CN102564059A - Twin-stage multi-component mixed refrigerant refrigeration natural gas liquefaction system and method - Google Patents
Twin-stage multi-component mixed refrigerant refrigeration natural gas liquefaction system and method Download PDFInfo
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- CN102564059A CN102564059A CN2012100365745A CN201210036574A CN102564059A CN 102564059 A CN102564059 A CN 102564059A CN 2012100365745 A CN2012100365745 A CN 2012100365745A CN 201210036574 A CN201210036574 A CN 201210036574A CN 102564059 A CN102564059 A CN 102564059A
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- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 title claims abstract description 66
- 238000005057 refrigeration Methods 0.000 title claims abstract description 52
- 239000003345 natural gas Substances 0.000 title claims abstract description 33
- 238000000034 method Methods 0.000 title claims abstract description 29
- 239000003507 refrigerant Substances 0.000 title claims abstract description 27
- 230000008569 process Effects 0.000 claims abstract description 22
- 239000007789 gas Substances 0.000 claims abstract description 21
- 239000007788 liquid Substances 0.000 claims abstract description 17
- 239000007791 liquid phase Substances 0.000 claims abstract description 14
- 239000012071 phase Substances 0.000 claims abstract description 11
- 239000000203 mixture Substances 0.000 claims description 12
- 230000006835 compression Effects 0.000 claims description 11
- 238000007906 compression Methods 0.000 claims description 11
- 239000004215 Carbon black (E152) Substances 0.000 claims description 6
- 238000000926 separation method Methods 0.000 claims description 6
- 229930195733 hydrocarbon Natural products 0.000 claims description 5
- 150000002430 hydrocarbons Chemical class 0.000 claims description 5
- 239000012808 vapor phase Substances 0.000 claims description 3
- IJGRMHOSHXDMSA-UHFFFAOYSA-N nitrogen Substances N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 2
- 229910052757 nitrogen Inorganic materials 0.000 claims description 2
- QJGQUHMNIGDVPM-UHFFFAOYSA-N nitrogen group Chemical group [N] QJGQUHMNIGDVPM-UHFFFAOYSA-N 0.000 claims description 2
- 238000005265 energy consumption Methods 0.000 abstract description 10
- 238000001816 cooling Methods 0.000 abstract description 7
- 238000004519 manufacturing process Methods 0.000 abstract description 5
- 230000008092 positive effect Effects 0.000 abstract 1
- 238000007711 solidification Methods 0.000 abstract 1
- 230000008023 solidification Effects 0.000 abstract 1
- 238000005516 engineering process Methods 0.000 description 34
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 description 20
- 239000001294 propane Substances 0.000 description 10
- 230000008901 benefit Effects 0.000 description 2
- 230000008676 import Effects 0.000 description 2
- 230000006872 improvement Effects 0.000 description 2
- QWTDNUCVQCZILF-UHFFFAOYSA-N isopentane Chemical compound CCC(C)C QWTDNUCVQCZILF-UHFFFAOYSA-N 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- AFABGHUZZDYHJO-UHFFFAOYSA-N dimethyl butane Natural products CCCC(C)C AFABGHUZZDYHJO-UHFFFAOYSA-N 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- IJDNQMDRQITEOD-UHFFFAOYSA-N sec-butylidene Natural products CCCC IJDNQMDRQITEOD-UHFFFAOYSA-N 0.000 description 1
Classifications
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- 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
- F25J1/0002—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the fluid to be liquefied
- F25J1/0022—Hydrocarbons, e.g. natural gas
-
- 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
- F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
- F25J1/0047—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using an "external" refrigerant stream in a closed vapor compression cycle
- F25J1/0052—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using an "external" refrigerant stream in a closed vapor compression cycle by vaporising a liquid refrigerant stream
- F25J1/0055—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using an "external" refrigerant stream in a closed vapor compression cycle by vaporising a liquid refrigerant stream originating from an incorporated cascade
-
- 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
- F25J1/0211—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 a multi-component refrigerant [MCR] fluid in a closed vapor compression cycle
- F25J1/0214—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 a multi-component refrigerant [MCR] fluid in a closed vapor compression cycle as a dual level refrigeration cascade with at least one MCR cycle
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- Engineering & Computer Science (AREA)
- Physics & Mathematics (AREA)
- Mechanical Engineering (AREA)
- Thermal Sciences (AREA)
- General Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Separation By Low-Temperature Treatments (AREA)
Abstract
The invention discloses a twin-stage multi-component mixed refrigerant refrigeration natural gas liquefaction system and a method. On the basis of a traditional single mixed refrigerant refrigeration circulation process, a pre-cooling system is provided, wherein natural gas and high pressure mixed refrigerant are pre-cooled to -30 DEG C to -60 DEG C; and a single over-cooling and throttling design is adopted for the gas phase and liquid phase mixed refrigerant in the refrigeration circulation procedure. The invention has the positive effects that subsection refrigeration is more efficient and energy consumption can be saved by more than 12% in comparison with the traditional mixed refrigerant refrigeration process; domestication of key equipment and upsizing of liquefaction devices can be facilitated; the power of a single compressor can be reduced greatly and requirements on the power grid are reduced; a pre-cooling section is separated from a liquefaction and over-cooling sections, so the problem that heavy components cannot be gasified at a low temperature section and the refrigeration system cannot circulate normally due to liquid block or solidification is solved; refrigerant proportioning can be optimized and modulated and refrigeration efficiency can be improved; the pre-cooling circulation process has simple procedures and saved investment; and the pre-cooling compressor has a simple structure and low manufacture cost and is convenient to realize domestication.
Description
Technical field
The present invention relates to a kind of natural gas liquefaction process, especially relate to a kind of twin-stage multicomponent azeotrope refrigeration natural gas liquefaction system and method.
Background technology
Natural gas liquefaction process is broadly divided into following three kinds both at home and abroad at present:
1) stepwise kind of refrigeration cycle; 2) azeotrope kind of refrigeration cycle is subdivided into band again or does not circulate with circulation of the single-stage mixing cryogen of precooling and multistage azeotrope; 3) swell refrigeration is subdivided into band again or does not freeze with the single-stage expansion of precooling refrigeration and multiple expansion.
Above technology is adapted to the natural gas liquefaction plant of different disposal scale because of characteristics separately.Table 1 has been listed the refrigerating cycle liquefied technology of stepwise than the comparison of power consumption with the ratio power consumption of other several kinds of liquefaction process; The ratio power consumption of the refrigerating cycle liquefied technology of typical case's stepwise is 0.33kW.h/kgLNG; Ratio power consumption with the refrigerating cycle liquefied technology of stepwise in table 1 is a standard of comparison, is taken as 1.
The contrast of table 1 liquefaction process energy consumption
| Liquefaction flow path | The energy consumption contrast | The liquefaction scale that is fit to |
| The refrigerating cycle liquefied technology of stepwise | 1.0 | Large-scale plant |
| Single-stage mixing cryogen refrigerating cycle liquefied technology | 1.25 | 30~200x10 4m 3/d |
| The mixing cryogen refrigerating cycle liquefied technology of band propane precooling | 1.15 | 200~300x10 4m 3/d |
| Multistage mixing cryogen refrigerating cycle liquefied technology | 1.05 | 200~400 x10 4m 3/d |
| The refrigerating cycle liquefied technology of single-stage expansion | 2.0 | 10 x10 4m 3/d |
| The single-stage expansion refrigeration liquefying technology of band propane precooling | 1.7 | 20 x10 4m 3/d |
| Double expansion refrigeration liquefying technology | 1.7 | 20 x10 4m 3/d |
The natural gas liquefaction process of band swell refrigeration circulation is too high because of plant energy consumption, is substituted by the mixing cryogen refrigerating cycle liquefied technology of single-stage gradually in recent years.Single-stage mixing cryogen refrigerating cycle liquefied technology is present domestic and international 50 * 10
4The main flow technology of the liquefaction factory of the following treatment scale of t/a.And the mixing cryogen refrigerating cycle liquefied technology (C3/MRC) and the multistage azeotrope refrigeration liquefying flow path of the precooling of band propane are used for 50x10 more
4The large-scale base load type natural gas liquefaction device that the t/a natural gas is above.The refrigerating cycle liquefied technology of stepwise is because flow sheet equipment is many, flow process is complicated, investment is big, only is applicable to the ultra-large type natural gas liquefaction device.
1) azeotrope kind of refrigeration cycle (MRC)
The azeotrope kind of refrigeration cycle is to adopt N
2And C
1～C
5Hydrocarbon mixture is as the technology of circulating refrigerant.The characteristics of this technology are in kind of refrigeration cycle, to adopt mix refrigerant, only need a compressor, and it is simple to compare stepwise kind of refrigeration cycle flow process, invests low.Simultaneously, the single-stage mixing cryogen kind of refrigeration cycle also has its shortcoming: in actual production process, it is the comparison difficulty that the required cold that cold and cryogen provided of whole liquefaction process (from normal temperature to-162 ℃) is mated fully.Therefore the stepwise circulation process of 9 thermograde levels of ability loss-rate of mix refrigerant circulation process is high.
Simultaneously, when greater than 50x10
4During t/a liquefaction scale, limited and the mix refrigerant pipe diameter is limited because of separate unit cryogen compressor load, developed band propane precooling+azeotrope kind of refrigeration cycle technology or multistage azeotrope kind of refrigeration cycle technology.
2) C3/MRC technology and DMRC technology
Development is further maximized when natural gas liquefaction plant, develops into the MRC technology of propane precooling, is called for short C3/MRC, and its efficient circulates near stepwise, and investment is near single azeotrope kind of refrigeration cycle (SMR) technology.This ratio juris is that branch is supplied with cold for two sections: high temperature section provides cold with propane refrigeration system, by 3～4 thermogrades raw natural gas and high pressure section azeotrope is pre-chilled to-30 ℃; The low-temperature zone heat exchange provides cold by high-pressure refrigerant.The propane chilldown system has complicated multistage pressure control system in the C3/MRC technology, and its technology is only grasped by U.S. APCI company, and the multistage air suction structure of propane compressor causes this compressor to need import.
On the basis of C3/MRC technology, the precooling technology that adopts azeotrope to replace propane to carry out abbreviates DMRC technology as.Adopt azeotrope to replace the propane cryogen, make the enthalpy curve of precooling zone cold flow and hot-fluid more approaching on the one hand, improved thermodynamic efficiency; Compressor arrangement is simple on the other hand, is convenient to production domesticization.But receive the influence of azeotrope heat exchange efficiency in heat exchanger, its energy consumption is a little more than C3/MRC.
Because Gas Prices rises steadily in recent years, the natural gas liquefaction plant cost of material constantly increases, thereby causes the liquefaction plant profit margin constantly to descend.A kind of energy consumption of exploitation improvement is low, the variable working condition ability is strong, and the home-made equipment degree is high, and the liquefaction process that can effectively reduce cost of investment is very necessary.
Summary of the invention
In order to overcome the above-mentioned shortcoming of prior art; The invention provides a kind of twin-stage multicomponent azeotrope refrigeration natural gas liquefaction system and method; In conjunction with traditional two azeotrope kind of refrigeration cycle technological advantages; Do technological improvement and innovation on heat exchange process and the cryogen proportioning to precooling zone and liquefaction super cooled sect simultaneously, had characteristics such as energy consumption is low, the variable working condition ability strong, key equipment can domesticize, gross investment is low.
The technical solution adopted for the present invention to solve the technical problems is: a kind of twin-stage multicomponent azeotrope refrigeration natural gas liquefaction system comprises precooling zone refrigeration system and liquefaction and super cooled sect refrigeration system; Said precooling zone refrigeration system comprises precooling compressor, precooling compressor outlet cooler and the precooling compressor outlet separator that connects successively; The liquid and gas of said precooling compressor outlet separator all insert the precooling zone heat exchanger, and entering precooling compressor circulates after going out the precooling zone heat exchanger; Said liquefaction and super cooled sect refrigeration system comprise high pressure mixing cryogen knockout drum, liquefaction and super cooled sect heat exchanger, high pressure mixing cryogen compressor and the high pressure mixing cryogen compressor outlet cooler that connects successively; The liquid and gas of said high pressure mixing cryogen knockout drum all insert liquefaction and super cooled sect heat exchanger, and entering high pressure mixing cryogen compressor circulates after going out liquefaction and super cooled sect heat exchanger.
The present invention also provides a kind of twin-stage multicomponent azeotrope refrigeration natural gas liquefaction, comprises the steps:
1) at precooling zone unstripped gas and high pressure mixing cryogen are cooled to-30 ℃～-60 ℃:
Azeotrope is pressurized to 1.0～1.2MPa.g after precooling compressor outlet cooler water-cooled to 40 ℃ entering precooling compressor outlet separator through precooling compressor one-level; In precooling compressor outlet separator, carry out gas-liquid separation, isolated gas phase and liquid phase refrigerant get into respectively the precooling zone heat exchanger further cool off, cold excessively; Liquid phase refrigerant is crossed and is gone out heat exchanger after cold, is that precooling zone provides-5 ℃～-20 ℃ cold through getting into heat exchanger after the J-T valve throttling; Vapor phase refrigerant liquefaction, crossing and go out the precooling zone heat exchanger after cold, is that precooling zone provides-30 ℃～-60 ℃ cold through getting into heat exchanger after the 2nd J-T valve throttling; Mix refrigerant is heated, gasifies in the precooling zone heat exchanger, and re-heat is returned the precooling compressor behind the normal temperature and carried out compression cycle;
2) natural gas is liquefied and cold excessively in liquefaction and super cooled sect:
The cooled high pressure mixing cryogen of process supercharging gets in the high pressure mixing cryogen knockout drum after precooling zone is pre-chilled to-30 ℃～-60 ℃ and carries out gas-liquid separation, and isolated gas phase and liquid phase get into liquefaction respectively and the super cooled sect heat exchanger further cools off; The liquid-phase mixing cryogen is crossed and is gone out heat exchanger after cold, is that liquefaction stages provides cold through getting into heat exchanger after the 3rd J-T valve throttling; Gas phase azeotrope liquefaction is also crossed and is gone out heat exchanger after cold, through getting into heat exchanger after the 4th J-T valve throttling, for liquefaction stages and super cooled sect provide cold; At last, the azeotrope re-heat is returned high pressure mixing cryogen compressor after-40 ℃ and is carried out compression cycle;
Natural gas is cooled to supercooled state and discharges in liquefaction and super cooled sect heat exchanger, after throttling, get into the LNG storage tank stores.
Compared with prior art, good effect of the present invention is:
One, the present invention is on the basis of the single azeotrope kind of refrigeration cycle technology of tradition (SMR); Increased by a cover chilldown system (mainly comprising precooling compressor and precooling zone heat exchanger); To-30 ℃～-60 ℃, two circulation azeotrope refrigeration process are compared SMR and are had following advantage with natural gas and the precooling of high pressure mixing cryogen:
1) the division system cold efficiency is higher, saves energy consumption more than 15%;
2) main cryogenic heat exchanger, cryogen compressor change two into by one, help the production domesticization of key equipment and the maximization of liquefying plant;
3) twin-stage multicomponent azeotrope refrigeration natural gas liquefaction flow process, the separate unit compressor horsepower significantly reduces, to the requirement reduction of electrical network;
4) with precooling zone and liquefaction and super cooled sect separately, heavy ends such as media such as normal butane, isopentane in the azeotrope do not get into low-temperature zone, have avoided heavy ends can't gasify in low-temperature zone, form the liquid plug or solidify to cause the problem that refrigeration system can't normal circulation.
Two, compare with traditional double circularly cooling technology, gas phase, the liquid-phase mixing cryogen of kind of refrigeration cycle process are taked cold excessively separately, throttling design, and (the cold throttling of the independent mistake of liquid refrigerant in the precooling compressor outlet separator forms a cryogenic temperature level; The cold throttling of the independent mistake of liquid refrigerant in the high pressure mixing cryogen knockout drum forms a cryogenic temperature level), can optimize and revise the cryogen proportioning, improved refrigerating efficiency, save energy consumption about 9%, cancelled the liquid refrigerant delivery pump simultaneously.
Three, compare with C3/MRC technology, precooling circulation technology flow process is simple, reduced investment; Precooling compressor (centrifugal) is the one-level compression, and simple in structure, cost is low, and is beneficial to the realization production domesticization; Two kinds of process energy consumptions are suitable.
Description of drawings
The present invention will explain through example and with reference to the mode of accompanying drawing, wherein:
Fig. 1 is a system principle sketch map of the present invention.
The specific embodiment
A kind of twin-stage multicomponent azeotrope refrigeration natural gas liquefaction system; As shown in Figure 1, comprising: precooling compressor 1, high pressure mixing cryogen compressor 2, main heat exchanger 3 (comprising precooling zone heat exchanger, liquefaction and super cooled sect heat exchanger), precooling suction port of compressor suction tank 4, precooling compressor outlet separator 5, precooling compressor outlet cooler 6, high pressure mixing cryogen suction port of compressor suction tank 7, high pressure mixing cryogen compressor interstage cooler 8, high pressure mixing cryogen compressor outlet cooler 9, high pressure mixing cryogen knockout drum 10, a J-T valve 11, the 2nd J-T valve 12, the 3rd J-T valve 13 and the 4th J-T valve 14.Wherein:
Precooling compressor 1, precooling compressor outlet cooler 6, precooling compressor outlet separator 5 and precooling zone heat exchanger constitute the precooling zone refrigeration system; The liquid and gas of precooling compressor outlet separator 5 all insert the precooling zone heat exchanger; Follow out the precooling zone heat exchanger; Get into the precooling zone heat exchanger again through a J-T valve 11 and the 2nd J-T valve 12 respectively then; Go out the precooling zone heat exchanger at last, suction tank 4 entering precooling compressors 1 circulate through the precooling suction port of compressor.
High pressure mixing cryogen knockout drum 10, liquefaction and super cooled sect heat exchanger, high pressure mixing cryogen compressor 2 and high pressure mixing cryogen compressor outlet cooler 9 constitute liquefaction and super cooled sect refrigeration system; The high pressure mixing cryogen outlet of precooling zone heat exchanger is connected with the import of high pressure mixing cryogen knockout drum 10; The liquid and gas of high pressure mixing cryogen knockout drum 10 all insert liquefaction and super cooled sect heat exchanger; Follow out liquefaction and super cooled sect heat exchanger; Get into liquefaction and super cooled sect heat exchanger again through the 3rd J-T valve 13 and the 4th J-T valve 14 respectively then; Go out liquefaction and super cooled sect heat exchanger at last, suction tank 7 gets into high pressure mixing cryogen compressor 2 through high pressure mixing cryogen suction port of compressor, and high pressure mixing cryogen compressor 2 inserts the precooling zone heat exchanger through high pressure mixing cryogen compressor outlet cooler 9 backs through pipeline.High pressure mixing cryogen compressor 2 has two stages of compression, between two stages of compression, is provided with high pressure mixing cryogen compressor interstage cooler 8.
Clean natural gas via pipeline passes through to pass through to get into the LNG storage tank stores behind the choke valve after pipeline gets into liquefaction and super cooled sect heat exchanger after getting into the precooling zone heat exchanger again.
A kind of twin-stage multicomponent azeotrope refrigeration natural gas liquefaction comprises the steps:
1) at precooling zone unstripped gas and high pressure mixing cryogen are cooled to-30 ℃～-60 ℃:
Azeotrope at precooling zone is a hydrocarbon mixture, forms the refrigerating capacity that can optimize and revise each temperature section through the adjustment hydrocarbon mixture.
Azeotrope is pressurized to 1.0～1.2MPa.g after precooling compressor outlet cooler 6 water-cooleds to 40 ℃ entering precooling compressor outlet separator 5 through precooling compressor 1 one-level; In precooling compressor outlet separator 5, carry out gas-liquid separation, isolated gas phase and liquid phase refrigerant get into respectively the precooling zone heat exchanger further cool off, cold excessively; Liquid phase refrigerant is crossed and is gone out heat exchanger after cold, is the cold that precooling zone provides higher temperature (5 ℃～-20 ℃) through getting into heat exchanger after a J-T valve 11 throttlings; Vapor phase refrigerant liquefaction, crossing and go out the precooling zone heat exchanger after cold, is the cold that precooling zone provides lower temperature (30 ℃～-60 ℃) through getting into heat exchanger after 12 throttlings of the 2nd J-T valve; Mix refrigerant is heated, gasifies in the precooling zone heat exchanger, and re-heat is returned precooling compressor 1 through precooling suction port of compressor suction tank 4 behind the normal temperature and carried out compression cycle.
2) natural gas is liquefied and cold excessively in liquefaction and super cooled sect:
Azeotrope at liquefaction and super cooled sect is nitrogen and hydrocarbon mixture, forms the refrigerating capacity that can optimize and revise each temperature section through the adjustment azeotrope.
Get in the high pressure mixing cryogen knockout drum 10 after precooling zone is pre-chilled to-30～-60 ℃ through the cooled high pressure mixing cryogen of supercharging and to carry out gas-liquid separation, isolated gas phase and liquid phase get into liquefaction respectively and the super cooled sect heat exchanger further cools off; The liquid-phase mixing cryogen is crossed and is gone out heat exchanger after cold, is that liquefaction stages provides cold through getting into heat exchanger after 13 throttlings of the 3rd J-T valve; Gas phase azeotrope liquefaction is also crossed and is gone out heat exchanger after cold, through getting into heat exchanger after 14 throttlings of the 4th J-T valve, for liquefaction stages and super cooled sect provide cold; At last, the azeotrope re-heat is returned high pressure mixing cryogen compressor 2 through high pressure mixing cryogen suction port of compressor suction tank 7 after-40 ℃ and is carried out compression cycle.
Natural gas is cooled to supercooled state and discharges in liquefaction and super cooled sect heat exchanger, after throttling, get into the LNG storage tank stores.
Claims (4)
1. a twin-stage multicomponent azeotrope refrigeration natural gas liquefaction system is characterized in that: comprise precooling zone refrigeration system and liquefaction and super cooled sect refrigeration system; Said precooling zone refrigeration system comprises precooling compressor, precooling compressor outlet cooler and the precooling compressor outlet separator that connects successively; The liquid and gas of said precooling compressor outlet separator all insert the precooling zone heat exchanger, and entering precooling compressor circulates after going out the precooling zone heat exchanger; Said liquefaction and super cooled sect refrigeration system comprise high pressure mixing cryogen knockout drum, liquefaction and super cooled sect heat exchanger, high pressure mixing cryogen compressor and the high pressure mixing cryogen compressor outlet cooler that connects successively; The liquid and gas of said high pressure mixing cryogen knockout drum all insert liquefaction and super cooled sect heat exchanger, and entering high pressure mixing cryogen compressor circulates after going out liquefaction and super cooled sect heat exchanger.
2. twin-stage multicomponent azeotrope refrigeration natural gas liquefaction system according to claim 1, it is characterized in that: said high pressure mixing cryogen compressor has two stages of compression, between two stages of compression, is provided with high pressure mixing cryogen compressor interstage cooler.
3. a twin-stage multicomponent azeotrope refrigeration natural gas liquefaction is characterized in that: comprise the steps:
1) at precooling zone unstripped gas and high pressure mixing cryogen are cooled to-30 ℃～-60 ℃:
Azeotrope is pressurized to 1.0～1.2MPa.g after precooling compressor outlet cooler water-cooled to 40 ℃ entering precooling compressor outlet separator through precooling compressor one-level; In precooling compressor outlet separator, carry out gas-liquid separation, isolated gas phase and liquid phase refrigerant get into respectively the precooling zone heat exchanger further cool off, cold excessively; Liquid phase refrigerant is crossed and is gone out heat exchanger after cold, is that precooling zone provides-5 ℃～-20 ℃ cold through getting into heat exchanger after the J-T valve throttling; Vapor phase refrigerant liquefaction, crossing and go out the precooling zone heat exchanger after cold, is that precooling zone provides-30 ℃～-60 ℃ cold through getting into heat exchanger after the 2nd J-T valve throttling; Mix refrigerant is heated, gasifies in the precooling zone heat exchanger, and re-heat is returned the precooling compressor behind the normal temperature and carried out compression cycle;
2) natural gas is liquefied and cold excessively in liquefaction and super cooled sect:
The cooled high pressure mixing cryogen of process supercharging gets in the high pressure mixing cryogen knockout drum after precooling zone is pre-chilled to-30 ℃～-60 ℃ and carries out gas-liquid separation, and isolated gas phase and liquid phase get into liquefaction respectively and the super cooled sect heat exchanger further cools off; The liquid-phase mixing cryogen is crossed and is gone out heat exchanger after cold, is that liquefaction stages provides cold through getting into heat exchanger after the 3rd J-T valve throttling; Gas phase azeotrope liquefaction is also crossed and is gone out heat exchanger after cold, through getting into heat exchanger after the 4th J-T valve throttling, for liquefaction stages and super cooled sect provide cold; At last, the azeotrope re-heat is returned high pressure mixing cryogen compressor after-40 ℃ and is carried out compression cycle;
Natural gas is cooled to supercooled state and discharges in liquefaction and super cooled sect heat exchanger, after throttling, get into the LNG storage tank stores.
4. twin-stage multicomponent azeotrope refrigeration natural gas liquefaction according to claim 3, it is characterized in that: the azeotrope at precooling zone is a hydrocarbon mixture; Azeotrope at liquefaction and super cooled sect is nitrogen and hydrocarbon mixture.
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| CN103062989A (en) * | 2013-01-24 | 2013-04-24 | 成都深冷液化设备股份有限公司 | Natural gas liquefaction device and process for mixed refrigeration |
| CN103343877A (en) * | 2013-07-26 | 2013-10-09 | 武汉钢铁(集团)公司 | Method and system for pre-cooling ethylene storage tank by low temperature nitrogen |
| CN105737516A (en) * | 2016-04-18 | 2016-07-06 | 中国寰球工程公司 | System and method for liquefying natural gas by mixed refrigerant precooling and nitrogen expansion |
| CN105783420A (en) * | 2016-04-11 | 2016-07-20 | 中国海洋石油总公司 | Double-refrigerant circulating natural gas liquefaction system based on wound-tube heat exchanger |
| CN106441964A (en) * | 2016-09-14 | 2017-02-22 | 中海石油气电集团有限责任公司 | Floating type test platform of natural gas liquefaction system |
| CN107869881A (en) * | 2016-09-27 | 2018-04-03 | 气体产品与化学公司 | Mix refrigerant cooling procedure and system |
| CN109564057A (en) * | 2016-07-06 | 2019-04-02 | 塞彭公司 | For make natural gas liquefaction and recycling may be from natural gas liquid method, including to two semi-open refrigerant circulations of natural gas and one to the closed refrigerant circulation of refrigerant gas |
| CN113639523A (en) * | 2021-08-18 | 2021-11-12 | 中海石油气电集团有限责任公司 | Natural gas liquefaction system and method |
| US11460244B2 (en) | 2016-06-30 | 2022-10-04 | Baker Hughes Oilfield Operations Llc | System and method for producing liquefied natural gas |
| CN117029377A (en) * | 2023-07-27 | 2023-11-10 | 成都赛普瑞兴科技有限公司 | Cascaded refrigeration cycle LNG liquefaction system and method |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN103062989A (en) * | 2013-01-24 | 2013-04-24 | 成都深冷液化设备股份有限公司 | Natural gas liquefaction device and process for mixed refrigeration |
| CN103062989B (en) * | 2013-01-24 | 2015-03-11 | 成都深冷液化设备股份有限公司 | Natural gas liquefaction device and process for mixed refrigeration |
| CN103343877A (en) * | 2013-07-26 | 2013-10-09 | 武汉钢铁(集团)公司 | Method and system for pre-cooling ethylene storage tank by low temperature nitrogen |
| CN103343877B (en) * | 2013-07-26 | 2014-12-10 | 武汉钢铁(集团)公司 | Method and system for pre-cooling ethylene storage tank by low temperature nitrogen |
| CN105783420A (en) * | 2016-04-11 | 2016-07-20 | 中国海洋石油总公司 | Double-refrigerant circulating natural gas liquefaction system based on wound-tube heat exchanger |
| CN105737516A (en) * | 2016-04-18 | 2016-07-06 | 中国寰球工程公司 | System and method for liquefying natural gas by mixed refrigerant precooling and nitrogen expansion |
| US11460244B2 (en) | 2016-06-30 | 2022-10-04 | Baker Hughes Oilfield Operations Llc | System and method for producing liquefied natural gas |
| CN109564057A (en) * | 2016-07-06 | 2019-04-02 | 塞彭公司 | For make natural gas liquefaction and recycling may be from natural gas liquid method, including to two semi-open refrigerant circulations of natural gas and one to the closed refrigerant circulation of refrigerant gas |
| CN109564057B (en) * | 2016-07-06 | 2021-04-02 | 塞彭公司 | Method for liquefying natural gas and recovering liquids from natural gas |
| CN106441964B (en) * | 2016-09-14 | 2018-10-02 | 中海石油气电集团有限责任公司 | A kind of test platform of floating natural gas liquefaction system |
| CN106441964A (en) * | 2016-09-14 | 2017-02-22 | 中海石油气电集团有限责任公司 | Floating type test platform of natural gas liquefaction system |
| CN107869881A (en) * | 2016-09-27 | 2018-04-03 | 气体产品与化学公司 | Mix refrigerant cooling procedure and system |
| CN107869881B (en) * | 2016-09-27 | 2020-07-31 | 气体产品与化学公司 | Mixed refrigerant cooling process and system |
| CN113639523A (en) * | 2021-08-18 | 2021-11-12 | 中海石油气电集团有限责任公司 | Natural gas liquefaction system and method |
| CN117029377A (en) * | 2023-07-27 | 2023-11-10 | 成都赛普瑞兴科技有限公司 | Cascaded refrigeration cycle LNG liquefaction system and method |
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