CN103782120A - Methods and apparatus for cold energy recovery - Google Patents
Methods and apparatus for cold energy recovery Download PDFInfo
- Publication number
- CN103782120A CN103782120A CN201180071827.6A CN201180071827A CN103782120A CN 103782120 A CN103782120 A CN 103782120A CN 201180071827 A CN201180071827 A CN 201180071827A CN 103782120 A CN103782120 A CN 103782120A
- Authority
- CN
- China
- Prior art keywords
- heat
- heat exchanger
- fluid
- cold energy
- transfer fluid
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
- 238000000034 method Methods 0.000 title claims abstract description 32
- 238000011084 recovery Methods 0.000 title claims description 8
- 239000013529 heat transfer fluid Substances 0.000 claims abstract description 33
- 239000012530 fluid Substances 0.000 claims abstract description 22
- 239000002826 coolant Substances 0.000 claims abstract description 20
- 238000001816 cooling Methods 0.000 claims abstract description 14
- 239000007788 liquid Substances 0.000 claims description 23
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 claims description 17
- LYCAIKOWRPUZTN-UHFFFAOYSA-N Ethylene glycol Chemical compound OCCO LYCAIKOWRPUZTN-UHFFFAOYSA-N 0.000 claims description 9
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 claims description 9
- 229910052799 carbon Inorganic materials 0.000 claims description 8
- 125000004432 carbon atom Chemical group C* 0.000 claims description 7
- AFABGHUZZDYHJO-UHFFFAOYSA-N 2-Methylpentane Chemical compound CCCC(C)C AFABGHUZZDYHJO-UHFFFAOYSA-N 0.000 claims description 6
- GDOPTJXRTPNYNR-UHFFFAOYSA-N methylcyclopentane Chemical compound CC1CCCC1 GDOPTJXRTPNYNR-UHFFFAOYSA-N 0.000 claims description 6
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 5
- 239000004215 Carbon black (E152) Substances 0.000 claims description 4
- 238000004378 air conditioning Methods 0.000 claims description 4
- 150000008282 halocarbons Chemical group 0.000 claims description 4
- 229930195733 hydrocarbon Natural products 0.000 claims description 4
- 150000002430 hydrocarbons Chemical class 0.000 claims description 3
- 239000012266 salt solution Substances 0.000 claims description 3
- 239000000243 solution Substances 0.000 claims description 3
- 230000001105 regulatory effect Effects 0.000 claims description 2
- -1 carbon atom hydrocarbon Chemical class 0.000 claims 1
- 239000007789 gas Substances 0.000 description 32
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 12
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 10
- 230000008020 evaporation Effects 0.000 description 6
- 238000001704 evaporation Methods 0.000 description 6
- 229910052757 nitrogen Inorganic materials 0.000 description 6
- 239000001569 carbon dioxide Substances 0.000 description 5
- 229910002092 carbon dioxide Inorganic materials 0.000 description 5
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 4
- 239000004149 tartrazine Substances 0.000 description 4
- XKRFYHLGVUSROY-UHFFFAOYSA-N Argon Chemical compound [Ar] XKRFYHLGVUSROY-UHFFFAOYSA-N 0.000 description 2
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 description 2
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 239000003345 natural gas Substances 0.000 description 2
- 239000001301 oxygen Substances 0.000 description 2
- 229910052760 oxygen Inorganic materials 0.000 description 2
- 229910052786 argon Inorganic materials 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 238000009835 boiling Methods 0.000 description 1
- UBAZGMLMVVQSCD-UHFFFAOYSA-N carbon dioxide;molecular oxygen Chemical compound O=O.O=C=O UBAZGMLMVVQSCD-UHFFFAOYSA-N 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000007710 freezing Methods 0.000 description 1
- 230000008014 freezing Effects 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 239000007791 liquid phase Substances 0.000 description 1
- 230000008018 melting Effects 0.000 description 1
- 238000002844 melting Methods 0.000 description 1
- 150000002894 organic compounds Chemical class 0.000 description 1
- 230000001590 oxidative effect Effects 0.000 description 1
- 239000012071 phase Substances 0.000 description 1
- 238000010926 purge Methods 0.000 description 1
- 239000000376 reactant Substances 0.000 description 1
- 238000005057 refrigeration Methods 0.000 description 1
- 230000032258 transport Effects 0.000 description 1
- 239000002912 waste gas Substances 0.000 description 1
Images
Classifications
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
- F25J1/0221—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using the cold stored in an external cryogenic component in an open refrigeration loop
- F25J1/0222—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using the cold stored in an external cryogenic component in an open refrigeration loop in combination with an intermediate heat exchange fluid between the cryogenic component and the fluid to be liquefied
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
- F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
- F17C2227/00—Transfer of fluids, i.e. method or means for transferring the fluid; Heat exchange with the fluid
- F17C2227/03—Heat exchange with the fluid
- F17C2227/0302—Heat exchange with the fluid by heating
- F17C2227/0309—Heat exchange with the fluid by heating using another fluid
- F17C2227/0323—Heat exchange with the fluid by heating using another fluid in a closed loop
Landscapes
- Engineering & Computer Science (AREA)
- Physics & Mathematics (AREA)
- Mechanical Engineering (AREA)
- Thermal Sciences (AREA)
- General Engineering & Computer Science (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
A method and apparatus for recovering cold energy for use in cooling applications from a fluid such as liquefied gas or cold gas. The fluid is fed to a first heat exchanger where it will contact with a cryogenic fluid transferring cold energy into the heat transfer fluid. The heat transfer fluid is fed to a second heat exchanger where it will contact a cooling medium which receives the cold energy from the heat transfer fluid. The cooling medium is recovered and cold energy from the cooling medium is used for the cooling applications.
Description
Background of invention
The present invention relates to be recovered in the method for the cold energy of ordinary loss in liquid gas evaporation process, and relevant equipment.These liquid gas are generally nitrogen, oxygen, argon, carbon dioxide, natural gas and ethene.
Industrial gasses, for example nitrogen, oxygen, carbon dioxide, natural gas and ethene are widely used in many different industrial circles.They can be used as inert media, Purge gas, reactant, cooling medium etc.According to application and consumption, these gases are with gas phase or stored in liquid phase and supply.When gas demand is greater than 1000Nm
3when/hr, because economic cause gas is supplied with conventionally at the scene, liquid gas is supplied/transports and be stored in vacuum jacket container for liquid gas user and small size gas user simultaneously.
Except supplying with at the scene, gas also can be by evaporation liquefied gas supplying.Nitrogen under atmospheric pressure, the boiling point of oxygen and carbon dioxide is respectively-196 ℃ ,-183 ℃ and-78.5 ℃.But well-known is that these gases are liquefied is the process of lot of energy.When these liquid gas evaporate in surrounding air evaporimeter, cold energy loses completely.To there is the gas of environment temperature and the formation of ice is minimized in order to provide, need very large-scale independently evaporator module.In some cases, for example, in winter, need extra heater.For example, when cold energy loss also occurs in liquid gas (liquid nitrogen and liquid carbon dioxide) and is used to cooling object.Due to lower heat exchange efficiency or other process technology limit, the sensible heat of cold energy, especially liquid can not be effectively utilized.
The cold energy losing in evaporation process is produced the cold energy for freezing and cooling use by some gas users by using extra mechanical refrigeration system to reclaim.But directly carrying out heat exchange between liquid gas and water, to reclaim cold energy be dangerous, thereby cause damage because the water in heat exchanger may freeze.
The present invention addresses these problems by service-strong cold energy recovery unit, and cold energy recovery unit can be for substituting traditional surrounding air evaporimeter, and can be in liquid gas evaporation process or from cold waste gas direct recovery cold energy.
Summary of the invention
In one embodiment of the invention, disclose a kind of method that reclaims cold energy from fluid, comprised the steps:
A) fluid is sent into the first heat exchanger and fluid is contacted with heat-transfer fluid;
B) heat-transfer fluid is sent into the second heat exchanger and heat-transfer fluid is contacted with cooling medium; And;
C) from cooling medium, reclaim cold energy.
Fluid or cold energy source are selected from the group for example, being made up of liquid gas and refrigerating gas (liquid nitrogen or liquid carbon dioxide).
The first heat exchanger can be that two heat exchangers and first and second heat exchangers of series connection are all low temperature heat exchanger, for example fin-tube heat exchanger.Fluid is heated and its cold energy is passed to heat-transfer fluid in the first heat exchanger.Heat-transfer fluid is selected from the group being made up of following item: have the absolute alcohol of 1 to 2 carbon atom, for example methyl alcohol or ethanol; There is the hydrocarbon of about six carbon atom, for example isohexane and methyl cyclopentane; And halogenated hydrocarbons, for example carrene group.
Cooling medium or cold energy carrier are selected from the group being made up of light water, ethylene glycol solution and salt solution, and from the second heat exchanger, are extracted out and are used in cooling application, for example reaction temperature control, and air conditioning and technique are cooling.
The flow of heat-transfer fluid is regulated so that its temperature maintains on the set point of cooling medium, with the difficulty of avoiding in the second heat exchanger, cooling medium being condensed.By using expansion tank and control valve, flow is controlled.
In another embodiment of the present invention, disclose a kind of equipment, it comprises the first heat-exchange device being communicated with the second heat-exchange device fluid.This equipment further comprises the expansion tank being communicated with the first heat-exchange device fluid and the circulating pump being communicated with the first and second heat-exchange device fluids.The first heat-exchange device can comprise that the heat exchanger of two series connection and the first and second heat-exchange devices can be all low temperature heat exchangers.
The first and second heat-exchange devices are by line or pipe and the connection of heat-transfer fluid fluid, and described heat-transfer fluid is for obtaining cold energy and passed to the second heat-exchange device from described the first heat-exchange device.Heat-transfer fluid will contact with the cooling medium in the second heat-exchange device, and cooling medium from heat-transfer fluid, reclaims cold energy and this cold energy is recovered for cooling object.
Accompanying drawing summary
Fig. 1 is the process flow diagram of cold energy recovery unit of the present invention.
Detailed description of the Invention
The present invention is a kind of in liquid gas evaporation process or reclaim the method for cold energy from perishing gas.The cold energy reclaiming can be for example, for cooling (technology and equipment be cooling) and for air conditioning.
Referring to Fig. 1, cold energy recovery unit comprises two heat exchanger E101A/B and E102, circulating pump P101, expansion tank V101 and control valve A10.Liquid gas or cold air are introduced into low temperature heat exchanger E101A/B by pipeline 30.In low temperature heat exchanger E101A/B, liquid gas is evaporated and/or cold air is heated and discharge heat exchanger by pipeline 40.
In heat exchanger E101A/B, be delivered to internal heat transfer fluid (HTF) from the cold energy of liquid gas or cold gas, it enters E101A/B by pipeline 50 and discharges by pipeline 60.Adopt special HTF to be minimized in possibility icing in heat exchanger E101A/B.HTF should have at low temperatures relatively low viscosity and produce any condense to prevent HTF at low temperature heat exchanger for guaranteeing good pumpability and having low melting point.The example of suitable HTF used in the present invention is selected in the group being made up of following item: have the absolute alcohol of 1 to 2 carbon atom, for example methyl alcohol or ethanol; There is the hydrocarbon of about six carbon atom, for example isohexane, methyl cyclopentane; Halogenated hydrocarbons, for example carrene; And other has suitable viscosity and the fusing point organic compound with the inside HTF as cold energy recovery unit.
The cold HTF that carrys out automatic heat-exchanger E101A/B is pumped and enters heat exchanger E102, HTF and another kind of cooling medium (for example light water, ethylene glycol solution or salt solution) contact therein and exchanged heat.Cooling medium is introduced into heat exchanger E102 by pipeline 10.Discharge in pipeline 20 through overcooled cooling medium, it can be for any cooling object, for example reaction temperature control, and air conditioning and technique are cooling.
Adopt the flow of the HTF of control valve A10 to circulation to regulate, to guarantee that the temperature T 01 of cold HTF in pipeline 70 is not less than the set point of cooling medium in pipeline 10.Pass through the flow of the HTF of pipeline 70 by change, can make icing the minimizing in heat exchanger E102.
When desired be from liquid gas, for example liquid nitrogen or liquid carbon dioxide reclaim cold energy, can in first step, adopt two heat exchangers.Heat exchanger E101A/B can be divided into two heat exchangers, the low temperature heat exchanger E101A use of can connecting with low temperature heat exchanger E101B.Liquid gas evaporates and is further heated in heat exchanger E101B in heat exchanger E101A.In the case of cold gas, can use one or two heat exchanger according to the temperature of cold gas flow and flow.These two heat exchanger E101A and E101B can be integrated into single heat exchanger, thus evaporation and heating fluid oxidizing gases in single low temperature heat exchanger.
Expansion tank V101 is also necessary for balance HTF about the change in volume of temperature correlation.
Although the present invention is described with reference to its specific embodiment, be apparent that multiple other form of the present invention and improvement it will be apparent to those skilled in the art that.The appended claim of the present invention should be interpreted as covering whole these apparent form and improvement within true spirit of the present invention and scope that are positioned at generally.
Claims (23)
1. from a method for fluid recovery cold energy, comprise the steps:
A) described fluid is sent into the first heat exchanger and described fluid is contacted with heat-transfer fluid;
B) described heat-transfer fluid is sent into the second heat exchanger and described heat-transfer fluid is contacted with cooling medium; And
C) reclaim cold energy from described cooling medium.
2. the method for claim 1, is characterized in that, described fluid is selected from the group being made up of liquid gas and cold air.
3. the method for claim 1, is characterized in that, described the first heat exchanger is low temperature heat exchanger.
4. the method for claim 1, is characterized in that, described the first heat exchanger is two heat exchangers of series connection.
5. the method for claim 1, is characterized in that, described fluid is heated in described the first heat exchanger.
6. the method for claim 1, is characterized in that, cold energy is delivered to the described heat-transfer fluid in described the first heat exchanger.
7. the method for claim 1, is characterized in that, described heat-transfer fluid is from selecting by having the group that the absolute alcohol of 1 to 2 carbon atom, the hydrocarbon with about six carbon atom and halogenated hydrocarbons form.
8. method as claimed in claim 7, is characterized in that, described in there is 1 to 2 carbon atom absolute alcohol from the group being formed by methyl alcohol and ethanol, select.
9. method as claimed in claim 8, is characterized in that, described in there is about six carbon atom hydrocarbon from the group being formed by isohexane and methyl cyclopentane, select.
10. method as claimed in claim 7, is characterized in that, described halogenated hydrocarbons is carrene.
11. the method for claim 1, is characterized in that, described the second heat exchanger is low temperature heat exchanger.
12. the method for claim 1, is characterized in that, described cooling medium is selected from the group being made up of light water, ethylene glycol solution and salt solution.
13. the method for claim 1, is characterized in that, extract described cooling medium and for cooling application from described the second heat exchanger.
14. methods as claimed in claim 13, is characterized in that, described cooling application is from by selecting the cooling group forming of reaction temperature control, air conditioning and technique.
15. the method for claim 1, is characterized in that, the flow of described heat-transfer fluid is regulated so that its temperature maintains on the set point of described cooling medium.
16. methods as claimed in claim 15, is characterized in that, by using expansion tank and control valve to carry out described Flow-rate adjustment.
17. 1 kinds of equipment, comprise the first heat-exchange device being communicated with the second heat-exchange device fluid.
18. equipment as claimed in claim 17, further comprise the expansion tank being communicated with described the first heat-exchange device fluid.
19. equipment as claimed in claim 17, further comprise the circulating pump being communicated with described the first and second heat-exchange device fluids.
20. equipment as claimed in claim 17, is characterized in that, described the first heat-exchange device comprises two heat exchangers of series connection.
21. equipment as claimed in claim 17, is characterized in that, described the first and second heat-exchange devices are low temperature heat exchanger.
22. equipment as claimed in claim 17, is characterized in that, described the first and second heat-exchange devices are communicated with by heat-transfer fluid fluid.
23. equipment as claimed in claim 17, is characterized in that, cold energy is recovered from described the second heat-exchange device.
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| PCT/CN2011/075921 WO2012174700A1 (en) | 2011-06-21 | 2011-06-21 | Methods and apparatus for cold energy recovery |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN103782120A true CN103782120A (en) | 2014-05-07 |
Family
ID=47421967
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201180071827.6A Pending CN103782120A (en) | 2011-06-21 | 2011-06-21 | Methods and apparatus for cold energy recovery |
Country Status (3)
| Country | Link |
|---|---|
| EP (1) | EP2724101A1 (en) |
| CN (1) | CN103782120A (en) |
| WO (1) | WO2012174700A1 (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108759303A (en) * | 2018-08-03 | 2018-11-06 | 丁斌 | A kind of cryogenic liquid gasification cold energy recycle device |
| CN112325548A (en) * | 2020-10-26 | 2021-02-05 | 常德宜利管道制造有限公司 | Water-saving circulating device and water circulating method for production of PE pressure-resistant and pressure-resistant pipeline |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20150273977A1 (en) * | 2014-03-26 | 2015-10-01 | Ron C. Lee | Method and apparatus for in-transit refrigeration |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN2499774Y (en) * | 2001-08-19 | 2002-07-10 | 中国科学技术大学 | Air separator using liquefied natural gas cold energy |
| CN1407303A (en) * | 2001-08-19 | 2003-04-02 | 中国科学技术大学 | Air separator by utilizing cold energy of liquefied natural gas |
| US20060156757A1 (en) * | 2005-01-14 | 2006-07-20 | Ryuichi Honda | Apparatus for improving production efficiency of dry ice |
| CN201532078U (en) * | 2009-06-04 | 2010-07-21 | 中国海洋石油总公司 | Air separating system using liquefied natural gas cold energy |
Family Cites Families (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS5252261A (en) * | 1975-10-24 | 1977-04-26 | Hitachi Zosen Corp | Heat exchange for utilizing cold energy of liquefied natural gas |
| US20110297346A1 (en) * | 2009-02-11 | 2011-12-08 | Moses Minta | Methods and Systems of Regenerative Heat Exchange |
-
2011
- 2011-06-21 CN CN201180071827.6A patent/CN103782120A/en active Pending
- 2011-06-21 EP EP11868360.6A patent/EP2724101A1/en not_active Withdrawn
- 2011-06-21 WO PCT/CN2011/075921 patent/WO2012174700A1/en active Application Filing
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN2499774Y (en) * | 2001-08-19 | 2002-07-10 | 中国科学技术大学 | Air separator using liquefied natural gas cold energy |
| CN1407303A (en) * | 2001-08-19 | 2003-04-02 | 中国科学技术大学 | Air separator by utilizing cold energy of liquefied natural gas |
| US20060156757A1 (en) * | 2005-01-14 | 2006-07-20 | Ryuichi Honda | Apparatus for improving production efficiency of dry ice |
| CN201532078U (en) * | 2009-06-04 | 2010-07-21 | 中国海洋石油总公司 | Air separating system using liquefied natural gas cold energy |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108759303A (en) * | 2018-08-03 | 2018-11-06 | 丁斌 | A kind of cryogenic liquid gasification cold energy recycle device |
| CN112325548A (en) * | 2020-10-26 | 2021-02-05 | 常德宜利管道制造有限公司 | Water-saving circulating device and water circulating method for production of PE pressure-resistant and pressure-resistant pipeline |
Also Published As
| Publication number | Publication date |
|---|---|
| EP2724101A1 (en) | 2014-04-30 |
| WO2012174700A1 (en) | 2012-12-27 |
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