Method and plant for the production of ice, slush / ice particles, snow, hydrates, cold water or combinations thereof or mixtures / suspensions in a closed process

Abstract

Method for producing ice, slush / ice particles, snow, hydrates, cold water or combinations thereof or mixture / suspension in a closed process, characterized in that a) at least one material stream (2) in the form of ice, slush / ice particles, snow, hydrates, cold water or combinations thereof or mixture / suspension b) with a refrigerant of a material stream (1) c) are gathered in an apparatus (3) and relax and cool in and / or upon exiting the apparatus (3), d) the stream (1 / 2) exiting the apparatus (3) from the material streams (1) and (2) is fed into a container (4) with storage function, e) in the container (4) a phase separation of the material streams (1) and (2) takes place and - the first material stream (1) containing the refrigerant is taken from the container (4) and - the second material stream (2) reduced in temperature in the form of ice, slush / ice particles, snow, hydrates, cold water or combinations thereof or mixture / suspension performs a cooling function - wherein at least one further material flow leads into the apparatus (3) as a secondary circuit.

Description

[0001] The invention relates to a method and a plant for producing ice, slush / ice particles, snow, hydrates, cold water or combinations or mixtures / suspensions thereof in a closed process according to the preamble of claims 1 and 15.

[0002] Storing cold water and water ice offers many (theoretical) advantages (e.g., ecological storage medium, pumpability of ice slurry). However, ice slurry systems have failed to gain widespread acceptance for various reasons (e.g., excessively expensive equipment, insufficient efficiency). Furthermore, various technologies cannot be scaled to large capacities, or scaling them to large capacities has not resulted in cost reductions or efficiency improvements.

[0003] Therefore, the production of ice slurry requires a process engineering approach (e.g., injector technology). Furthermore, conventional refrigeration machines with (still) approved refrigerants (due to climate and environmental damage, flammability, explosion hazard, toxicity, etc.) are often used for refrigeration.

[0004] From publication DE 10 2010 0184 97 A1, a method and a device for producing ice slurry are known. In this solution, water is mixed with a supercooled refrigerant using a mixing nozzle. Upon contact, the water freezes, forming a so-called ice slurry. Expansion also occurs in the mixing nozzle. In a storage tank, the refrigerant and ice slurry are separated, allowing the ice slurry to be discharged through an outlet and perform its cooling function. After use, it is returned to the tank via a return line, discharged from the storage tank together with the refrigerant, and separated into water and refrigerant by means of a pump and a separation device. The refrigerant is then returned to its initial state, and the cycle is closed. This is a complex separation process (e.g.,Reverse osmosis, nanofiltration) is required to cool a partial flow in an evaporator (material separation of heat transfer fluid and refrigerant) of a refrigeration system.

[0005] Publication WO 2007121603 A1 describes a device for producing ice slush, specifically using carbon dioxide as a refrigerant. The carbon dioxide is injected into an aqueous solution via nozzle devices to produce ice slush.

[0006] Carbon dioxide can be injected in liquid and / or gaseous form into an aqueous solution using injector nozzles or - as an alternative - by prior mixing in a nozzle.

[0007] The refrigerant is also under pressure and exists at a temperature around or below 0 degrees Celsius. The refrigerant circuit and the waste cycle (with a refrigeration consumer) are separated into two material flows.

[0008] The hydrated slurry (possibly containing ice particles) forms in the container either through cooling coils or by decompression. The coil can be located inside or outside the container and also serves to control the temperature.

[0009] Cooling the refrigerant in the form of carbon dioxide is not planned and may not be strictly necessary for the production of hydrates, however, it does limit the possibility of improved process control.

[0010] Furthermore, the heat of hydration is drawn from the storage tank, which can negatively impact temperatures. The heat exchanger located on the tank does not allow for high capacities. Ultimately, ice production occurs in a two-stage process through the dissolution of hydrates. Overall, the described system is not energy-efficient and is incapable of providing high cooling capacities.

[0011] A method and apparatus for cooling are also described in EP 2 667 116 A1. A refrigerant is mixed with liquid carbon dioxide under pressure at which the mixture is in a liquid state. The mixture of refrigerant and liquid carbon dioxide is then depressurized to a pressure at which at least some of the carbon dioxide evaporates. The depressurized mixture is then fed to a separator in which the evaporated carbon dioxide is separated from the refrigerant. The separated refrigerant is then repressurized and recirculated for mixing with liquid carbon dioxide. The mixture, after depressurization, and / or the refrigerant from the separator, passes through a heat exchanger in which it is brought into thermal contact with a medium to be cooled.The gaseous carbon dioxide is discharged via the gas outlet 19 and used in a heat exchanger 20 to cool a medium or released into the atmosphere. Therefore, this is an open process.

[0012] Disadvantageously, the heat transfer fluid is not stored; the separator merely performs phase separation. Furthermore, no ice slurry generation, etc., is achieved. The cooling of a medium in the temperature range of -85 to -56 °C takes place. The heat exchanger 9 represents an additional component that is not required in the solution according to the invention and would not function effectively.

[0013] A pressure relief device is required after a mixing unit for the liquid carbon dioxide and the carrier medium, which also means additional effort.

[0014] A refrigerant compressor for the liquid carbon dioxide is, unfortunately, not provided. Furthermore, the regulation of the refrigerant and heat transfer fluid flow (liquid carbon dioxide and heat transfer medium) is carried out via a valve 8, which is disadvantageous.

[0015] The pressure range is limited to 10 to 20 bar, resulting in a restricted operating range. A further disadvantage is the inadequate description of how the medium is cooled by the heat exchanger. Additionally, this solution uses alcohols / terpenes as the heat transfer fluid, which does not undergo a phase change.

[0016] Another solution is described in German patent application DE 10 2019 127 488 A1, which is a closed-loop process. The objective of this solution is to provide a flexibly deployable fluid circuit with a circulating working fluid and a method for operating the fluid circuit to generate cooling capacity. The cooling is to be utilized at a temperature or pressure level below the triple point of the working fluid. The device should be able to be operated reliably and safely, efficiently, and easily controlled, particularly without the risk of clogging by solid particles in the working fluid. A mixture of environmentally friendly, non-flammable fluids should be usable. There is no cold storage, no ice slurry generation, etc. The document primarily describes the operational optimization of a refrigeration machine (safety, prevention of clogging).

[0017] The refrigerant used is CO2 (R744), and the heat transfer fluid is either R125 (which is also a refrigerant) or R410 (a refrigerant mixture), although R410 is not environmentally friendly. A mixing device is provided for blending the heat transfer fluid with the working fluid, as well as a separator for separating the heat transfer fluid from the gaseous fluid flow. A compressor and a heat exchanger are located between the separator and the mixing device. Furthermore, another heat exchanger is located between the mixing device and the separator, which adds to the complexity of the system.

[0018] Furthermore, the cooling effect here is achieved through sublimation rather than evaporation, gas hydrate dissociation, or outgassing. Additionally, lubricating oil is used as the heat transfer fluid instead of water, although the use of water is not possible at the specified temperatures. The refrigerant acts as a heat transfer fluid in the form of solid particles within the carrier fluid, which has only this function (and lubrication).

[0019] In general, no refrigeration or ice production plants or storage systems are known that are suitable for the large-scale utilization of surplus electricity, particularly from renewable energy sources. Furthermore, no solutions exist for the industrial provision of process cooling and process heat. The flexibilization of energy supply systems and the consistent ecological design of processes and plants are novel concepts in this context.

[0020] The object of the invention is to develop a system and a process for producing ice, slush / ice particles, snow, hydrates, chilled water, or combinations or mixtures / suspensions thereof for industrial or technical applications. This system, using an environmentally friendly refrigerant and heat transfer fluid, enables high cooling capacities and high ice production, while allowing for very high storage charging and discharging capacities, system integration, and, if desired, direct application to, for example, food products or feeding into pipelines (e.g., district cooling). Furthermore, it should be possible to provide ice, slush / ice particles, snow, hydrates, chilled water, or combinations or mixtures / suspensions thereof at temperatures ranging from -100 °C to -20 °C.

[0021] This problem is solved by the features of claims 1 and 15. Advantageous embodiments are described in the dependent claims.

[0022] In the process for producing ice, slush / ice particles, snow, hydrates, cold water or combinations thereof or mixtures / suspensions in a closed process, according to the invention, a) at least one second material stream in the form of ice, slush / ice particles, snow, hydrates, cold water or combinations thereof or mixture / suspension, b) and a first material stream containing at least one refrigerant, c) combined in an apparatus, wherein the material streams relax and cool in the apparatus and / or upon exiting the apparatus, d) wherein the stream exiting the apparatus from the first and second material streams is fed into at least one container with a storage function, e) phase separation of the first and second material streams takes place in the container and - the first stream of material containing the refrigerant is taken from the container and - the second material stream, reduced in temperature and in the form of ice, slush / ice particles, snow, hydrates, cold water or combinations or mixtures / suspensions thereof, performs a cooling function, - wherein at least one further material flow leads as a secondary circuit into the apparatus (3).

[0023] After phase separation in the container, the first material stream is drawn out of the container, compressed and cooled in the refrigerant circuit, and fed back into the apparatus. in a first variant the second material stream is taken from the container as a refrigerant circuit to fulfill the cooling task and fed into the refrigerant circuit via a heat exchanger to the container, whereby - the refrigerant circuit leads from a heat exchanger through the apparatus to the tank or - the refrigerant circuit leads from the heat exchanger to the tank and at least one further secondary fluid flow leads as a secondary circuit via the apparatus into the tank and / or in a second variant The cooling task is achieved with at least one heat exchanger assigned to the container and at least one additional second material stream leads as a secondary circuit through the apparatus into the container.

[0024] This involves indirect and / or direct heat transfer between the first material stream and the second material stream in the apparatus and / or upstream of the apparatus, whereby it is also possible to heat and / or cool the material streams in the apparatus by means of at least one additional heating and / or at least one additional cooling, particularly in zones.

[0025] It is possible that a first secondary circuit and a second secondary circuit of the refrigerant of the second material stream from the container lead back into the container under pressure via the apparatus.

[0026] Because the temperature at the exit of the apparatus is significantly reduced compared to the entry into the apparatus, the cooling task can be accomplished with the heat transfer fluid separated in the container.

[0027] The apparatus can be used for mixing and / or dispersion and / or dissolution of the first stream into the second stream and / or temporary hydration and / or a reaction, for example to carbonic acid.

[0028] The expansion takes place in and / or after the apparatus for the production of ice, ice slush / ice particles, snow, hydrates, cold water or combinations thereof, or mixing / suspension of the cooled second material stream, using one or a combination of the following effects: ◯ Change in the thermodynamic state of the first mass stream through evaporation at 10 to 300 kJ / kg or possibly even higher, ◯ Degassing of the first material stream due to physical solubility, ◯ Dissolution of the hydrates of the first and second mass streams, ◯ Joule-Thompson effect and thus relaxation of the refrigerant in the first material stream.

[0029] The pressure increase of the second material stream before its introduction to the apparatus is carried out in particular to a pressure of 1.1 bar to 200 bar, whereby the pressure increase is implemented in multiple stages if necessary.

[0030] Furthermore, the first material stream is fed into the apparatus at a pressure of preferably 1.1 bar to 200 bar and may be introduced in different phases and at a temperature of typically -40°C to 50°C, depending on the need for recooling in the first heat exchanger and / or intermediate cooling or further cooling in an additional heat exchanger.

[0031] The first material stream consists of or contains at least one refrigerant, wherein the refrigerant is preferably not or only slightly soluble in the heat transfer medium.

[0032] The refrigerant consists in particular of carbon dioxide, or propane or nitrous oxide (laughing gas) or gases or vapors with / without phase change or combinations of the aforementioned substances or other suitable refrigerants, or contains such substances.

[0033] The coolant of the second material stream can consist of a mixture of water with at least one freezing point lowering substance for operation with storage temperatures significantly below 0 °C.

[0034] It is possible to implement the following modifications to the first material stream individually or in any combination: a. transcritical or subcritical operating mode, b. single- or multi-stage compression up to a maximum compression pressure of approx. 200 bar, with or without intake superheating c. Parallel connection of compressors, d. with and without intercooling, in particular using internal and / or external heat exchangers, e. possibly use of one or more ejectors, f. possibly the use of one or more refrigerant dryers. g. possibly the use of one or more oil separators.

[0035] After phase separation, a refrigerant from the second material stream of the refrigerant cycle can be fed from the container to a second heat exchanger, and in the second heat exchanger the refrigerant from the second material stream can take over the cooling task.

[0036] In parallel or alternatively, at least one cooling task can be carried out by the container with at least one heat exchanger combined with the container.

[0037] Since the expansion of the material flows in the apparatus causes a strong cooling, the apparatus can be heated to prevent ice formation or to dissolve ice.

[0038] The invention further comprises a system for producing ice, slush / ice particles, snow, hydrates, chilled water or combinations thereof or mixtures / suspensions thereof, wherein the system according to the invention has at least one apparatus comprising at least one first feed for a pressurized first mass flow of a refrigerant of a refrigerant circuit and at least one second feed for a pressurized second mass flow of a heat transfer fluid of a heat transfer fluid circuit and / or at least one secondary mass flow with / from a heat transfer fluid in the form of ice, slush / ice particles, snow, hydrates, chilled water or combinations thereof.The apparatus comprises a mixture / suspension and has at least one chamber in which the first and second material streams can be combined, decompressed and cooled, wherein a container with storage function for phase separation of the first and second material streams is connected to the apparatus, wherein the container has at least one first outlet for the refrigerant and at least one further outlet for the heat transfer medium, wherein at least one further material stream leads as a secondary circuit into the apparatus (3).

[0039] The system for producing ice, slush / ice particles, snow, hydrates, cold water or combinations thereof or mixtures / suspensions in a closed process for fulfilling a cooling task is further characterized according to the invention in that in a first variant the second material stream is taken from the container as a heat transfer fluid circuit to fulfill the cooling task and fed into the container via a second heat exchanger, wherein a) the refrigerant circuit leads from the heat exchanger via the apparatus to the container or b) the refrigerant circuit leads from the heat exchanger to the tank and at least one further second fluid flow leads as a secondary circuit via the apparatus into the tank and / or in a second variant The cooling task is realized with at least one heat exchanger assigned to the container and at least one further second material flow leads as a secondary circuit via the apparatus into the container.

[0040] The system is equipped as follows in the first variant: - with at least one apparatus for combining and subsequently releasing the first and second material streams to produce ice, slush / ice particles, snow, hydrates, cold water or combinations thereof, or a mixture / suspension of the second material stream, - with the second heat exchanger to realize heat transfer for the cooling task from the cooled material / cooling medium to the second material stream, - with a pump to convey the second material stream and to increase the pressure to 1.1 bar to 200 bar in front of the apparatus, - with at least one first heat exchanger to achieve recooling of the refrigerant of the first material stream to a temperature between -40°C and 50°C before the apparatus, - with at least one compressor for compressing and conveying the first material stream and for achieving a pressure of 1.1 bar to 200 bar upstream of the apparatus, - with the container for phase separation of the first and second material streams.

[0041] The container with storage function can have a tangential or substantially tangential supply for at least one current supplied from the apparatus.

[0042] In the container for phase separation of the first and second material streams, the refrigerant of the first material stream is separated in an upper area and the heat transfer fluid of the second material stream is separated in a lower area.

[0043] The refrigerant is then drawn from the upper section and the heat transfer fluid from the lower section of the container, each under pressure, back into the container via the apparatus.

[0044] Advantageously, areas of the system that ice up or where there is a risk of icing can be provided with at least one additional heater and / or at least one heat exchanger, whereby several heating areas can be provided and the heating is effected, for example, by means of electrical resistance and / or microwaves and / or an induction heater and / or a flow of material.

[0045] Furthermore, it is possible to provide the apparatus with additional cooling to dissipate the heat generated during hydration and / or reactions and / or dissolution processes.

[0046] According to the invention, at least one further second material stream can be routed as a secondary circuit via the apparatus into the container.

[0047] Advantageously, the at least one apparatus has at least one inlet for the first material flow and at least one or more inlets for the second material flow and, if necessary, also for the secondary circuits.

[0048] The apparatus may also include means for generating a swirling flow in order to achieve better contact between the material flows.

[0049] These devices can be designed with or without rigid or moving internal components to influence the flow.

[0050] The apparatus can be used to create a continuous or pulsating flow. Furthermore, other flow effects such as turbulence, instability, boundary layer effects, subsonic and supersonic flow can be implemented as needed.

[0051] The system and method according to the invention can be used, for example, as a heat pump system and / or as a combined cooling and heating system.

[0052] The invention is explained in more detail below with reference to exemplary embodiments and accompanying drawings. These show: Fig. 1 Schematic representation of the closed process, feeding of the second material stream 2 from the container via a heat exchanger and the apparatus into the container (cold storage), Fig. 2 Schematic representation of the closed process, feeding of the second material stream 2 from the container (cold storage) via the heat exchanger into the container and first by-product stream from the container (cold storage) and the apparatus into the container, Fig. 3 in addition to the variant according to Fig. 2. Further by-product flow from the container (cold storage) via the apparatus into the container, Fig. 4 in addition to the variant according to Fig. 2. Two-stage compression and intercooling as well as further cooling of the first material stream 1, Fig. 5 in addition to the variant according to Fig. 4. Expansion of the refrigerant with a turbine to generate mechanical power; arrangement of the turbine in front of the apparatus. Fig. 6 in addition to the variant according to Fig. 1 - Heat transfer from the container to a heat exchanger to implement the cooling function, Fig. 7 a first variant of the apparatus with a feed for the material flow 1 (refrigerant) and a feed for the material flow 2 (heat transfer fluid), Fig. 8 a second variant of the apparatus with one feed for the material flow 1 (refrigerant) and two feeds for the material flow 2 (heat transfer fluid).

[0053] According to Fig. 1. In a closed process, the system has a first material stream 1 comprising at least one or consisting of at least one refrigerant and a second material stream 2 comprising at least one or consisting of at least one heat transfer fluid.

[0054] The system is further equipped with an apparatus 3, and an adjoining container 4 with storage function.

[0055] In the closed process, container 4 is first filled with refrigerant (for material stream 1) and heat transfer fluid (for material stream 2), whereby phase separation takes place in container 4.

[0056] The first material stream 1 leads in a refrigerant circuit A from the container 4, in which a phase separation of the material stream 1 and the material stream 2 takes place, via a compressor 5 into a first heat exchanger 1.1, of the first material stream 1 in which a recooling R of the material stream 1 is realized and under pressure into the apparatus 3.

[0057] The second material stream 2 leads in a refrigerant circuit B from the container 4, via a heat exchanger 2.1 of the material stream 2 to realize a cooling task K via a pump 6 also under pressure into the apparatus 3.

[0058] The pressure increase of mass stream 2 to a high pressure may also occur in multiple stages. In apparatus 3, the first and second mass streams 1, 2 are combined and expand, cooling down from temperatures T1 of the first mass stream 1 and T2 of the second mass stream 2 before apparatus 3 to a lower temperature T of the stream 1 / 2 exiting the apparatus.

[0059] The stream 1 / 2, reduced to a temperature T, is fed from the apparatus 3 to the container 4, where phase separation of the two material streams 1 and 2 takes place again, with the refrigerant of material stream 1 preferably settling in the upper region and the heat transfer fluid of material stream 2 settling in the lower region of the container 4. This allows very low temperatures of the heat transfer fluid, down to -20 °C and even lower, down to -100 °C, to be achieved.

[0060] In apparatus 3, a direct or indirect heat transfer takes place between the first material stream 1 and the second material stream 2.

[0061] According to an example not shown, heat transfer / temperature equalization of the two material flows 1, 2 can already be realized in a device upstream of the apparatus 3 (e.g. heat exchanger).

[0062] Furthermore, the material flows 1, 2 can also be heated and / or cooled in the apparatus 3 by at least one additional heating ZH and / or at least one additional cooling ZK, especially zone by zone.

[0063] A continuous or pulsating flow preferably passes through the apparatus 3, and further flow effects such as turbulence, instability, boundary layer effects, subsonic and supersonic flow can be implemented as required.

[0064] The supply of the material stream 1 (e.g. carbon dioxide R744 or other refrigerant) to the apparatus 3 preferably takes place at high pressure, in particular at 1.1 bar to 200 bar and possibly in different phases with a temperature of typically - 40 °C to 50 °C depending on the recooling and / or intermediate cooling.

[0065] The second material stream 2 is preferably conveyed into the apparatus at a pressure of 1.1 bar to 200 bar and at a temperature of -40 °C to 50 °C.

[0066] When the two material streams 1 and 2 are combined in the apparatus 3, they come into complete and / or partial contact, resulting in the formation of, for example, bubbles or droplets. It is also possible that the two material streams are mixed with direct heat transfer.

[0067] The following processes are possible when the two material streams 1, 2 are combined in the apparatus 3, - possibly dissolution of mass flow 1 in mass flow 2, - possibly temporary hydration formation (possibly limiting the process), - possibly reactions to e.g. carbonic acid, - possibly downstream heat transfer with an external heat exchanger.

[0068] The expansion taking place in and / or following the apparatus 3 to produce ice, slush / ice particles, snow, hydrates, cold water or combinations thereof or mixture / suspension of a cooled second material stream 2 is preferably carried out using the following individual effects or combinations thereof: - Change in the thermodynamic state of mass stream 1 due to the evaporation of mass stream 1 / refrigerant (approx. 10 kJ / kg to 300 kJ / kg), - possibly degassing of the refrigerant (substance 1) due to its physical solubility, - possibly dissolution of the hydrates (substances 1 and 2), - possibly Joule-Thompson effect during the expansion of the refrigerant (material flow 1), - possibly evaporation of the material stream 2.

[0069] Furthermore, the phase separation of the material streams takes place in the container / storage 4 (preferably at -100 °C to 20 °C) and / or at least partially in the apparatus during the removal of the gaseous phase (material stream 1) and the collection of the ice, slush, ice particles, snow, hydrates, cold water or their combinations or mixtures or suspensions (material stream 2).

[0070] The first material stream 1 consists of inorganic or organic substances or mixtures or suspensions thereof, wherein in particular all gases and all vapors as well as mixtures thereof with or without phase change can be used as refrigerants, wherein, for example, carbon dioxide or propane or nitrous oxide (laughing gas) or combinations thereof are preferably used as gases and mixtures with, in particular, air are preferably realized.

[0071] Depending on the choice of refrigerant, the pressure when supplying it to apparatus 3 may need to be changed or adjusted accordingly.

[0072] The material stream 1 preferably consists of or contains a refrigerant which is not or only slightly soluble in the heat transfer medium of the material stream 2, thereby promoting phase separation.

[0073] Preferably, the refrigerant is not soluble or only slightly soluble in water (e.g., R290, propane) and, if necessary, in the subcritical region.

[0074] Mixtures (e.g., water and freezing point lowering substances) and / or substances that promote a phase change, such as nucleating particles and / or droplets, can also be used as refrigerants for operation with storage temperatures significantly below 0 °C.

[0075] The appropriate pressure of the material streams 1 and 2 when fed to the apparatus 3 can be calculated or determined by experiments.

[0076] The material stream 2 contains a cold carrier or consists of a cold carrier in the form of ice, slush / ice particles, snow, hydrates, cold water or combinations thereof or mixtures / suspensions.

[0077] From container 4, the material stream 1 (e.g., carbon dioxide, possibly with very low water vapor content) is drawn in and compressed in a closed circuit from the upper area of ​​container 4 by means of the compressor 5, the material stream 1 is cooled back down via the first heat exchanger 1.1 of the material stream 1 and fed into the apparatus 3.

[0078] The following modifications to the refrigerant circuit (material flow 1) can be made, whereby the measures can be implemented individually or in various combinations: - preferably transcritical operation (but also subcritical operation), - Single- or multi-stage compression up to a maximum final compression pressure of approx. 200 bar, with or without intake superheating, - Parallel connection of compressors, - with and without intermediate cooling, - possibly using one or more ejectors, - possibly the use of one or more refrigerant dryers, - possibly the use of at least one oil separator.

[0079] Furthermore, parallel to mass flow 1, mass flow 2 in the form of ice, slush / ice particles, snow, hydrates, cold water or combinations thereof or their mixture / suspension is extracted from the lower area of ​​the container 4 and fed to the second heat exchanger 2.1 of the second mass flow 2 to perform a cooling task K and from there pumped back under pressure into the apparatus 3 by means of the pump 6.

[0080] The storage container (container 4 with storage function) can be discharged directly or indirectly with respect to the second material stream 2.

[0081] The system according to the invention serves for the production and / or storage of ice, ice slush / ice particles, snow, hydrates, cold water or combinations or mixtures / suspensions thereof.

[0082] In this process, container 4 can be filled at the beginning / before the start of the process with a heat transfer fluid (preferably water) and the refrigerant (e.g. carbon dioxide), from / in which ice, slush / ice particles, snow, hydrates, cold water or combinations or mixtures / suspensions of these will form due to the strong cooling in and / or after the apparatus.

[0083] Before first use, the container 4 is preferably evacuated and then filled with the heat transfer fluid (2) and refrigerant (1).

[0084] It is possible to connect several units 3 in parallel to increase cooling capacity or ice production.

[0085] Furthermore, it is possible to use two higher-pressure pumps for the second material stream, particularly in the area of ​​apparatus 3, to partially draw in material stream 1 (injector effect). This also makes it possible to lower the temperature of material stream 1, or to reduce the temperature reduction for material stream 1 and / or the compression rate for material stream 1, and / or to achieve better pre-cooling for material stream 2.

[0086] Further pre-cooling of the material stream 1 is possible internally (in the apparatus) or externally, also by means of external cooling elements or cooling elements provided in the apparatus 3.

[0087] The process and the system can be used as a heat pump system and / or as a combined cooling and heating system.

[0088] The heat recovered from the recooling of the refrigerant can be used for heating purposes.

[0089] It is also possible to use the waste heat generated during the execution of the inventive method, e.g. for heating purposes, for process heat supply, for charging thermal energy storage systems (heat storage) with warm water, hot water, steam and other heat transfer fluids; but also for generating cold with absorption chillers, adsorption chillers, steam jet chillers or as a heat source system for at least one further heat pump.

[0090] In this process, heat can be extracted from the first material stream using at least one cooler and / or at least one recooler and used for heating purposes and / or storage charging within a temperature range of 40°C to 400°C.

[0091] To recover the compression power of compressor 5 of the first material stream 1, it is possible to integrate an expansion machine into the refrigerant circuit of the first material stream 1. This is preferably done upstream of apparatus 3. This also allows for partial expansion of the material stream 1, resulting in cooling.

[0092] The expansion machine can, for example, be a displacement machine and / or turbine T, which in particular drives a generator G for electricity generation (see Fig. 5).

[0093] Further embodiments of the system according to the invention are described in the Fig. Numbers 2 to 6 are shown.

[0094] Fig. 2 shows, in contrast to Fig. 1. The fluid flow 2 of the refrigerant circuit B, intended for cooling, is returned from the heat exchanger 2.1 to the tank 4. For this purpose, a pump 6 is located between the tank 4 and the heat exchanger 2.1.

[0095] To reduce the temperature of the heat transfer fluid, a first by-product stream 2N1 from container 4 is pumped at high pressure and temperature T2 by a pump 6.2 into apparatus 3 (to which the first mass stream is also fed) and from there, after expansion and cooling, back into container 4. The heat transfer fluid returned to container 4 is significantly cooled, which also reduces the temperature of mass stream 2 to achieve the cooling function.

[0096] The first material stream 1 of the refrigerant circuit A is processed as in Fig. 1 from the container 4 via the compressor 5 and the first heat exchanger 1.1 to the apparatus 3.

[0097] In the facility according to Fig. 3 is in addition to the variant according to Fig. 2 a second bypass 2N2 is present in the refrigerant circuit B, which is supplied from the container 4 to the apparatus 3 via a further pump 6.3 at a high pressure and a temperature T3.

[0098] In the facility according to Fig. 4 is the coolant circuit B as in Fig. 2 executed. In addition to the variant according to, refrigerant circuit A has Fig. 2 via a two-stage compression and intercooling process, followed by further cooling of the substance 1. For this purpose, the first substance stream 1 flows from the compressor 5, which performs the first compression stage, via an intermediate tank 7 and a further compressor 5.1, which performs the second compression stage, to the first heat exchanger 1.1. Between the first heat exchanger 1.1 and the apparatus 3, a further heat exchanger 1.2 is provided for further cooling of the first substance stream 1. Furthermore, the further heat exchanger 1.2 is coupled to the further compressor 5.1 via the tank 7. This causes a partial flow of the refrigerant between the two heat exchangers 1.1 and 1.2 to expand in the expansion device 1.3, cooling the remaining substance stream (approximately 20% to 90% of the total first substance stream) and the substance stream after compression by the compressor 5.

[0099] The variant according Fig. 5 essentially has the same structure as in Fig. 4, but additionally realizes in the first material flow 1 before the apparatus 3 an expansion of the refrigerant with an expansion machine, here a turbine T to obtain mechanical power, here the drive of a generator G for electricity generation is realized.

[0100] At Fig. 6 is the refrigerant circuit A as in the Fig. 1, Fig. 2 and Fig. 3. The cooling function of the refrigerant circuit B is implemented here by means of heat transfer from the tank 4 to a pipe system (heat exchanger 8) that surrounds or is integrated into the tank, through which a refrigerant flows. The low temperatures in the tank 4 are thereby transferred to the heat exchanger 8 and the refrigerant flowing through the heat exchanger 8, causing the refrigerant in the heat exchanger 8 to cool down and thus achieving the cooling function K.

[0101] According to the design variants not shown, it is also possible in all variants to provide one or more auxiliary flows of the refrigerant of refrigerant circuit A.

[0102] Furthermore, all described variants can operate with a multi-stage compression of the refrigerant circuit and be equipped with a device for expanding the refrigerant before the apparatus 3, e.g. a turbine T for generating mechanical power, such as for driving a generator G for electricity generation.

[0103] Thus, the in the Fig. Variants 1 to 6 described can be combined depending on the requirements.

[0104] Furthermore, several devices 3 can be used in a system and then, if necessary, several containers 4 and a corresponding number of pumps and heat exchangers for the refrigerant circuit B as well as compressors and heat exchangers for the refrigerant circuit A.

[0105] Alternatively, several devices 3 can be coupled with only one container 4 (not shown).

[0106] The following will be discussed in the Fig. 7 and Fig. 8 Two constructive designs of apparatus 3 are shown.

[0107] Fig. Figure 7 shows a variant of the apparatus 3 with an inner hollow cylindrical / tubular first shell 9, which has an inlet 9.1 and an outlet 9.2 and is provided with a funnel-shaped extension 9.3 towards the outlet 9.2. The first shell 9 is surrounded at a distance by a further hollow cylindrical / tubular second shell 10, which is longer than the first shell 9 and projects beyond the outlet 9.2 of the first shell 9. The first and second shells 9, 10 are arranged concentrically to each other along a longitudinal axis A.

[0108] Between the outer circumference of the first mantle 9 and the inner contour of the second mantle 10, a first annular space 3.1 is formed, and after the exit opening 9.2 of the first mantle 9, a first chamber 3.2 is formed.

[0109] The second jacket 10 has a funnel-shaped diameter widening 10.3 after the cylindrical area in the direction of the outlet 10.2 and a funnel-shaped diameter reduction 10.4 at the inlet 10.1.

[0110] It is possible to supply the first mass stream 1 via inlet 9 and the second mass stream 2 via inlet 10 (as shown), or vice versa. The two mass streams 1 and 2, supplied under high pressure, come into contact in the region of chamber 3.2 and exit the apparatus 3 at outlet 10.2 as a single stream 1 / 2, which is then introduced into the container 4 (not shown). The mass streams expand within the apparatus 3 and consequently cool down significantly. Indirect heat transfer occurs between the mass streams in region 3.1, while direct heat transfer occurs in region 3.2.

[0111] In Fig. Figure 8 shows another variant of an apparatus 3, in which the first coat 9 and the second coat 10 are as in Fig. 7 are executed, with these additionally being surrounded by a third hollow cylindrical shell 11.

[0112] The third hollow cylindrical shell 11 also has an inlet 11.1 and an outlet 11.2 and is provided with a funnel-shaped extension 11.3 in the direction of the outlet 11.2.

[0113] The second jacket 11 is surrounded at a distance by the hollow cylindrical / tubular third jacket 11, which is longer than the second jacket 10 and thus projects beyond the outlet 10.2 of the second jacket 10. The first, second, and third jackets 9, 10, 11 are also arranged concentrically to one another along the longitudinal axis A. A second annular space 3.3 is formed between the outer circumference of the second jacket 10 and the inner contour of the third jacket 11, and a second chamber 3.4 is formed after the outlet opening 10.2 of the second jacket 10.

[0114] It is also possible here to introduce the first mass flow 1 via inlet 9.1 and the second mass flow 2 via inlet 10.1 (as shown), or vice versa. One or both secondary flows 2N1 and 2N2, for example, can be introduced into inlet 11.1.

[0115] The two material streams 1, 2, supplied under high pressure, come into contact in the area of ​​chamber 3.2 and enter the second chamber 3.4 at outlet 10.2, where they come into contact, for example, with the material stream of the secondary circuit(s) 2N1, 2N2.

[0116] Indirect heat transfer is implemented in the annular spaces 3.1, 3.3 and direct heat transfer in the chambers 3.2, 3.4.

[0117] In apparatus 3 and / or after apparatus 3, all material streams expand, thereby cooling down significantly and are introduced as stream 1 / 2 into the container 4, which is not shown here.

[0118] In both variants after Fig. 7 and Fig.8 is, for example, the outermost jacket (second jacket 10 or third jacket 11) equipped with an additional heater ZH and / or additional cooling ZK and / or a heat exchanger 3W, which may also be divided into zones.

[0119] The auxiliary heater ZH or the heat exchanger 3W can, for example, prevent an obstruction of the function according to the invention, e.g., an undesirable ice formation on the surfaces of the apparatus 3.

[0120] Additional cooling (ZK) is preferably used in cases of hydration.

[0121] According to alternative embodiments not shown, the flows 1 / 2 exiting the apparatus can also be introduced essentially tangentially into the container / storage tank 4. This achieves a better separation of the heat transfer fluid and the refrigerant.

[0122] Alternatively, a different method of introducing the material flows into apparatus 3 can be chosen.

[0123] For example, material flow 2 can be introduced via inlet 9.1 and material flow 1 via inlet 10.1.

[0124] When a casing in the form of the third casing 11 is arranged, for example a secondary material stream 2N1, 2N2 can be introduced into the apparatus 3 via the feeder 11.1.

[0125] The supply of material flows can also be radial or oblique, as shown in the examples not illustrated.

[0126] In apparatus 3, the expansion, acceleration and pressure reduction take place which is necessary for the production of ice, ice slush / ice particles, snow, hydrates, cold water or combinations thereof or mixtures / suspensions.

[0127] When the material streams are combined, hydrates may form, or reactions may occur between the material streams, or a physical dissolution of gases from the first material stream 1 into the liquid of the second material stream 2 may occur.

[0128] The hydrates can also decompose in the direction of outlet 10.2 or 11.2 or after the outlets; outgassing of the refrigerant, possibly also a Joule-Thompson effect and possibly also a reverse reaction may occur.

[0129] In apparatus 3, desired turbulence effects, boundary layer effects and instability effects can occur through the flow guidance and various known design modifications in order to reduce the pressure and / or improve the heat transfer between the material streams or to avoid unfavorable operating conditions.

[0130] With the method and system according to the invention, high cooling capacities and high ice productions can be achieved, for example for industrial applications, using an environmentally friendly refrigerant (such as carbon dioxide) and a heat transfer medium (ice, slush / ice particles, snow, hydrates, chilled water or combinations or mixtures / suspensions thereof), whereby temperatures of the heat transfer medium from 20 °C to -100 °C can be provided.

[0131] The system and method according to the invention enable very high storage charging capacities (up to, for example, the megawatt range) and very high storage discharging capacities (up to, for example, the megawatt range). Depending on its dimensions, the system can also provide smaller capacities in the kilowatt range.

[0132] Furthermore, district cooling, for example, can also be provided via pipelines.

[0133] It can also be applied directly to, for example, food.

[0134] Due to the relatively simple design of the system, only minimal operating and maintenance costs are required.

[0135] Another advantage is that the system can also be used as a heat pump system and / or as a combined cooling and heating system.

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