IPC분류정보
국가/구분 |
United States(US) Patent
등록
|
국제특허분류(IPC7판) |
|
출원번호 |
US-0558645
(2004-06-04)
|
등록번호 |
US-7293421
(2007-11-13)
|
우선권정보 |
FR-03 06839(2003-06-06) |
국제출원번호 |
PCT/FR04/001388
(2004-06-04)
|
§371/§102 date |
20051130
(20051130)
|
국제공개번호 |
WO04/111556
(2004-12-23)
|
발명자
/ 주소 |
- Michalski,Pierre
- Gourmelen,Pierre
- Blaizat,Claude
|
출원인 / 주소 |
- Gaz Transport et Technigaz
|
대리인 / 주소 |
|
인용정보 |
피인용 횟수 :
2 인용 특허 :
5 |
초록
▼
A method for cooling a product (P) including N ordered adsorption/desorption cycles (100, 200, 300), each cycle having the following steps: expanding a refrigerant in liquid phase from a condenser (101, 201, 301) inside an evaporator (103, 203, 303) for evaporating at least one portion of the refrig
A method for cooling a product (P) including N ordered adsorption/desorption cycles (100, 200, 300), each cycle having the following steps: expanding a refrigerant in liquid phase from a condenser (101, 201, 301) inside an evaporator (103, 203, 303) for evaporating at least one portion of the refrigerant, and; adsorbing this refrigerant in vapor phase inside at least one adsorption/desorption chamber (120, 220, 320) containing a zeolite adsorbent (Z) whereby cooling a remaining portion of the refrigerant in the evaporator to a predetermined low temperature, the low temperature decreasing from one cycle to the next. The method also includes the following steps: effecting N-1 heat exchanges each time the refrigerant enters the evaporator (103, 203) of a cycle and each time the refrigerant enters the condenser (201, 301) of the following cycle for condensing the refrigerant in the condenser.
대표청구항
▼
The invention claimed is: 1. A method for cooling a product (P) comprising N ordered adsorption/desorption cycles (100, 200, 300, 400, 500, 600) performed under vacuum, N being an integer greater than 1, each cycle comprising the steps consisting in: extracting heat from a refrigerating fluid in th
The invention claimed is: 1. A method for cooling a product (P) comprising N ordered adsorption/desorption cycles (100, 200, 300, 400, 500, 600) performed under vacuum, N being an integer greater than 1, each cycle comprising the steps consisting in: extracting heat from a refrigerating fluid in the vapor phase in a condenser (101, 201, 301, 401, 501, 601) at a first pressure (P2) below the critical pressure of said fluid for condensing said refrigerating fluid, introducing said refrigerating fluid in the liquid phase into an evaporator (103, 203, 303, 403, 503, 603) at a second pressure (P1) lower than the first pressure in order to vaporize some of said refrigerating fluid and cool the rest of said refrigerating fluid to a vaporization temperature (T1) of said refrigerating fluid at said second pressure, said vaporization temperature decreasing from one cycle to the next, said first and second pressures being chosen in each cycle so that said vaporization temperature (T1) in one cycle is each time lower than the condensation temperature (T2) of the refrigeration fluid in the next cycle at the first pressure of said next cycle, supplying heat to the liquid fraction of said refrigerating fluid at said second pressure in said evaporator in order to evaporate said refrigerating fluid, adsorbing said refrigerating fluid in the vapor phase in at least one adsorption/desorption chamber (120, 220, 320, 421-423, 521-523, 621-623) connected to said evaporator and containing a zeolite adsorbent (Z) once a quantity of said refrigerating fluid has been adsorbed into said zeolite adsorbent, regenerating said zeolite adsorbent by heating in order to desorb said quantity of refrigerating fluid in the vapor phase, returning said quantity of refrigerating fluid in the vapor phase to said condenser, said method further comprising the steps consisting in: performing N-1 heat exchanges, each performed between the refrigerating fluid in the evaporator (103, 203, 403, 503) of one cycle and the refrigerating fluid in the condenser (201, 301, 501, 601) of the next cycle in the order of the cycles in order thus to supply said heat to said evaporator and extract said heat in said condenser, and cooling said product by exchange of heat with the refrigerating fluid at least in the evaporator (303, 603) of the last cycle. 2. The method as claimed in claim 1, characterized in that said extraction of heat in the condenser of the first cycle is performed by exchange of heat with an environmental fluid at ambient temperature. 3. The method as claimed in claim 1, characterized in that, in at least one of said cycles, the heating of said zeolite adsorbent (Z) to be regenerated is performed by exchange of heat with an environmental fluid at ambient temperature. 4. The method as claimed in claim 1, characterized in that it comprises the step that consists in performing at least one exchange of heat, preferably at least N-1 exchanges of heat, each heat exchange being between said zeolite adsorbent (Z) undergoing adsorption in an adsorption/desorption chamber (121) of one cycle and said zeolite adsorbent (Z) undergoing regeneration in an adsorption/desorption chamber (223) of the next cycle. 5. The method as claimed claim 1, characterized in that it comprises the step that consists in performing at least one exchange of heat, preferably N-1 exchanges of heat, each heat exchange being between the refrigerating fluid in the evaporator (103, 203) of one cycle and said zeolite adsorbent (Z) in the adsorption/desorption chamber (220, 320) of the next cycle undergoing adsorption, in order to cool said zeolite adsorbent. 6. The method as claimed claim 1, characterized in that, in each cycle, there are at least two adsorption/desorption chambers, so that said adsorption of the refrigerating fluid can be performed in one (121, 221) of said adsorption/desorption chambers while at the same time said regeneration of the zeolite adsorbent (Z) is being performed in another (123, 223) of said adsorption/desorption chambers. 7. The method as claimed in claim 6, characterized in that, in each cycle, there are at least three adsorption/desorption chambers so that a step of cooling the zeolite adsorbent (Z) after regeneration can also be performed at the same time in yet another (122, 222) of said adsorption/desorption chambers. 8. The method as claimed in claim 7, characterized in that it comprises the step that consists in performing at least one exchange of heat, preferably N-1 exchanges of heat, each heat exchange being between the refrigerating fluid in the evaporator (103) of one cycle and said zeolite adsorbent (Z) in the adsorption/desorption chamber (222) of the next cycle undergoing post-regeneration cooling. 9. The method as claimed in claim 1, characterized by the step that consists, in at least one of said cycles, preferably in each of said cycles, in cooling said quantity of refrigerating fluid in the vapor phase by exchange of heat with a source at ambient temperature before said quantity of refrigerating fluid is reintroduced into the condenser. 10. The method as claimed in claim 1, characterized in that, in at least one of said cycles, the first pressure (P2) in said condenser (101, 201, 301, 401, 501, 601) is lower than 3 bar, preferably close to normal pressure. 11. The method as claimed in claim 1, characterized in that, in at least one of said cycles, the maximum pressure is lower than 5 bar, preferably close to normal pressure. 12. The method as claimed in claim 1, characterized in that, in at least one of said cycles, said refrigerating fluid in the liquid phase is introduced in atomized form into the evaporator (103, 203, 303, 403, 503, 603). 13. The method as claimed in claim 1, characterized in that the partial pressure of air in each cycle is less than about 1 kPa, preferably less than about 0.1 kPa. 14. The method as claimed in claim 1, characterized in that the refrigerating fluid in the first cycle (100, 400) is chosen from the group consisting of water, alcohols and mixtures thereof. 15. The method as claimed in claim 14, characterized in that the refrigerating fluid in the second cycle (200, 500) is chosen from the group consisting of butane, butadiene, propadiene, propane and mixtures thereof. 16. The method as claimed in claim 15, characterized in that it comprises a third cycle (300, 600) with a refrigerating fluid chosen from the group consisting of ethane, carbon dioxide, nitrous oxide and mixtures thereof. 17. The method as claimed in claim 16, characterized in that it comprises a fourth cycle with a refrigerating fluid chosen from the group consisting of methane, krypton and mixtures thereof. 18. The method as claimed in claim 17, characterized in that it comprises a fifth cycle with a refrigerating fluid chosen from the group consisting of neon, oxygen, helium, nitrogen, argon, carbon monoxide and mixtures thereof. 19. The method as claimed in claim 1, characterized in that, in at least one of said cycles, said refrigerating fluid has a latent heat of vaporization higher than 300 kJ/kg, preferably greater than or equal to about 450 kJ/kg. 20. The method as claimed in claim 1, characterized in that, in at least one of said cycles, the vaporization temperature (T1) in the evaporator is above the triple point of said refrigerating fluid. 21. The method as claimed in claim 1, characterized in that said product (P) is initially in the vapor phase and in that said product is cooled until it liquefies. 22. The method as claimed in claim 21, characterized in that said product (P) is a gas used as a fuel or as a polymerizable raw material. 23. The method as claimed in claim 1, characterized in that said product (P) is a gas for use as a raw material that is cooled or liquefied to between-80C. and-220C. 24. A device for implementing the method as claimed in claim 1, comprising N ordered cooling stages (100, 200, 300, 400, 500, 600) performed under vacuum, N being an integer greater than 1,each stage comprising: a condenser (101, 201, 301, 401, 501, 601) which contains a refrigerating fluid in a liquid phase, an evaporator (103, 203, 303, 403, 503, 603) connected to said condenser by a pipe (104, 204, 304, 404, 504, 604) at least one adsorption/desorption chamber (120, 220, 320, 421-423, 521-523, 621-623) containing a zeolite adsorbent (Z) and connected to said evaporator via an upstream valve (130, 230, 330) a pipe (160, 260, 360, 460, 560, 660) equipped with a downstream valve (150, 250, 350) for returning said refrigerating fluid from said adsorption/desorption chamber to said condenser, a heating means (140, 240, 243, 340) in said or each adsorption/desorption chamber able to heat said zeolite adsorbent to a regeneration temperature, said device comprising N-1 heat exchangers (280, 380, 501, 601) each arranged in such a way as to exchange heat between the refrigerating fluid in the evaporator (103, 203, 403, 503) of one stage and the refrigerating fluid in the condenser (201, 301, 501, 601) of the next stage in the order of the cycles in order to cool this fluid, and a final heat exchanger (80, 701) arranged in such a way as to exchange heat between a product (P) that is to be cooled and the refrigerating fluid in at least the evaporator of the last stage (303, 603). 25. The device as claimed in claim 24, characterized in that it comprises a heat exchanger (126, 480) arranged in such a way as to exchange heat between the refrigerating fluid in the condenser (101, 401) of the first stage and an environmental fluid at ambient temperature. 26. The device as claimed in claim 24, characterized in that it comprises, by way of heating means for heating at least one of said adsorption/desorption chambers (521-523, 621-623), a heat exchanger (540, 640) arranged in such a way as to exchange heat between said zeolite adsorbent (Z) undergoing adsorption and an environmental fluid at ambient temperature. 27. The device as claimed in claim 24, characterized in that it comprises, in at least one of said stages, a liquid-atomization device (435, 535, 635) arranged in such a way as to atomize the refrigerating fluid in the liquid phase as it is introduced into the evaporator (403, 503, 603). 28. The device as claimed in claim 24, characterized in that, in at least one of said stages, a cooling chamber (216, 316) for cooling the refrigerating fluid is arranged between said or each adsorption/desorption chamber (220, 320) and said condenser (201, 301) and is in thermal contact with a source of heat at ambient temperature. 29. The device as claimed in claim 24, characterized in that it comprises, by way of heating means for heating said adsorption/desorption chambers, at least one heat exchanger (290), preferably at least N-1 heat exchangers, each arranged in such a way as to exchange heat between said zeolite adsorbent (Z) undergoing adsorption in said or one of said adsorption/desorption chamber(s) (121) of one stage and said zeolite adsorbent (Z) undergoing regeneration in said or one of said adsorption/desorption chamber(s) (223) of the next stage. 30. The device as claimed in claim 24, characterized in that it comprises, by way of cooling means for cooling said adsorption/desorption chambers, at least N-1 heat exchangers (280; 380) each arranged in such a way as to exchange heat between the refrigerating fluid in the evaporator (103; 203) of one stage and said zeolite adsorbent (Z) in said or each adsorption/desorption chamber (221, 222, 223; 320) of the next stage. 31. The device as claimed claim 24, characterized in that each stage comprises at least two adsorption/desorption chambers (121, 122, 123) each connected to said evaporator (103) via a respective upstream valve (131, 132, 133) and to said condenser (101) via a respective downstream valve (151, 152, 153). 32. The device as claimed in claim 31, characterized in that it comprises a means of controlling said valves (105) which is programmed to open and close said upstream and downstream valves in a cycle of concurrent operations, in which each chamber (121, 122, 123) performs in succession an adsorption step, for which the upstream valve (131) is open and the downstream valve (151) is closed, a regeneration or desorption step for which the downstream valve (153) is open and the upstream valve (133) is closed, and a post-regeneration cooling step for which the downstream valve (152) and the upstream valve (132) are closed. 33. The device as claimed in claim 24, characterized in that it is associated with a chamber (1) containing said product that is to be cooled, said final heat exchanger (26) being supported within said chamber in order to exchange heat between the refrigerating fluid in the evaporator (303) of the last stage and the product (P) in the liquid or vapor phase contained in said chamber. 34. A methane tanker equipped with a storage tank (1) for liquefied gas (P), with which a device as claimed in claim 33 is associated by way of a refrigerating re-liquefaction unit. 35. A gas-liquefaction plant comprising a cooling chamber (1) for cooling the gas (P) that is to be liquefied, which chamber is associated with a device as claimed in claim 33.
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