second distillation column (102b) can be condensed through one or more evaporators (130) in the evaporation section (132). In one example, the first distillation column (102a) may operate at a lower pressure than the second distillation column (102b) and the upper vapor stream from the second distillation column (102b) may be condensed through one or more evaporators (130) in the evaporation section (132).In some respects, the condensed top stream from the second distillation column (102b) can be directed to a separation system of the dehydration section. In other respects, the condensed top stream from the second distillation column (102b) can be directed to a rectification column (108) of the rectification distillation section. In still other respects, a first portion of the condensed top stream from the second distillation column (102b) can be... Petition 870260078936, dated 06 / 08 / 2026, page 19 / 84 10 / 52 directed to the separation system, while a second portion of the condensed upper stream from the second distillation column (102b) can be directed to the rectification column (108).

[033] The bottom stream from the first distillation column (102a) can be directed to the evaporation section (132). At least a portion of the organic solvent-free bottom stream from the second distillation column (102b) can be directed to the evaporation section (132). For example, in the illustrated example in Figure 1, the bottom streams from the first distillation column (102a) and the second distillation column (102b) are directed to the evaporation section (132). In some cases, a portion of the bottom stream from the second distillation column (102b) can be directed to the evaporation section via a vaporization vessel (104a) and / or a heat exchanger (114a-g) to recover its sensible heat.The various heat exchangers (114) discussed herein can be used to adjust (e.g., heating or cooling) the temperature of a first medium by exchanging heat with a second medium of a different temperature, thereby affecting the opposite temperature adjustment in the second medium. In some respects, a portion of the bottom stream from the second distillation column (102b) can be directed to the first distillation column (102a). In some respects, a portion of the bottom stream from the second distillation column (102b) can be directed to a vaporization vessel (104) where the generated vapors are directed to the evaporator vapors to drive the first distillation column (102a) or rectification column (108). In some respects, a remaining liquid portion resulting from the evaporation of the bottom stream portion from the second distillation column (102b) can exchange heat with another process stream before being directed to the evaporation section (132).

[034] In at least some respects, the distillation section Petition 870260078936, dated 06 / 08 / 2026, page 20 / 84 11 / 52 rectifier may include a rectifier / extraction column (112) (Figure 1A). The rectifier / extraction column (112) may be a single distillation unit in which both rectification and extraction occur. In some respects, the rectifier / extraction column (112) may be a rectifier column (108) in fluid communication with a separate side extraction column (110). Although some of the Figures show the rectifier / extraction column (112) as a separate rectifier column (108) and a side extraction column (110), it should be appreciated that the following description applies equally to a single integrated rectifier / extraction column (112). For example, streams described as being directed to or from the rectifier column (108) or to the side extraction column (110) may be directed to or from a single rectifier / extraction column (112).

[035] In various embodiments, the vaporous top stream from the first distillation column (102a) can be directed directly to the rectifier column (108), thus forming an organic solvent-rich top stream and a bottom stream. The bottom stream from the rectifier can be directed to the side extraction column (110) in some aspects, which can thereby form a top stream directed back to the rectifier column (108) and an organic solvent-free bottom stream. The organic solvent-free bottom stream can be directed to another area of ​​the organic solvent production plant (e.g., the cooking section) in which the supplied system is located. In some aspects, the side extraction column (110) can be driven by direct steam injection and / or steam. In other aspects, the side extraction column (110) can be driven by process steam or steam through a reboiler (106b).In some examples, a first portion of the organic solvent-free bottom stream generated by the side extraction column (110) can be directed to a reboiler (106) driven by steam or vapors. Petition 870260078936, dated 06 / 08 / 2026, page 21 / 84 12 / 52 of the vaporization process and a second portion of the organic solvent-free bottom stream can be routed to a forward end of the organic solvent production plant where the supplied system is located.

[036] In several respects, the organic solvent-rich top stream formed by the rectifier column (108) may have any concentration below the azeotropic concentration. In one example, the top rectifier stream may be 190 proof (190P). A portion of the top rectifier stream may be condensed, such as through a capacitor (140). In some respects, at least a portion of the condensed top rectifier stream may be directed to a storage tank (116a-e) (generally or collectively, storage tank (116)). In some respects, a portion of the condensed top rectifier stream may return to the rectification section as a reflux stream. At least a portion of the condensed top rectifier stream may be directed (e.g., through the storage tank (116a)) to a separation system of the dewatering section.For example, a portion of the condensed rectifier overhead stream can be directed to an extraction column (122) or a vaporizer (118) of the separation system.

[037] At least a portion of the rectifier overhead stream may be directed to a vapor recompression unit (120a-c) (generally or collectively, vapor recompression unit (120)) of the compression section. The vapor recompression unit (120a) may be configured to compress the portion of the rectifier overhead stream, thereby generating a compressed vaporous rectifier overhead stream. In various respects, a vapor recompression unit (120) may include a compressor or jet pump that is used to compress and thus increase the pressure of a vapor received by the vapor recompression unit (120) to produce a vapor Petition 870260078936, dated 06 / 08 / 2026, page 22 / 84 13 / 52 tablet at a higher pressure.

[038] In some instances, the vapor recompression unit (120) may be a mechanical vapor recompression unit. A mechanical vapor recompression unit uses an electrically driven compressor. Typical compressors that may be used include rotary lobe positive displacement compressors (also known as Roots System Roots-type blowers), centrifugal turbocompressors, centrifugal fans, or axial compressors. As an example, a typical positive displacement rotary lobe compressor operates with two interlocking rotors mounted on parallel shafts. The two rotors rotate in opposite directions. As each rotor passes the blower inlet, a defined volume of vapor / gas is retained (e.g., the displaced volume) and this retained vapor / gas is carried around the jacket to the blower outlet.As each rotor passes through the blower outlet, the gas / vapor is compressed to the desired system pressure and expelled. The appropriate compressor type may depend on the operating conditions (e.g., required pressure, volumetric flow rate, etc.) of the application for which the mechanical vapor recompression unit is used.

[039] In some examples, the vapor recompression unit (120) may be a thermal vapor recompression unit. A thermal vapor recompression unit is based on the principle of the steam jet pump which compresses low pressure vapor / steam (e.g. vaporization vapors or evaporator effect vapors) using a portion of high pressure vapor, also known as motive steam, to produce intermediate pressure vapor / steam which can be used as a heating medium (e.g. distillation heating).

[040] In several respects, the compressed upper rectifier current can be directed entirely to one or more evaporators. Petition 870260078936, dated 06 / 08 / 2026, p. 23 / 84 14 / 52 (130) of the evaporation section (132). For example, the compressed rectifier top stream can be directed entirely to a first evaporator (130a) (1) (e.g., as in Figure 2). In another case, a portion of the compressed rectifier top stream can be directed to a first evaporator (130a) while another portion is directed to a second evaporator (130b) (e.g., as in Figure 1). The compressed rectifier top stream can be condensed by one or more evaporators (130) in the evaporation section (132), thus transmitting energy in cascade between distillation and evaporation. Such energy cascade helps to reduce (or eliminate) steam consumption in evaporation compared to typical systems that are heavily dependent on steam to drive evaporation, which therefore reduces the energy consumption of the supplied system compared to typical systems.In some respects, the compressed rectifier overhead stream directed to the evaporation section (132) may return as reflux to the rectifier column (108).

[041] In some aspects, a portion of the compressed rectifier topstream may be directed to the dehydration section, such as to the extraction column (122) or to a vaporizer (118). In such aspects, the portion of the compressed rectifier topstream directed to the dehydration section may be further compressed through one or more compression stages (e.g., one or more separate vapor recompression units (120)) before being introduced into the dehydration section. A particular example of the system provided includes a portion of the compressed rectifier topstream being directed to the evaporation section (132) while another portion of the compressed rectifier topstream is directed to the dehydration section.

[042] As further described in connection with Figure 2, the portions of the upper rectifier current that are condensed or Petition 870260078936, dated 06 / 08 / 2026, p. 24 / 84 15 / 52 compressed currents can be varied. For example, the portion of the upper rectifier current that is compressed may depend on the energy required to drive the evaporation, with the remaining upper rectifier current being condensed. As such, capacitor (140) may or may not be operational in several respects.

[043] In at least some respects, the dehydration section includes a separation system. In the exemplary system of Figure 1, the separation system may include an extraction column (122) and a membrane (124) (e.g., a semipermeable membrane). The extraction column (122) generates an upper vapor stream from a concentrated organic solvent-water feed stream that is directed to contact the membrane (124). The extraction column (122) may also generate a bottom stream that may be directed to another area of ​​the organic solvent production plant where the supplied system is located. In several respects, the bottom stream from the extraction column may be used to heat a suitable cold stream (e.g., steam condensate, process water, purification water, 190P, a regenerated stream, a beer feed stream, etc.).In some respects, the extraction column (122) may be driven by a reboiler (106c). In some examples, the vapor condensate from the extraction column reboiler (106c) is evaporated in a vaporization vessel (104). In such examples, the low-pressure vapor generated by the vaporization vessel (104) may be used to drive the reboiler (106b) of the side extraction column (110) in the rectification distillation section and / or heat the upper stream of the rectification column (108), or may be used to heat any other suitable stream having a lower temperature.

[044] The membrane (124) continuously removes water from the concentrated organic solvent-water feed stream to produce a Petition 870260078936, dated 06 / 08 / 2026, page 25 / 84 16 / 52 a water-rich vapor stream (permeate) and an anhydrous organic solvent-rich vapor stream (retentate). For example, the anhydrous ethanol-rich vapor stream may include 99% by volume or more of organic solvent. In some respects, the membrane (124) may be a polymer membrane. The polymer membrane (124) may be constructed of hollow fibers. A selective layer may be placed on the outer (e.g., shell side) or inner (e.g., lumen side) of the hollow fibers. In other examples, the membrane (124) may have other suitable forms that adequately dewater a feed vapor stream as part of a high-grade organic solvent production process, such as tubular membranes including zeolite membranes or spiral-wound membranes.

[045] In at least some respects, the retentate vapor generated by the membrane (124) in the separation system can be condensed. For example, the retentate vapor can be condensed through a condenser (140) against any available cold stream. In other cases, the retentate vapor can be condensed through one or more of the evaporators (130) in the evaporation section (132). The condensed retentate liquid can be directed to a tank (116b) (e.g., a tank (200P)) for storage. In some respects, before the condensed retentate liquid reaches the tank (116b), the condensed retentate can be directed to a vaporization vessel (104b) where the 200-proof vaporization vapor stream produced can recover its heat elsewhere and be directed to a CO2 removal system. The CO2 removal system is a low-pressure vaporization vessel (104c) in which vapor and a liquid stream are generated.The vapor stream is directed to a 190 (114b) proof heat exchanger and the liquid stream is directed to the condensate retentate stream. In some cases of the system supplied, the condensate retentate from the 200P (104b) vaporization vessel is directed. Petition 870260078936, dated 06 / 08 / 2026, page 26 / 84 17 / 52 for an economizer (126). The net energy of the retentate can be further recovered against other process streams (e.g., permeate liquid, purification bottoms). For example, the retentate liquid can heat both the permeate liquid in a heat exchanger (114) and the purification bottoms in a heat exchanger (114).

[046] In several examples, the permeate vapor generated by the membrane (124) in the separation system can be condensed. For example, the heat available in the permeate vapor can be used to heat a suitable cold stream (e.g., steam condensate, process water, purification water, 190P, a regenerated stream, a beer feed stream, etc.) in a condenser (140), thus condensing the permeate vapor into a liquid.

[047] In some examples, such as that illustrated in Figure 1, the condensed permeate liquid can be directed back to the extraction column (122). The permeate liquid can be heated by a suitable hot stream (e.g., vaporization vapors, side extraction bottom stream, extraction column bottom stream, retentate liquid, etc.) in a heat exchanger (114) before being introduced into the extraction column (122) in some respects. For example, the permeate liquid can be heated by the retentate liquid in the heat exchanger (114).

[048] The use of membrane dehydration with vapor recompression may offer advantages over the use of molecular sieve units (128) (MSUs). For example, the use of membrane dehydration may provide an organic solvent plant with: (i) a stable and continuous distillation section by eliminating regenerated streams from molecular sieves, (ii) continuous operation compared to cyclic operation for molecular sieve regeneration, (iii) a constant rectifying overhead stream flow that can then be used by a unit of Petition 870260078936, dated 06 / 08 / 2026, page 27 / 84 18 / 52 vapor recompression to allow its heat recovery, (iv) lower energy consumption in distillation, removing the treatment of additional streams from the MSUs (128), such as regeneration, and (v) a modular system and therefore easy to increase capacity by introducing additional membrane cartridges (124).

[049] In several respects, the evaporation section (132) includes an evaporation system of one or more evaporators (130). In some respects, one or more evaporators (130) may be configured for multi-effect evaporation. For example, the vapors generated from a first-effect evaporator (130a) may be used to drive a second-effect evaporator (130b). In some respects, the vapors generated from the second-effect evaporator (130b) may be used to drive a third-effect evaporator (130c). In several respects, the number of evaporation stages varies from two to eight (e.g., including in a cascade arrangement a fourth-effect evaporator (130d), a fifth-effect evaporator (130e), etc.). As the number of evaporation effects increases, the energy required to drive the evaporation (e.g., to drive the first-effect evaporator) decreases.One advantage of the evaporators (130) being configured for multiple-effect evaporation is that it reduces the amount of rectifier overhead current that needs to be condensed to drive the energy demands of the evaporation system. For example, in one example, only a quantity of the rectifier overhead current needed to drive the first effect evaporator (130a) of the evaporation system is compressed and directed to the first effect evaporator (130a), thus enabling energy cascading in the multiple-effect evaporator configuration.

[050] In several respects, the vapors from the evaporators (130) can be used to power the distillation system. In one example, Petition 870260078936, dated 06 / 08 / 2026, page 28 / 84 19 / 52 the fourth-effect vapors from a fourth-effect evaporator (130d) can be used to power the first distillation column (102a).

[051] In at least some respects, the decrease in energy required to drive evaporation helps to enable the compressed rectifier overhead stream generated by the vapor recompression unit (120a) to drive evaporation. In some cases, without one or more evaporators (130) being configured for multiple-effect evaporation, the energy demand to drive the evaporation section (132) may require large, possibly impractical vapor recompression systems in order to generate a sufficient compressed rectifier overhead stream to drive one or more evaporators (130).

[052] In some respects, the supplied system may include the second distillation column (102b). In these respects, the second distillation column (102b) may help to enable the supplied system to break the codependency between evaporation and feed extraction. This, in turn, may help to enable optimization / reconfiguration of the evaporators (130) to produce multi-effect evaporation (e.g., third or fourth effect evaporation), although multi-effect evaporation may be achieved through system configurations including only the first distillation column (102a) as well, such as by adding a reboiler (106) to drive the first distillation column (102a).

[053] In the evaporation section (132), the bottom stream from the first distillation column (102a) and / or the bottom stream from the second distillation column (102b) can be subjected to a centrifuge system (134a-b) (generally or collectively, centrifuge system (134)) in which a concentrate of solids (wet cake) and a solution with a low concentration of solids (fine vinasse) are produced. The fine vinasse can then be divided into two streams: countercurrent and evaporator feed. One advantage Petition 870260078936, dated 06 / 08 / 2026, page 29 / 84 20 / 52 of the supplied system is that the countercurrent and evaporator feed rates can be adjusted and the countercurrent recirculation to the plant front can be reduced, which improves plant yield and efficiency. The evaporator feed is fed to the evaporator section (132) to increase its solids concentrations. In some respects, the evaporator feed may receive top vapors from the beer column to drive evaporation in at least one evaporator (130). In at least some respects, retentate vapor from the separation system in the dehydration section may be used to drive the evaporation section (132). In some cases, the top vapor stream from a distillation column (102) (e.g., the top stream from the second distillation column (102b)) may be used to drive evaporation. An advantage of the supplied system is that it eliminates the need for steam to drive the evaporation section (132).

[054] Figure 2 illustrates an alternative embodiment of the exemplary system of Figure 1. Only the differences between the exemplary organic solvent production system of Figure 1 and the organic solvent production system of Figure 2 are described here. In the exemplary system (200) of Figure 2, the retentate vapor generated by the membrane (124) is directed to the evaporation section (e.g., to the second evaporator (130b)). In other examples, the retentate vapor may drive more than one evaporator (130) or may be directed to a different evaporator (130) (e.g., an evaporator different from the second evaporator (130b)) in the evaporation section (132). In at least some respects, the retentate vapor is directed to a different evaporator (130) from the compressed rectifier overhead stream.For example, in the illustrated example, with the retentate vapor driving the second evaporator (130b), the compressed rectifying overhead stream can now be directed entirely to the first one. Petition 870260078936, dated 06 / 08 / 2026, page 30 / 84 21 / 52 evaporator (130a), instead of being directed to both the first evaporator (130a) and the second evaporator (130b), as in Figure 1. In other words, less compressed rectifier overhead stream is directed to the evaporation section (132), given that the retentate vapor is directed to the evaporation section (132). With less compressed rectifier overhead stream being used to drive evaporation, a larger portion of the rectifier overhead stream can be condensed through the condenser (140) instead of being compressed. An advantage of less compressed rectifier overhead stream being used to drive evaporation is that the vapor recompression unit (120) can be smaller and require less energy.

[055] Figure 3 illustrates an alternative embodiment of the exemplary system of Figure 1. Only the differences between the example organic solvent production system of Figures 1 to 2 and the organic solvent production system (300) of Figure 3 are described here. In the exemplary system (300) of Figure 3, the dehydration section may include (1) a vaporizer (118) and a molecular sieve bed array (e.g., an MSU (128)) and (2) an extraction column (122) and a membrane (124). A portion of the condensed rectifier top stream may be directed to the vaporizer (118). The vaporizer (118) generates a vaporized stream that is directed to the MSU (128). The molecular sieve bed array of the MSU (128) is configured to generate a product stream and two regenerated streams from the vaporized stream. The two regenerated currents are a regeneration current (MSU Regen) and a depression current.The product stream is a stream rich in organic solvent (e.g., 200 proof).

[056] The MSU (128) may include two or three beds filled with zeolite pellets, which adsorb water to produce anhydrous vapor until the zeolite pellets are saturated with water. A bed of zeolite pellets Petition 870260078936, dated 06 / 08 / 2026, page 31 / 84 22 / 52 saturated can be regenerated. In some cases, the newly dehydrated organic solvent can be directed to contact a saturated zeolite pellet bed to remove water from the saturated zeolite pellet bed, which produces a regenerated stream. In other cases, regeneration is done by vacuum generating two regeneration streams, the regeneration stream and the depression stream. The MSU regeneration stream can have an organic solvent concentration between 50-80% by volume and is therefore recycled to upstream distillation for reprocessing. For example, the regeneration stream can be directed to the extraction column (122) of the separation system. The low-pressure stream can have a concentration above 80% by volume of organic solvent and can also be recycled to upstream distillation for reprocessing.For example, the pressure reduction stream can be directed to the rectifier column (108) and / or to the storage tank (116a), storing a portion of the rectifier heads. In cases where the MSU (128) includes multiple zeolite pellet beds, a saturated zeolite pellet bed can be regenerated while an unsaturated zeolite pellet bed is used to dehydrate a vaporized feed stream. In at least some respects, the product stream from the MSU (128) can be condensed (e.g., through one or more evaporators (130)) and directed to a tank (116b) for storage.

[057] A portion of the condensed rectifier overhead stream (e.g., (190P)) can be directed (e.g., through a storage tank (116a)) to the extraction column (122) which generates a vaporized stream that is directed to come into contact with the membrane (124), as described in relation to Figure 1.

[058] Figure 4 illustrates an alternative embodiment of the exemplary system in Figure 1. Only the differences between the example of Petition 870260078936, dated 06 / 08 / 2026, page 32 / 84 23 / 52 The organic solvent production system of Figures 1 to 3 and the organic solvent production system (400) of Figure 4 are described herein. In the exemplary system (400) of Figure 4, the separation system may include a vaporizer (118) and a membrane (124). A portion of the rectifying top stream may be directed to the vaporizer (118). In some respects, at least a portion of the top stream from the second distillation column may be directed to the vaporizer (118). The vaporizer (118) thus generates a vaporized stream that is directed to come into contact with the membrane (124).

[059] Figure 5 illustrates an alternative embodiment of the exemplary system of Figure 1. Only the differences between the example organic solvent production system of Figures 1 to 4 and the organic solvent production system (500) of Figure 5 are described here. In the exemplary system (500) of Figure 5, the separation system may include an extraction column (122) and an MSU (128). A portion of the rectifying top stream may be directed to the extraction column (122). In some respects, at least a portion of the top stream from the second distillation column may be directed to the extraction column (122). The extraction column (122) thus generates a vaporized top stream that is directed to contact the MSU (128). The regeneration stream from the MSU (128) may be directed to the rectifying column (108).

[060] Figure 6 illustrates an alternative embodiment of the exemplary system of Figure 1. Only the differences between the example organic solvent production system (100) of Figure 1 and the example organic solvent production system (600) of Figure 6 are described here. In the exemplary system (600) of Figure 6, the vapor recompression unit includes a vapor condensate vessel (136) which includes a vapor-side heat exchanger (114i) in fluid communication with the rectifier column. Petition 870260078936, dated 06 / 08 / 2026, page 33 / 84 24 / 52 (108) and a supplementary heat exchanger (114i) in fluid communication with the membrane (124) to extract usable heat from the 190P steam and the retentate steam, respectively.

[061] In several respects, a steam compressor (120a) is disposed in the fluid path between the rectifier column (108) and the steam condensate vessel (136), which pressurizes the steam 190P to improve the efficiency at which usable thermal energy can be passed to the steam condensate vessel (136) via the steam-side heat exchanger (114h). In some respects, the steam compressor (120) is a mechanical vapor recompression (MVR) compressor, although other types of compressors are contemplated, such as, but not limited to, thermal vapor recompression (TVR) compressors that use high-pressure steam as motive steam to compress the steam 190P. For example, higher-pressure steam may be used. The motive steam may be used in an evaporator (130) to effect a higher pressure therein.

[062] In several respects, the pressure differential transmitted to the 190P steam by the steam compressor (120) in Figure 6 to improve heat transfer is less than the pressure differential transmitted by the condenser (140) in Figure 1 to produce the return reflux stream. Since 190P steam is combustible, using a lower compression ratio (and lower final pressure) can improve the overall safety of the system (as well as reduce the cost and complexity of compressors to install, operate and maintain), but the lower pressure in the resulting compressed steam can affect how quickly thermal energy can be transferred to various system modules. Therefore, the steam condensate vessel (136) provides an intermediate heat exchange with a non-combustible (or less combustible) working fluid that can extract thermal energy from low-pressure steam and provide higher-pressure steam to other systems for Petition 870260078936, dated 06 / 08 / 2026, page 34 / 84 25 / 52 transfer thermal energy to them. In some embodiments, compared to Figure 1, when the 190P steam is passed to the steam condensate vessel (136) to extract usable thermal energy, the waste heat exchanger (114h) in the return reflux stream may be omitted or regulated (e.g., through a valve assembly) to affect the amount of 190P steam that has heat released to the environment instead of (or in addition to) exchanging heat with the working fluid in the steam condensate vessel (136).

[063] Heat exchangers (114) in fluid communication with the steam condensate vessel (136) (e.g., a shell and tube heat exchanger, evaporator, etc.) receive a heated fluid or steam from various system modules (e.g., 190P steam from the rectifier column (108), retentate steam from the membrane modules (124), overheads from the distillation columns (102), permeate streams, etc.) and transfer the thermal energy to a working fluid (e.g., water) and return the cooled / condensed fluid or steam to an appropriate module (e.g., via a reflux stream to the rectifier column (108), a retentate stream to a 200P tank (116b)). Although generally described as a steam condensate vessel (136) using water as the working fluid, in several respects the condensate vessel (136) may utilize various other working fluids.In several respects, the steam condensate vessel (136) includes additional heaters that are in fluid communication with the condensate vessel (136) (e.g., evaporators, shell and tube heat exchangers, plate heat exchangers, etc.) that can transmit additional thermal energy to the working fluid to supplement the thermal energy available through the heat exchangers (114).

[064] The steam condensate container (136) produces, through the supplied thermal energy, a low-pressure steam that a first Petition 870260078936, dated 06 / 08 / 2026, page 35 / 84 26 / 52 steam compressor (120b) then compresses into a medium pressure steam to transfer heat to other modules in the system (e.g., fluid paste tanks, distillation columns (102), evaporators (130), side extraction columns (110), extraction columns (122), cooking water heaters, superheaters, vaporizers (118), hydroheaters, dryers, etc.). As illustrated in Figure 6, the first steam compressor (120b) supplies medium pressure steam to the evaporators (130) to transfer thermal energy to them. However, some modules in the system (600) may operate more effectively at higher pressures (e.g., to receive a greater percentage of the thermal energy available in the working fluid) than the medium pressure steam produced by the first steam compressor (120b).Therefore, the output feed from the first steam compressor (120b) can be supplied directly to various system modules (e.g., the evaporators (130)) and indirectly supplied to other modules via a second steam compressor (120c). The second steam compressor (120c) can supply higher pressure steam than initially supplied by the first steam compressor (120b) to one or more system modules, such as the extraction column (122) illustrated in Figure 6. For example, low pressure can include any pressure range below 15 pounds per square inch absolute (psia), and high pressure can include any pressure range above 85 psia, while medium pressure includes any pressure range between the low and high pressure ranges. In several respects, the steam compressors (120b-c) can be MVR or TVR compressors.

[065] As illustrated in Figure 6, the second steam compressor (120b) supplies high-pressure steam to the extraction column (122) via a heat exchanger used in a reboiler (106c), and the cooled steam then returns to the steam condensate vessel (136) as a condensate of Petition 870260078936, dated 06 / 08 / 2026, page 36 / 84 27 / 52 steam. Although generally described as an extraction column (122) receiving high-pressure steam, in several respects, high-pressure steam may be supplied to other modules (e.g., fluid paste tanks, distillation columns (102), evaporators (130), side extraction columns (110), cooking water heaters, superheaters, vaporizers (118), hydroheaters, dryers, etc.) in addition to or instead of the extraction column (122). Similarly, although generally described as supplying two different steam pressures to two different modules of the system, the steam recompression unit (120) may supply several different steam pressures to several different numbers of modules in several respects.

[066] Figure 7 illustrates an alternative embodiment of the exemplary system of Figure 6. Only the differences between the example organic solvent production system (600) of Figure 6 and the example organic solvent production system (700) of Figure 7 are described here. In the exemplary system (700) of Figure 7, low-pressure steam from the condensate vessel (136) is supplied to a medium-pressure steam compressor (120b) to generate medium-pressure steam that is supplied to one or more of the evaporators (130) of the evaporation section (132). However, the system (700) of Figure 7 omits the feed lines and the high-pressure compressor (120c) that compresses and directs the medium-pressure steam to the extraction column (122) or to the extraction reboiler (106c).

[067] Figure 8 illustrates an alternative embodiment of the exemplary system (600) of Figure 6. Only the differences between the example organic solvent production system (600) of Figure 6 and the example organic solvent production system (800) of Figure 8 are described here. In the exemplary system (800) of Figure 8, medium pressure vapor is directed from the medium pressure compressor (120b) to four of the evaporators (130), while in the exemplary system of Figure 6, the vapor Petition 870260078936, dated 06 / 08 / 2026, page 37 / 84 Medium pressure 28 / 52 is directed from the medium pressure compressor (120b) to two of the evaporators (130), which can be configured to add one or more effects or evaporators (130). Consequently, the first distillation column (102a) is driven by the fourth effect steam and the second distillation column (102b) is driven by the third effect steam, both via direct steam injection. Additionally or alternatively, the distillation columns (102) in this configuration could also be driven by the respective reboiler (106), where the heating medium is evaporator steam, cooking steam, process steam or other suitable hot source.Furthermore, the permeate is described in Figure 6 as being condensed and directed to the extraction column (122), while in Figure 8, the permeate is directed to the rectifier column (108) (or to the distillation columns (102)) in vapor form without the need for prior condensation. In some respects, additionally or alternatively, the permeate can also be condensed in a heat exchanger (114) against a cold stream and sent to the rectifier column (108), to the side extraction column (110) or to the extraction column (122).In addition to the change in permeate routing, the exemplary system (800) of Figure 8 does not include a side extraction column (110), the second distillation column (102b) does not include a reboiler (106) (instead, it uses direct steam injection), although the second distillation column (102b) in this configuration can also be driven by a reboiler (106) where the heating medium can be one or more of the following: steam from the evaporators (130), cooking steam, process steam, or another hot source. In some respects, the operator can turn off a hydroheater in the system (800) and thus not generate instant cooking steam for use when other hot sources are available.

[068] Figure 9 illustrates an alternative embodiment of Petition 870260078936, dated 06 / 08 / 2026, page 38 / 84 29 / 52 exemplary system (600) of Figure 6. Only the differences between the example organic solvent production system (600) of Figure 6 and the example organic solvent production system (900) of Figure 9 are described here. In the exemplary system (900) of Figure 9, medium pressure vapor is directed from the medium pressure compressor (120b) to one of the evaporators (130), while in the exemplary system of Figure 6, medium pressure vapor is directed from the medium pressure compressor (120b) to both evaporators (130). Furthermore, the permeate is described in Figure 6 as being condensed and directed to the extraction column (122), while in Figure 8, the permeate is directed to the rectification column (108) as a vapor (or to the distillation columns (102)).In some respects, additionally or alternatively, the permeate may also be condensed in a heat exchanger (114) against a cold stream and sent to a rectifier column (108), side extraction column (110) or extraction column (122).

[069] An operator can direct or redirect steam from the steam condensate container (136) to various downstream systems by opening or closing various ducts or pipes via valves or by installing / uninstalling different pipes and ducts.

[070] Figure 10 illustrates an alternative embodiment of the exemplary system (600) of Figure 6. Only the differences between the example organic solvent production system (600) of Figure 6 and the example organic solvent production system (1000) of Figure 10 are described here. Figure 10 illustrates that the vapor condensate vessel (136) can receive 200P vapor from the extraction column (122) and an MSU (128) that receives its feed from an extraction column (122) or rectification column (108) as a potential source of thermal energy in addition to or instead of the retentate vapor from the membranes (124) in the exemplary system (600) of Figure 6.

[071] Figure 11 illustrates an alternative embodiment of Petition 870260078936, dated 06 / 08 / 2026, page 39 / 84 30 / 52 exemplary system (600) of Figure 6. Only the differences between the example organic solvent production system (600) of Figure 6 and the example organic solvent production system (1100) of Figure 11 are described here. Figure 11 illustrates a portion of the compression vapor (e.g., ethanol 190P in an ethanol production plant) being directed to the vapor condensate vessel (136) for heat recovery. Furthermore, the 200P vapor can be directed directly from the MSU (128) to one or more of the evaporators (130) as a heat source for the same, instead of supplementing the thermal energy supplied by the compressed 190P vapor to the vapor condensate vessel (136).

[072] Figure 12 illustrates an organic solvent production system (1200) including a heat recovery system, according to one aspect of the present invention. The organic solvent production system (1200) includes a first distillation column (102a) and a second distillation column (102b) that receive a shared feed, which may be preheated by a heater (114e). The evaporator section (132) also provides inputs to the first distillation column (102a) (e.g., fourth-effect vapors) and second distillation column (102b) (e.g., third-effect vapors), and the distillation columns (102) in turn provide bottom streams to a centrifuge (134a) and splitter (134) that feed back to the evaporator section (132).

[073] The second distillation column (102b) provides an upper flow that is also directed to the evaporator section (132), which in an ethanol production plant may be a 120P ethanol mixture, which may be stored in a third storage tank (116c) before being heated (e.g., through the first effect vapors from the evaporator section (132) in a second heat exchanger (114b)) as used as a wash or supplementary inlet for the second distillation column. Petition 870260078936, dated 06 / 08 / 2026, page 40 / 84 31 / 52 (102b) or extraction column (122).

[074] The first distillation column (102a) provides an upper stream to a rectifier column (108), which further refines the organic solvent in the upper stream, producing a rectifier upper stream that is directed to a vapor recompression unit (120a). The vapor recompression unit compresses the rectifier upper stream and feeds the compressed vapor stream to an eighth heat exchanger (114h) to a vapor condensate vessel (136) to heat a working fluid in the vapor condensate vessel (136) to produce a low-pressure vapor.Low-pressure steam is directed to a first steam compressor (120b) to produce medium-pressure steam which can be directed to one or more of a fluid slurry tank (116d), a second steam compressor (120c) or the evaporator section (132) (e.g., to drive evaporation in the same or any other low-pressure steam consumer in the plant, such as a slurry tank, cooking system, etc.). The second steam compressor (120c), in turn, produces high-pressure steam from the medium-pressure steam, which can be used in the fourth heat exchanger (114d) to preheat the inlet to the membrane (124) and in the third reboiler (160c) to drive the extraction column (122) or any other high-pressure steam consumer in the plant (e.g., an MSU evaporator, superheater, etc.).

[075] The compressed steam, after heat exchange with the working fluid in the steam condensate vessel (136), can return to the rectifier column (108) via a reflux line or be directed to a first storage tank (116a). The first storage tank (116a) can store 190P ethanol when used in an ethanol production plant, which is supplied via an economizer (126) to a separation system. In Figure 12, the separation system includes a Petition 870260078936, dated 06 / 08 / 2026, page 41 / 84 32 / 52 extraction column (122), a heat exchanger (114d) and a membrane (124). The membrane (124) receives the heated top stream from the extraction column (122) and produces a permeate stream that is directed back to the rectifier column (108) (or the distillation columns (102)) for use as supplementary feed, and a retentate vapor stream that is directed to the evaporator section (132) for heat recovery, thus producing a retentate liquid, which is supplied to a vaporization vessel (104d).

[076] The rectifier column (108) also produces a bottom stream, which is directed to a first heat exchanger (114a) that uses heat supplied from refined organic solvent (e.g., 200P ethanol) from the vaporization vessel (104d) to heat the bottom vapor before delivering the bottom vapor as an inlet to the extraction column (122). The refined organic solvent stream, after the heat is extracted by the first heat exchanger (114a), is then directed to the economizer (126), before being directed to the third heat exchanger (114c) for further cooling before being stored in the second storage tank (116b). In addition, other outputs from the vaporization vessel (104d) can be fed back to the evaporator section (132) (e.g., desuperheated 200P ethanol along with the retentate vapor stream) or to the rectifier top stream for acidity control.

[077] Figure 13 illustrates an organic solvent production system including a heat recovery system, according to one aspect of the present invention. The organic solvent production system (1300) includes a first distillation column (102a) and a second distillation column (102b) that receive a shared feed, which can be preheated by a heater (114e). The evaporator section (132) also provides inlets for the first distillation column (102a) (e.g., Petition 870260078936, dated 06 / 08 / 2026, page 42 / 84 33 / 52 fourth effect vapors) and second distillation column (102b) (e.g., third effect vapors), and the distillation columns (102) in turn provide bottom streams to a centrifuge (134a) and splitter (134) that feed back to the evaporator section (132).

[078] The second distillation column (102b) provides an upper stream that is also directed to the evaporator section (132).

[079] The first distillation column (102a) provides an upper stream to a vapor recompression unit (120a). The vapor recompression unit (120a) compresses the upper stream and feeds the compressed vapor stream to an eighth heat exchanger to a vapor condensate vessel (136) to heat a working fluid in the vapor condensate vessel (136) to produce a low-pressure vapor. The low-pressure vapor is directed to a first vapor compressor (120b) to produce a medium-pressure vapor which may be directed to one or more of a fluid paste tank (116d), a second vapor compressor (120c), a cooking system or the evaporator section (132) (e.g. to conduct evaporation therein).The second steam compressor (120c), in turn, produces high-pressure steam from medium-pressure steam, which can be used in the fourth heat exchanger (114d) to preheat the inlet to the membrane (124) and in the third reboiler (160c) to drive the extraction column (122) or any other high-pressure steam user in the plant (e.g., MSU steamer (118), superheater, etc.).

[080] The compressed steam, after heat exchange with the working fluid in the steam condensate vessel (136) via the eighth heat exchanger (114h) may be directed to a third storage tank (116c) together with at least a portion of the evaporator section outlet (132). The third storage tank (116c) the tank (116c) Petition 870260078936, dated 06 / 08 / 2026, page 43 / 84 34 / 52 can store 120P ethanol when used in an ethanol production plant, which is fed to the second distillation column (102b) for washing (e.g., to ensure ducts / pipes are free of accumulated solids) or to the separation system for further refining. In Figure 13, the separation system includes an extraction column (122), a heat exchanger (114d), and a membrane (124). The membrane (124) receives the heated top stream from the extraction column (122) and produces a permeate stream that is directed back to the first distillation column (102a) to use for heat recovery and a retentate vapor stream that is directed to the evaporator section (132) to produce a retentate liquid, which is fed to a vaporization vessel (104d) for acidity control.

[081] The vaporization vessel (104) produces the refined organic solvent (e.g., ethanol 200P) from the liquid retentate stream. The refined organic solvent stream is then directed to the economizer (126), before being directed to the third heat exchanger (114c) for further cooling before being stored in the second storage tank (116b) or returned to the evaporator section (132) for desuperheating. In addition, other outlets from the vaporization vessel (104d) can be directed to the vapor recompression unit (120a) with the upper stream from the first distillation column (102a).

[082] Figure 14 illustrates an organic solvent production system including a heat recovery system, according to one aspect of the present invention. The organic solvent production system (1400) includes a first distillation column (102a) and a second distillation column (102b) that receive a shared feed, which can be preheated by a heater (114e). The evaporator section (132) also provides inlets for the first distillation column (102a) (e.g., Petition 870260078936, dated 06 / 08 / 2026, page 44 / 84 35 / 52 fourth effect vapors) and second distillation column (102b) (e.g., third effect vapors), and the distillation columns (102) in turn provide bottom streams to a centrifuge (134a) and splitter (134) that feed back to the evaporator section (132).

[083] The second distillation column (102b) provides an upper stream that is also directed to the evaporator section (132) (e.g., to a fourth effect evaporator (130d)), which in an ethanol production plant may be a 120P ethanol blend.

[084] The first distillation column (102a) provides an upper stream to a rectifier column (108), which further refines the organic solvent in the upper stream, producing a rectifier upper stream that is directed to a vapor recompression unit (120a). The vapor recompression unit (120a) compresses the rectifier upper stream and feeds the compressed vapor stream to an eighth heat exchanger to a vapor condensate vessel to heat a working fluid in the vapor condensate vessel to produce a low-pressure vapor.Low-pressure steam is directed to a first steam compressor (120b) to produce medium-pressure steam which may be directed to one or more of a fluid paste tank (116d), a second steam compressor (120c), a cooking section of the organic solvent plant or the evaporator section (132) (e.g., to a first-effect evaporator (130a) to conduct evaporation therein and any other low-pressure steam user in the plant). The second steam compressor (120c), in turn, produces high-pressure steam from the medium-pressure steam, which may be used in the fourth heat exchanger (114d) to preheat the inlet to the membrane (124), the seventh heat exchanger (114f) to vaporize the inlet to the MSU (128), and the third reboiler (160c) to drive the extraction column (122) and any other users thereof. Petition 870260078936, dated 06 / 08 / 2026, page 45 / 84 36 / 52 high-pressure steam in the plant.

[085] The compressed steam, after exchanging heat with the working fluid in the steam condensate vessel (136) via the eighth heat exchanger (114h), can return to the rectifier column (108) via a reflux line or be directed to a first storage tank (116a). The first storage tank (116a) can store 190P ethanol when used in an ethanol production plant, which is supplied via an economizer (126) to a separation system. In Figure 14, the separation system includes an extraction column (122), heat exchangers (114d), a vaporizer (114f), a membrane (124), and an MSU (128).The membrane (124) receives the heated upper stream from the extraction column (122) and produces a permeate stream that is directed back to the rectifier column (108) for use as a heat source, and a retentate vapor stream that is directed to the evaporator section (132) to produce a retentate liquid, which is supplied to a vaporization vessel (104d). In addition, the MSU (128) vapor feed mixture from the vaporizer (114f) (which is downstream of the economizer (126)) produces a regeneration stream that is directed to a fifth storage tank (116e), an enriched organic solvent stream (e.g., 200P ethanol vapor in an ethanol production plant) that is directed to the evaporator section (132), and a depression stream that is directed through a first preheater (142a) (generally or collectively, reheater) that may be loaded through cooking water from the cooking section.

[086] The fifth storage tank (116e) may be a feed tank for the separation section, which is fed from the MSU and a fourth storage tank (116d) which is fed from the evaporator section (132) (e.g., from the outlet of a fourth effect evaporator (130d), which in an ethanol production plant may Petition 870260078936, dated 06 / 08 / 2026, page 46 / 84 37 / 52 supply ethanol 120P). The outlet of the fifth storage tank (116e) is supplied to the extraction column (122) as an inlet after being heated through one of two, a second preheater (142b) and a third preheater (142c). The second preheater (142b) uses, as a heat source, the enriched organic solvent from the vaporization vessel (140d) (e.g., vaporization vapor of ethanol 200P in an ethanol production plant) as the enriched organic solvent is directed to the second storage tank (116b). The third preheater (142c) uses, as a heat source, the vapors from the evaporator section of the evaporator, which are then directed to the front end of the organic solvent production plant.

[087] The rectifier column (108) also produces a bottom stream, which is directed to the side extraction column (110) as an inlet. The side extraction column (110) produces an upper stream, which returns to the rectifier column (108) as an inlet, and produces a bottom stream, which can be directed to the cooking water. In several respects, the side extraction column (110) is also provided with evaporator vapors from the evaporator section (132) or cooking vaporization as inlets.

[088] Figure 15 illustrates a heat recovery system (1500), according to one aspect of the present invention. In several respects, the heat recovery system discussed in Figure 15 forms part of the vapor recompression unit of the system discussed in relation to Figures 6-11. As illustrated in Figure 15, a reaction vessel (1502) (e.g., a rectifier column (108)) is shown, which produces a volatile combustible vapor or concentrates the vapor to (but not to) the azeotropic point (e.g., an upper stream from the rectifier / extraction column of ethanol, butanol, isobutanol, methanol, acetone, ammonia, etc., or other organic solvent) that Petition 870260078936, dated 06 / 08 / 2026, page 47 / 84 38 / 52 transports thermal energy from the refining process. Although this thermal energy can be absorbed by the environment (for example, through an optional reflux condenser (140) and heat sink) to return the volatile vapor to the rectifier as a cooler liquid or vapor, this thermal energy can additionally or alternatively be extracted for use in other processes in a system or plant that includes the described heat recovery system.

[089] In several respects, a steam compressor (1504) receives (on the low pressure side) heated volatile steam from the reaction vessel (1502) and produces compressed steam (on the high pressure side) for heat exchange with a working fluid in a steam condensate vessel (136). However, compressing this volatile steam to improve the extraction of usable thermal energy may present additional safety considerations, which increase as the volatile steam is compressed to higher pressures. Consequently, the compression ratio used by the steam compressor (1504) may be kept low for safety reasons.For example, when refining ethanol, the steam compressor (1504) may receive 190P steam from a reaction vessel (1502) or a rectifier column (108) at a first pressure range and produce a high-pressure steam (at a higher pressure than that received from the reaction vessel (1502)) which is passed to a heat exchanger (114h) in the steam condensate vessel (136). In several respects, the steam compressor (1504) is controlled to produce the compressed high-pressure volatile steam at a more consistent pressure than the steam exiting the reaction vessel (1502), but at a lower pressure than that produced by the compressors (1506a-b) in fluid communication with the steam condensate vessel (136). In several respects, one or more additional systems or others may also pass heated vapors (volatile or non-volatile) to other heat exchangers (114i) in the steam condensate vessel (136). Once the steam exchanges. Petition 870260078936, dated 06 / 08 / 2026, page 48 / 84 39 / 52 thermal energy with the working fluid, the cooled volatile vapor (or liquid) is directed to return to the reaction vessel (1502) (or other system that uses volatile vapor as input or output).

[090] Using the heat provided by the supplied volatile steam (e.g., through the heat exchangers (114h-i)), the working fluid in the steam condensate vessel (136) is heated until it forms steam at a first pressure range. Although the examples given here generally refer to the working fluid as water and the resulting steam as vapor, the working fluid may include various other fluids that produce non-volatile vapors or vapors that are less volatile than the volatile steam used to heat the working fluid.

[091] The steam produced at the first pressure by the steam compressor (1504) may be referred to as low-pressure (LP) steam, because the heat recovery system (1500) includes additional steam compressors (1506a-b) (generally or collectively, steam compressors (1506)) that produce various higher-pressure steams for use by other systems to receive the thermal energy carried by the steam (e.g., receiving systems (1508a-b) (generally or collectively, receiving system (1508))). For example, the steam condensate vessel (136) may supply a first steam compressor (1506a) (on the low-pressure side) with LP steam and the first steam compressor (1506a) emits (on the high-pressure side) medium-pressure (MP) steam.This MP steam can be supplied to one or more MP receiving systems (1508a) (e.g., evaporators (130), fluid paste tanks, distillation columns (102), side extraction columns (110), extraction columns (122), cooking water heaters, superheaters, vaporizers (118), hydroheaters, dryers, etc.) which can use the MP steam as a heat source through the corresponding heat exchangers (114). In addition, the first steam compressor (1506a). Petition 870260078936, dated 06 / 08 / 2026, page 49 / 84 40 / 52 provides a second steam compressor (1506b) (on a low pressure side) with MP steam, and the second steam compressor (1506b) emits (on the high pressure side) a high pressure (HP) steam having a higher pressure than MP steam, which can be supplied to one or more HP receiving systems (1508b) (e.g., extraction columns (122)) that can use the HP steam as a heat source through corresponding heat exchangers (114).

[092] Once the higher pressure vapors (e.g., MP and HP vapors) transfer thermal energy to their respective receiving systems (1508), the cooled vapor is returned to the steam condensate vessel (136) as a steam condensate (1510) to recirculate and pass additional thermal energy from the circulating steam outlet through the reaction vessel (1502). In several respects, the steam compressors (1506) may be MVR compressors or TVR compressors. For example, the HP steam outlet from the high-pressure steam compressor (1506b) may be used as motive steam in the medium-pressure steam compressor (1506a) to compress the LP vapor received from the steam condensate vessel (136) into MP vapor to supply the receiving systems (1508) (and / or the high-pressure steam compressor (1506b)).

[093] Although illustrated with a two-stage compressor serving two receiving systems (1508), the heat recovery system (1500) of Figure 15 can be used with more or fewer steam compressors (1506) serving more or fewer receiving systems (1508). Furthermore, although illustrated with a reaction vessel (1502), in several respects the heat recovery system (1500) of Figure 15 can receive volatile steam input from multiple reaction vessels (1502). Although not illustrated in Figure 12, the receiving systems (1508) can accept additional inputs (e.g., a precipitate from a rectifier, liquid 190P) that the energy Petition 870260078936, dated 06 / 08 / 2026, page 50 / 84 41 / 52 recovered thermal energy can be used for preheating, and receiving systems can produce various outputs (e.g., nth effect vapors, syrup) that are not illustrated in Figure 12.

[094] By passing volatile vapor from an outlet rectifier through a steam compressor connected to a vapor condensate receptacle, an operator can use a lower compression ratio when converting the volatile vapor into a cooled liquid or vapor to return to the rectifier than by using an ambient heat sink and reflux compressor. Consequently, the operator can utilize a simpler compressor in a safer operating range (e.g., reducing the risk of fire or explosion) by employing the heat recovery system presently described.The heat transfer medium (e.g., the working fluid) can therefore have a different material composition from the volatile steam output of the rectifier (e.g., a mixture of alcohol versus water) with different material properties, including lower volatility, which improves the safety of the heat recovery system, reduces operating costs, simplifies ducting or piping between modules, among other benefits. Furthermore, by using multiphase compression of the steam produced from the working fluid, the operator can transfer heat at different rates to the various receiving systems using a single steam condensate vessel through at least two different pressures.By using a lower compression ratio (and a lower ultimate pressure) to compress volatile vapor, an operator can improve the overall safety of the system (as well as reduce the cost and complexity of compressors to install, operate, and maintain) compared to using systems with higher compression ratios. Furthermore, using steam as a hot medium source instead of 190P steam is practical, as steam is already commonly used as a typical utility by factories and equipment designed to allow its use. Petition 870260078936, dated 06 / 08 / 2026, page 51 / 84 42 / 52 steam without the need for any special material equipment (e.g., corrosion-resistant material) required to handle 190P steam. Furthermore, the use of steam allows the plant the flexibility to produce different steam qualities for different applications simply by adding or removing compression stages.

[095] Figure 16 is a flowchart of an exemplary method (1600) for operating an organic solvent production plant via an integrated heat process using vapor recompression, according to an aspect of the present invention. Although various inputs and outputs of the plant subsystems are described as being directed, sent, or otherwise actuated in the method (1600), the present invention contemplates that some or all of the basic components may be partitioned, divided, or redirected into multiple sub-elements. Therefore, the discussion of an element inherently contemplates that all or a subpart of the element is actuated as discussed in this document, where a remainder of the element may be actuated differently by the plant.For example, the plant can direct a raw material to a distillation column, which describes scenarios where 100% of the raw material (in a given period of time) is directed to the distillation column and where 100-X% of the raw material (in a given period of time) is directed to the distillation column and X% (e.g., the remainder) is directed to a second distillation column.

[096] Furthermore, although presented with several operations in distinct blocks, the present invention intends that this method (1600) can be understood as a continuous process that an operator can adjust to meet production demands. Consequently, it will be understood that the blocks (1610-1670) can be executed substantially simultaneously or in different orders from those shown in the flowchart of Petition 870260078936, dated 06 / 08 / 2026, page 52 / 84 43 / 52 Figure 16 shows some operations being (at least temporarily) omitted or executed at different rates than other operations.

[097] In block (1610), the plant generates an organic solvent topstream distillation in a distillation system. In various aspects, the plant generates an organic solvent from a feedstock supplied to one or more distillation columns. In various aspects, the distillation system includes at least one of a rectifier column, a rectifier column in direct fluid communication with the separation system (via a bottomstream generated by the rectifier column), a rectifier column in direct fluid communication with a side separator (via the bottomstream of the rectifier column), a rectifier / extraction column, and a brewing column.In several respects, the distillation system comprises a first distillation column operating at a first pressure that receives a first portion of a feed mixture comprising an organic solvent, water, and solids operating in fluid communication with a second distillation column that receives a second portion of the feed mixture and operates at a second pressure different from the first distillation column. In several respects, the distillation system is a rectification system that receives a first vaporous upper stream from a first distillation column as an input, wherein a second distillation column produces a second vaporous upper stream from a feed mixture shared with the first distillation column that is directed to the separation system without passing through the distillation system.In several respects, the generation of the upper distillation stream includes the production of a first and a second vaporous upper stream in the respective first and second distillation columns using a shared feed mixture, where the second vaporous upper stream is directed to different plant subsystems than the first stream. Petition 870260078936, dated 06 / 08 / 2026, page 53 / 84 44 / 52 vaporous upper vapor, such as a plurality of multi-effect evaporators that condense the second upper vaporous stream into a second condensate stream, which can be directed to the separation system.

[098] In block (1620), the plant directs the upper distillation stream to a compression system to produce a compressed vapor from the upper distillation stream. In several respects, the compression system is a vapor recompression unit, comprising either a mechanical vapor recompression (MVR) compressor or a thermal vapor recompression (TVR) compressor.

[099] In block (1630), the plan sends the compressed steam to an energy recovery system that generates steam at a first pressure, using the heat from the compressed steam stream to (at least partially) heat a steam condensate into a low-pressure steam. In several respects, hot sources from other plant subsystems may also be used to heat the steam condensate, and other heaters may also be used.

[0100] Additionally or as an alternative to sending compressed steam to the energy recovery system, the plant can direct several steam or liquid streams against each other through heat exchangers to increase the temperature of a cold stream (for example, recapturing energy from a warmer stream) or to lower the temperature of a hot stream to adjust the temperature of the various inputs and outputs of the plant subsystem using existing temperature differentials in the material handled by the plant.

[0101] In block (1640), the plant sends the compressed vapor to a condensation system that produces a condensate stream of the organic solvent. In several respects, the condensate stream is one of 120P ethanol. Petition 870260078936, dated 06 / 08 / 2026, pages 54 / 84 45 / 52 or 190P, which can be used as feedstock by another plant system for further refining (e.g., into 200P ethanol), as a renewal stream (e.g., to recharge an MSU), or for other purposes in the plant. In various respects, the condensation system is a single evaporator, a plurality of multi-effect evaporators, a heat exchanger, an energy recovery system, or a vapor condensate vessel.

[0102] In block (1650), the plant directs the condensate stream to a separation system to produce an enriched product stream as a separated organic solvent. In many respects, the enriched product stream may be 200P ethanol. The separation system includes at least one of a vaporizer, an extraction column, a membrane, and an MSU, and various combinations thereof, as described in relation to Figures 1-14. In many respects, the portion of the condensate stream sent to the separation system is less than the entire condensate stream, and a remainder of the condensate stream is sent to the distillation system as at least part of a reflux stream for further processing.

[0103] In block (1660), the plant directs the separated organic solvent to storage, such as a storage tank. Portions of the condensate stream separated from the enriched product stream can be discarded, used for heat exchange, returned to an upstream portion of the plant for reprocessing to extract more of the organic solvent and combinations thereof.

[0104] In block (1670), the plant compresses the low-pressure steam generated by the energy recovery system into medium-pressure steam. In many respects, the steam is compressed by a vapor recompression unit, comprising either a mechanical vapor recompression (MVR) compressor or a thermal vapor recompression compressor. Petition 870260078936, dated 06 / 08 / 2026, page 55 / 84 46 / 52 (TVR).

[0105] In block (1680), the plant directs compressed steam to a receiving system that uses the compressed steam at the given pressure as input. In various embodiments, the receiving system includes one or more of a splitter, an evaporator, a plurality of multi-effect evaporators, a heat exchanger, an energy recovery system, and a steam condensate vessel. The steam may be used in an associated heat exchanger or integrated into various reaction vessels to drive various distillation or separation processes in the plant. In some aspects, the plant sends the compressed steam to a condensation system, which produces a condensate stream that is directed to a separation system.

[0106] In block (1690), when the receiving system is a supplementary compression unit (e.g., a second vapor recompression unit), the plant further compresses the compressed vapor (e.g., from medium pressure to high pressure), and method (1600) returns to block (1680) to enable the plant to direct high-pressure vapor from a receiving system that uses that vapor pressure as an input.

[0107] The present invention can also be understood with reference to the following numbered clauses: Clause 1: A distillation and dehydration method comprising: generating an upper distillation stream in a distillation system; directing the upper distillation stream to a compression system, producing a compressed vapor; sending the compressed vapor to a condensation system, producing a condensate stream; and directing the condensate stream to a separation system; Clause 2: The method of either clause 1 and 3-12, wherein the condensate stream is 120P ethanol or 190P ethanol; Petition 870260078936, dated 06 / 08 / 2026, page 56 / 84 47 / 52 Clause 3: The method described in any of clauses 1-2 and 4-12, wherein the compression system is a vapor recompression unit comprising a mechanical vapor recompression compressor (MVR) or a thermal vapor recompression compressor (TVR); Clause 4: The method described in any of clauses 1-3 and 5-12, wherein the condensation system includes at least one of: an evaporator; a plurality of multi-effect evaporators; a heat exchanger; an energy recovery system; and a vapor condensate receptacle; Clause 5: The method of any of clauses 1-4 and 6-12, wherein the distillation system includes at least one of: a rectification column; a rectification column in direct fluid communication with the separation system via a bottom stream generated by the rectification column; a rectification column in direct fluid communication with a side stripper via the bottom stream; a rectification / extraction column; and a brewing column; Clause 6: The method described in any of clauses 1-5 and 7-12, wherein the separation system includes at least one of: a vaporizer; an extraction column; a membrane; and a molecular sieve unit (MSU); Clause 7: The method of any of clauses 1-6 and 8-12, wherein the condensate stream sent to the separation system is less than the entire condensate stream output of the condensation system and a remainder of the condensate stream output is sent to the distillation system as at least part of a reflux stream; Clause 8: The method of any of clauses 1-7 and 9-12, wherein the distillation system comprises a first distillation column operating at a first pressure that receives a first portion of a feed mixture comprising an organic solvent, water and solids. Petition 870260078936, dated 06 / 08 / 2026, page 57 / 84 48 / 52 operating in fluid communication with a second distillation column that receives a second portion of the feed mixture and operates at a second pressure different from the first distillation column; Clause 9: The method of any of clauses 1-8 and 10-12, wherein the distillation system is a rectification system that receives a first vaporous upper stream from a first distillation column as an input, wherein a second distillation column produces a second vaporous upper stream from a feed mixture shared with the first distillation column that is directed to the separation system without passing through the distillation system; Clause 10: The method of any of clauses 1-9 and 11-12, further comprising: producing a second vaporous top stream in a second distillation column using a feed mixture shared with the distillation column; directing the second vaporous top stream to a plurality of multi-effect evaporators; condensing, in the plurality of multi-effect evaporators, the second vaporous top stream into a second condensate stream; and directing the second condensate stream to the separation system; Clause 11: The method of any of clauses 1-10 and 12, further comprising: sending the compressed steam to an energy recovery system that generates steam at a first pressure; compressing the steam from the first pressure to a second pressure, higher than the first pressure; and directing the steam at the second pressure to a receiving system; Clause 12: The method of any of clauses 1-11, further comprising: recovering heat from a hot stream to heat a cold stream while generating an enriched solvent stream through the separation system; Clause 13: A method of distillation and dehydration, Petition 870260078936, dated 06 / 08 / 2026, page 58 / 84 49 / 52 comprising: generating an upper distillation stream in a distillation system; directing the upper distillation stream to a compression system, producing compressed vapor; sending the compressed vapor to an energy recovery system that generates steam at a first pressure; compressing the vapor from the first pressure to a second pressure, higher than the first pressure; and directing the vapor at the second pressure to a receiving system; Clause 14: The method of any of clauses 13 and 15-18, further comprising: sending the compressed steam to a condensation system, producing a condensate stream; and directing a portion of the condensate stream to a separation system; Clause 15: The method of any of clauses 13-14 and 16-18, wherein the receiving system is one of: a splitter; an evaporator; a plurality of multi-effect evaporators; a heat exchanger; an energy recovery system; and a vapor condensate receptacle; Clause 16: The method of any of clauses 13-15 and 17-18, wherein the receiving system is a splitter, further comprising: directing a first portion of the steam at the second pressure of the splitter to a second receiving system; compressing a remainder of the steam not directed to the second receiving system from the second pressure to a third pressure, higher than the second pressure; and directing the steam at the third pressure to a third receiving system; Clause 17: The method described in any of clauses 13-16 and 18, wherein the steam is compressed by a vapor recompression unit comprising a mechanical vapor recompression compressor (MVR) or a thermal vapor recompression compressor (TVR); Clause 18: The method of any of clauses 13-17, wherein the upper distillation stream consists of 120P ethanol or 190P ethanol; Petition 870260078936, dated 06 / 08 / 2026, page 59 / 84 50 / 52 Clause 19: A heat recovery system, comprising: a vapor recompression unit connected on a first low-pressure side to an upper vapor outlet of a distillation unit and connected on a first high-pressure side to a first heat exchanger for a vapor condensate vessel; and a first vapor compressor connected on a second low-pressure side to a vapor outlet of the vapor condensate vessel and connected on a second high-pressure side to a second heat exchanger for a medium-pressure receiving system; Clause 20: The heat recovery system of clauses 19 and 21-26, further comprising: a reflux line connected to a second side of the first heat exchanger of the vapor recompression unit, configured to selectively direct portions of a condensate from the upper vapor outlet to the distillation unit as part of a reflux stream and to a separation system; Clause 21: The heat recovery system of clauses 1920 and 22-26, wherein the medium pressure receiving system is at least one of: an evaporation system including a plurality of evaporators arranged for multiple-effect evaporation; a cooking system; a slurry tank; and a turbine; Clause 22: The heat recovery system of clauses 1921 and 23-26, further comprising: a plurality of evaporators arranged for multiple-effect evaporation and in fluid communication on one inlet side with a second upper steam outlet from a second distillation unit; Clause 23: The heat recovery system of clauses 1922 and 24-26, in which the vapor recompression unit is configured to compress received vapor through the first high-pressure side by means of Petition 870260078936, dated 06 / 08 / 2026, pages 60 / 84 51 / 52 mechanical vapor recompression or thermal vapor recompression; Clause 24: The heat recovery system of any of clauses 19-23 and 25-26, wherein the steam condensate vessel further includes a third heat exchanger in fluid communication with an external system configured to supply thermal energy to the steam condensate vessel via the third heat exchanger; Clause 25: The heat recovery system of any of clauses 19-24 and 26, further comprising: a second steam compressor connected on a third low-pressure side to the second high-pressure side of the first steam compressor and connected on a third high-pressure side to a third heat exchanger included in a high-pressure receiving system; Clause 26: The heat recovery system of any of the clauses 19-25, wherein the high-pressure receiving system is at least one of: an extraction column; a vaporizer; a superheater; and a turbine; Clause 27: A heat recovery system, comprising: a steam condensate vaporization vessel including a first heat exchanger and configured to store steam condensate, wherein the first heat exchanger is configured to exchange heat from a hot source to the steam condensate to generate low-pressure steam; a receiving system including a second heat exchanger configured to receive medium-pressure steam and to exchange heat from the medium-pressure steam to a fluid retained in the receiving system; a steam recompression unit connected to the first heat exchanger and configured to compress an upper steam stream received from a distillation unit into a compressed upper steam that is supplied as a hot source to the first heat exchanger; and a first compressor. Petition 870260078936, dated 06 / 08 / 2026, pp. 61 / 84 The 52 / 52 steam configuration produces medium-pressure steam from low-pressure steam received from the steam condensate evaporation vessel and directs the medium-pressure steam to the second heat exchanger.

[0108] Without further elaboration, it is believed that a person skilled in the art may use the foregoing description to utilize the claimed inventions to their fullest extent. The examples and aspects disclosed herein should be interpreted as merely illustrative and not as a limitation of the scope of the present invention in any way. It will be evident to those skilled in the art that alterations can be made to the details of the examples described above without departing from the underlying principles discussed. In other words, various modifications and improvements of the examples specifically disclosed in the description above are within the scope of the appended claims. For example, any suitable combination of features of the various examples described is contemplated. Petition 870260078936, dated 06 / 08 / 2026, pages 62 / 84

Claims

1 / 9 Claims 1. HEAT RECOVERY SYSTEM, characterized by comprising: a vapor recompression unit (120a) connected on a first low-pressure side to an upper vapor outlet of a distillation unit and connected on a first high-pressure side to a first heat exchanger (114a) for a condensate vessel (136); and a first compressor (120b) connected on a second low-pressure side to an outlet of the condensate vessel (136) and connected on a second high-pressure side to a second heat exchanger (114b) for a medium-pressure receiving system, wherein the first heat exchanger (114a) transfers heat from a first vapor of an organic fluid received from the distillation unit through the vapor recompression unit (120a) to a working fluid of a non-organic fluid in the condensate vessel (136) to generate a second vapor of the working fluid which is emitted through the outlet to the first compressor (120b);and a second compressor (120c) connected on a third low-pressure side to the second high-pressure side of the first compressor (120b) and connected on a third high-pressure side to a third heat exchanger (114c) included in a high-pressure receiving system.

2. HEAT RECOVERY SYSTEM, according to claim 1, further characterized by comprising: a reflux line connected on an outlet side of the first heat exchanger (114a) opposite an inlet side through which the first heat exchanger (114a) receives the upper steam outlet from the vapor recompression unit (120a), configured to selectively direct portions of a condensate from the upper steam outlet to the distillation unit as part of a reflux stream and to a separation system.

3. HEAT RECOVERY SYSTEM, according to claim 2, characterized in that the distillation unit includes at least one of: a rectification column (108); a rectification column (108) in direct fluid communication with the separation system through a bottom stream generated by the rectification column (108); a rectification column (108) in direct fluid communication with a side stripper through the bottom stream; a rectification / extraction column (112); a beer column; and a beer column in direct fluid communication with the separation system through the upper steam outlet.

4. HEAT RECOVERY SYSTEM, according to claim 2, characterized in that the separation system includes at least one of the following: a vaporizer (118); an extraction column (122); a membrane (124); and a molecular sieve unit (128).

5. HEAT RECOVERY SYSTEM, according to claim 1, characterized in that the vapor recompression unit (120) comprises a mechanical vapor recompression compressor (MVR).

6. HEAT RECOVERY SYSTEM, according to claim 1, characterized in that the condensate vessel (136) further includes a third heat exchanger (114c) in fluid communication with an external system configured to supply thermal energy to the condensate vessel (136) via the third heat exchanger (114c).

7. HEAT RECOVERY SYSTEM, according to claim 1, characterized in that the vapor recompression unit (120) comprises a thermal vapor recompression compressor (TVR).

8. HEAT RECOVERY SYSTEM, according to claim 1, characterized in that the vapor recompression unit (120) compresses the first vapor from a first pressure to a second pressure, higher than the first pressure, and in that the first compressor (120b) compresses the second vapor to a third pressure, higher than the second pressure.

9. HEAT RECOVERY SYSTEM, according to claim 1, characterized in that the non-organic fluid has a different material composition that is less volatile than an organic fluid material composition.

10. HEAT RECOVERY SYSTEM, according to claim 1, characterized in that the first compressor (120b) comprises a thermal vapor recompression (TVR) compressor.

11. HEAT RECOVERY SYSTEM, according to claim 1, characterized in that the second compressor (120c) comprises a thermal vapor recompression (TVR) compressor.

12. DISTILLATION AND DEHYDRATION METHOD (1600), characterized by comprising: generating (1610) an upper distillation stream in a distillation system; directing (1620) the upper distillation stream to a compression system, producing a compressed vapor; sending (1640) the compressed vapor to a condensation system, producing a condensate stream from the compressed vapor and heating a non-organic working fluid in the condensation system for Petition 870260078936, dated 06 / 08 / 2026, page.65 / 84 4 / 9 produce a hot steam stream at a first determined pressure; direct (1650) the condensate stream from the condensation system to a separation system; compress at least a portion of the hot stream from the first determined pressure to a second determined pressure, higher than the first determined pressure; direct the hot stream at the second pressure to a heat exchanger (114) communicating with the separation system to produce a cold liquid stream, transferring thermal energy from the hot stream to a fluid contained by the separation system; and return the cold steam stream to the condensation system.

13. METHOD (1600), according to claim 12, characterized in that the compression system is a vapor recompression unit (120), comprising a mechanical vapor recompression compressor (MVR) or a thermal vapor recompression compressor (TVR).

14. METHOD (1600), according to claim 12, characterized in that the distillation system is one of: a rectification column (108); a rectification column (108) in direct fluid communication with the separation system through a bottom stream generated by the rectification column (108); a rectification column (108) in direct fluid communication with a side extraction column (110) through the bottom stream; a rectification / extraction column (112); and a beer column.

15. METHOD (1600), according to claim 12, characterized in that the separation system includes at least one of: a vaporizer (118); Petition 870260078936, dated 06 / 08 / 2026, page 66 / 84 5 / 9 an extraction column (122); a membrane (124); and a molecular sieve unit (128).

16. METHOD (1600), according to claim 12, characterized in that the condensate stream sent to the separation system is less than the entire condensate stream output of the condensation system and a remainder of the condensate stream output is sent to the distillation system as at least part of a reflux stream.

17. METHOD (1600), according to claim 12, characterized in that the distillation system comprises a first distillation column (102a) operating at a first pressure that receives a first portion of a feed mixture comprising an organic solvent, water and solids operating in fluid communication with a second distillation column (102b) that receives a second portion of the feed mixture and operates at a second pressure different from the first distillation column (102a).

18. METHOD (1600), according to claim 12, characterized in that the distillation system is a rectification system that receives a first vaporous upper stream from a first distillation column (102a) as an input, wherein a second distillation column (102b) produces a second vaporous upper stream from a feed mixture shared with the first distillation column (102a) that is directed to the separation system without passing through the distillation system.

19. METHOD (1600), according to claim 12, characterized by further comprising: producing a second vaporous upper stream in a second distillation column (102b) using a feed mixture shared with the distillation system; Petition 870260078936, dated 06 / 08 / 2026, page 67 / 84 6 / 9 directing the second vaporous upper stream to a plurality of multiple-effect evaporators (130); condensing, in the plurality of multiple-effect evaporators (130), the second vaporous upper stream into a second condensate stream; and directing the second condensate vapor to the separation system.

20. METHOD (1600), according to claim 12, characterized in that a first portion of the hot stream at the second determined pressure is directed to the heat exchanger (114) in communication with the separation system, the method (1600) further comprising: compressing (1670) a second portion of the hot stream from the second determined pressure to a third determined pressure, higher than the second determined pressure; and directing (1680) the second portion of the hot stream at the third determined pressure to a receiving system different from the separation system.

21. METHOD (1600), according to claim 12, characterized by further comprising: recovering heat from a hot stream to heat a cold stream while generating an enriched solvent stream through the separation system.

22. METHOD (1600), according to claim 12, characterized by comprising: sending (1630) compressed steam to a heat exchanger (114) enclosed in a condensate vessel (136) that generates steam at a first pressure; compressing (1670) the steam from the first pressure to a second pressure, higher than the first pressure; directing (1680) the steam at the second pressure to a first receiving system of a splitter; directing a first portion of the steam at the second pressure from the splitter to a second receiving system; compressing a remainder of the steam not directed to the second receiving system from the second pressure to a third pressure, higher than the second pressure; and directing the steam at the third pressure to a third receiving system.

23. METHOD (1600), according to claim 12, characterized by comprising: a first heat exchanger (114a) in communication with a working fluid composed of a non-organic fluid retained in a condensate vessel (136) to generate a second vapor of the working fluid at a first pressure; compressing the second vapor from the first pressure to a second pressure, higher than the first pressure; directing a first portion of the second vapor at the second pressure to a second heat exchanger (114b) in communication with a first receiving system; compressing a second portion of the second vapor at the second pressure to a third pressure, higher than the second pressure; and directing the second portion of the second vapor at the third pressure to a third heat exchanger (114c) in communication with a second receiving system.

24. METHOD (1600), according to claim 23, characterized in that the distillation system comprises a first distillation column (102a) operating at a first distillation pressure that receives a first portion of a feed mixture composed of an organic solvent, water and solids operating in fluid communication with a second distillation column (102b) that receives a second portion of the feed mixture and operates at a second distillation pressure different from the first distillation pressure.

25. METHOD (1600), according to claim 23, characterized by sending the compressed vapor to the first heat exchanger (114a), sending a first portion of the compressed vapor to the first heat exchanger (114a), the method (1600) further comprising: sending a second portion of the compressed vapor of the organic fluid to a condensation system, producing a condensate stream; and directing the condensate stream to a separation system to produce an output stream with a higher concentration of the organic fluid than the condensate stream, wherein the separation system includes at least one of the following: a vaporizer (118); an extraction column (122); a membrane (124); and a molecular sieve unit (128).

26. METHOD (1600), according to claim 23, characterized in that the condensate vessel (136) further includes a fourth heat exchanger (114d) in fluid communication with an external system configured to provide additional thermal energy to the condensate vessel (136) by means of the fourth heat exchanger (114d).

27. METHOD (1600), according to claim 26, characterized by further comprising: Petition 870260078936, dated 06 / 08 / 2026, page 70 / 84 9 / 9 directing the compressed vapor, after heat exchange with the working fluid retained in the condensate vessel (136), through the first heat exchanger (114a), to one or more of the following: the distillation system; the first receiving system; and the second receiving system.

28. METHOD (1600), according to claim 12, characterized by compressing at least a portion of the hot stream from the first determined pressure to a second determined pressure, further comprising: compressing the hot stream from the first determined pressure to an intermediate pressure between the first determined pressure and the second determined pressure; directing a first portion of the hot stream at the intermediate pressure to a receiving system other than the separation system; and compressing the remainder of the hot stream at the intermediate pressure to the second pressure. Petition 870260078936, dated 06 / 08 / 2026, pp. 71 / 84

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