CN203310202U - Dual-mixed-refrigerant liquefying system applied to base load type natural gas liquefaction factory - Google Patents
Dual-mixed-refrigerant liquefying system applied to base load type natural gas liquefaction factory Download PDFInfo
- Publication number
- CN203310202U CN203310202U CN2013202310164U CN201320231016U CN203310202U CN 203310202 U CN203310202 U CN 203310202U CN 2013202310164 U CN2013202310164 U CN 2013202310164U CN 201320231016 U CN201320231016 U CN 201320231016U CN 203310202 U CN203310202 U CN 203310202U
- Authority
- CN
- China
- Prior art keywords
- heat exchanger
- liquefaction
- precooling
- gas
- exchanger device
- 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.)
- Expired - Lifetime
Links
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 title claims abstract description 54
- 239000003345 natural gas Substances 0.000 title claims abstract description 22
- 239000003507 refrigerant Substances 0.000 title abstract description 9
- 239000007788 liquid Substances 0.000 claims description 32
- 239000007791 liquid phase Substances 0.000 claims description 20
- 238000005057 refrigeration Methods 0.000 claims description 16
- 241000196324 Embryophyta Species 0.000 claims description 8
- 240000002853 Nelumbo nucifera Species 0.000 claims description 6
- 235000006508 Nelumbo nucifera Nutrition 0.000 claims description 6
- 235000006510 Nelumbo pentapetala Nutrition 0.000 claims description 6
- 239000007792 gaseous phase Substances 0.000 claims description 6
- 239000007789 gas Substances 0.000 abstract description 25
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 abstract description 20
- 238000001816 cooling Methods 0.000 abstract description 19
- 238000000034 method Methods 0.000 abstract description 12
- 239000001294 propane Substances 0.000 abstract description 10
- 239000002826 coolant Substances 0.000 abstract description 2
- 239000002994 raw material Substances 0.000 abstract description 2
- OFBQJSOFQDEBGM-UHFFFAOYSA-N n-pentane Natural products CCCCC OFBQJSOFQDEBGM-UHFFFAOYSA-N 0.000 description 11
- IJGRMHOSHXDMSA-UHFFFAOYSA-N nitrogen Substances N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 11
- NNPPMTNAJDCUHE-UHFFFAOYSA-N isobutane Chemical compound CC(C)C NNPPMTNAJDCUHE-UHFFFAOYSA-N 0.000 description 10
- 239000000203 mixture Substances 0.000 description 9
- 238000001704 evaporation Methods 0.000 description 8
- 230000008020 evaporation Effects 0.000 description 8
- QWTDNUCVQCZILF-UHFFFAOYSA-N isopentane Chemical compound CCC(C)C QWTDNUCVQCZILF-UHFFFAOYSA-N 0.000 description 8
- 239000012071 phase Substances 0.000 description 8
- 238000007906 compression Methods 0.000 description 7
- 230000006835 compression Effects 0.000 description 7
- 229910052757 nitrogen Inorganic materials 0.000 description 6
- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 description 5
- 239000001273 butane Substances 0.000 description 5
- 239000001282 iso-butane Substances 0.000 description 5
- 235000013847 iso-butane Nutrition 0.000 description 5
- IJDNQMDRQITEOD-UHFFFAOYSA-N n-butane Chemical compound CCCC IJDNQMDRQITEOD-UHFFFAOYSA-N 0.000 description 5
- AFABGHUZZDYHJO-UHFFFAOYSA-N dimethyl butane Natural products CCCC(C)C AFABGHUZZDYHJO-UHFFFAOYSA-N 0.000 description 4
- 239000004215 Carbon black (E152) Substances 0.000 description 2
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 description 2
- 229930195733 hydrocarbon Natural products 0.000 description 2
- 150000002430 hydrocarbons Chemical class 0.000 description 2
- 210000000689 upper leg Anatomy 0.000 description 2
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 239000000470 constituent Substances 0.000 description 1
- 238000005261 decarburization Methods 0.000 description 1
- 230000018044 dehydration Effects 0.000 description 1
- 238000006297 dehydration reaction Methods 0.000 description 1
- 238000006477 desulfuration reaction Methods 0.000 description 1
- 230000023556 desulfurization Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- QJGQUHMNIGDVPM-UHFFFAOYSA-N nitrogen group Chemical group [N] QJGQUHMNIGDVPM-UHFFFAOYSA-N 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
- F25J1/0002—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
-
- 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
- F25J1/0228—Coupling of the liquefaction unit to other units or processes, so-called integrated processes
- F25J1/0235—Heat exchange integration
- F25J1/0237—Heat exchange integration integrating refrigeration provided for liquefaction and purification/treatment of the gas to be liquefied, e.g. heavy hydrocarbon removal from natural gas
- F25J1/0238—Purification or treatment step is integrated within one refrigeration cycle only, i.e. the same or single refrigeration cycle provides feed gas cooling (if present) and overhead gas cooling
-
- 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
- F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
- F25J1/0257—Construction and layout of liquefaction equipments, e.g. valves, machines
- F25J1/0262—Details of the cold heat exchange system
-
- 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
- F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
- F25J1/0257—Construction and layout of liquefaction equipments, e.g. valves, machines
- F25J1/0262—Details of the cold heat exchange system
- F25J1/0264—Arrangement of heat exchanger cores in parallel with different functions, e.g. different cooling streams
-
- 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
- F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
- F25J1/0279—Compression of refrigerant or internal recycle fluid, e.g. kind of compressor, accumulator, suction drum etc.
- F25J1/0292—Refrigerant compression by cold or cryogenic suction of the refrigerant 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
- F25J2220/00—Processes or apparatus involving steps for the removal of impurities
- F25J2220/60—Separating impurities from natural gas, e.g. mercury, cyclic hydrocarbons
- F25J2220/64—Separating heavy hydrocarbons, e.g. NGL, LPG, C4+ hydrocarbons or heavy condensates in general
Landscapes
- Engineering & Computer Science (AREA)
- Physics & Mathematics (AREA)
- Mechanical Engineering (AREA)
- Thermal Sciences (AREA)
- General Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Separation By Low-Temperature Treatments (AREA)
Abstract
The utility model discloses a dual-mixed-refrigerant liquefying system applied to a base load type natural gas liquefaction factory. The dual-mixed-refrigerant liquefying system comprises a precooling heat exchanger, a liquefying heat exchanger, a precooling mixed refrigerant refrigerating cycle mechanism and a liquefying mixed refrigerant refrigerating cycle mechanism. The precooling portion of the dual-mixed-refrigerant liquefying system employs mixed refrigerants so as to be high in heat exchange efficiency compared with existing propane precooling process. Furthermore, the number of the heat exchangers is small and the flow structure is simple. The precooling heat exchanger and the copious cooling heat exchanger are both the wound tube heat exchangers so as to be strong in adaptability to severe operation work conditions and long in service life. The precooling heat exchange uses three stages of throttling so as to effectively reduce heat exchange power consumption compared with existing two stages of throttling. Low-temperature BOG can directly exchange heat with raw material gas so as to improve heat exchange efficiency compared with existing process using BOG and coolants to exchange heat.
Description
Technical field
The utility model relates to a kind of two azeotrope liquefaction systems that are applied to base lotus type natural gas liquefaction plant, belongs to the liquefaction Technology of Natural Gas field.
Background technology
Domestic common liquefaction Technology of Natural Gas mostly is nitrogen expansion and single-stage mixing cryogen circularly cooling technique at present, and the LNG device that the scale that can only be applicable to is less, adopt plate-fin heat exchanger usually, not high to high-pressure air source adaptability, and service life is shorter.Abroad the liquefaction process for the large-scale natural gas liquefaction plant adopts propane pre-cooling mix refrigerant liquefaction process (C3/MR) or two azeotrope refrigeration liquefying techniques (DMR) more, the former adopts movable tube sheets heat exchanger by (C3/MR) precool heat exchanger device usually, more for the heat exchanger quantity that the multiple flow heat exchange need to arrange, thus the flowage structure complexity caused; The pre-cold-peace deep-cooling heat exchanger of the latter (DMR) adopts the heat exchange of two-stage refrigeration more, and heat exchange efficiency is lower.In addition, external DMR technique adopts BOG deep cooling cryogen to carry out heat exchange usually, with unstripped gas, carries out heat exchange again after the throttling of cooled deep cooling cryogen, this process using BOG directly and unstripped gas heat exchange mode heat exchange efficiency lower.
The utility model content
The purpose of this utility model is to provide a kind of two azeotrope liquefaction systems that are applied to base lotus type natural gas liquefaction plant, the adaptability of the liquefaction system that the utility model provides is high, safe and reliable, stability is strong, considered the engineering application after large-scale wound tube heat exchanger domesticizes, reduce equipment investment cost, can improve the liquefying power of liquefaction process.
A kind of two azeotrope liquefaction systems that are applied to base lotus type natural gas liquefaction plant provided by the utility model, it comprises precool heat exchanger device, liquefaction heat exchanger, precooling azeotrope kind of refrigeration cycle mechanism and liquefaction azeotrope kind of refrigeration cycle mechanism;
Described precooling azeotrope kind of refrigeration cycle mechanism comprises surge tank I, one-level precooling cryogen compressor, precooling cryogen cooler I, gas-liquid separator I, secondary precooling cryogen compressor, precooling cryogen cooler II and the gas-liquid separator II be communicated with successively; Described surge tank I is connected with the bottom of described precool heat exchanger device; The liquid-phase outlet of described gas-liquid separator I is connected with the bottom of described precool heat exchanger device; The liquid-phase outlet of described gas-liquid separator II is connected with the bottom of described precool heat exchanger device;
The gaseous phase outlet of described gas-liquid separator II is connected with the bottom of described precool heat exchanger device by the pipeline I, and described pipeline I extends to the top of described precool heat exchanger device, then from described Base top contact, is connected with described precool heat exchanger device by throttling;
The liquid-phase outlet of described gas-liquid separator II is connected with the bottom of described precool heat exchanger device by the pipeline II, and described pipeline II extends to the middle part of described precool heat exchanger device, then from described middle part, draws by throttling and is connected with described precool heat exchanger device;
Described liquefaction azeotrope kind of refrigeration cycle mechanism comprises surge tank II, liquefaction cryogen compressor and the liquefaction cryogen cooler be communicated with successively; Described surge tank II is connected with the bottom of described precool heat exchanger device; The outlet of described liquefaction cryogen cooler is connected with the bottom of described precool heat exchanger device by the pipeline III, and described pipeline III is from being connected with the gas-liquid separator III after the Base top contact of described precool heat exchanger device; The gaseous phase outlet of described gas-liquid separator III is connected with the bottom of described liquefaction heat exchanger by the pipeline IV, and described pipeline IV extends to the top of described liquefaction heat exchanger, then from described Base top contact, is connected with described liquefaction heat exchanger by throttling; The liquid-phase outlet of described gas-liquid separator III is connected with the bottom of described liquefaction heat exchanger by the pipeline V, and described pipeline V extends to the middle part of described liquefaction heat exchanger, then from described middle part, draws by throttling and is connected with described liquefaction heat exchanger.
In above-mentioned two azeotrope liquefaction systems, described precool heat exchanger device and described liquefaction cooler all can be wound tube heat exchanger.
While using of the present utility model pair of azeotrope liquefaction system, at first the natural gas (refer to through desulfurization, decarburization, demercuration, dehydration after meet base lotus type natural gas liquefaction plant to enter the quality requirement of liquefaction unit natural gas) of pretreatment after qualified is after the precooling of precool heat exchanger device, entering the liquefaction heat exchanger further lowers the temperature, finally by celebrating a festival, flow to into LNG storage tank, in storage tank, the natural gas after for precooling provides cold to boil-off gas through heat exchanger.Pre-cold-peace liquefaction azeotrope provides cold by azeotrope compression, the pre-cold-peace liquefaction of cooling rear introducing heat exchanger for natural gas by compressor circulation system independently respectively.
The utility model is applicable to producing the LNG scale per year in the natural gas liquefaction plant more than 1,000,000 tons.
The utlity model has following advantage:
1, mix refrigerant is partly adopted in precooling, and existing propane pre-cooling technique heat exchange efficiency is higher, and the heat exchanger negligible amounts, and flowage structure is simple;
2, precool heat exchanger device and deep-cooling heat exchanger all adopt wound tube heat exchanger, and cope with bad operates the adaptable of operating mode, long service life;
3, precool heat exchanger adopts three grades of throttlings, and existing two-stage throttling effectively reduces the heat exchange power consumption; Low temperature BOG directly carries out heat exchange with unstripped gas, has technique now and adopts BOG and cryogen to carry out heat exchange to have improved heat exchange efficiency more.
The accompanying drawing explanation
The structural representation of two azeotrope liquefaction systems that Fig. 1 provides for the utility model.
Fig. 2 is the schematic diagram that the utility model is used state.
In figure, each mark is as follows: 1 precool heat exchanger device, 2 liquefaction heat exchangers, 3 surge tank I, 4 one-level precooling cryogen compressors, 5 precooling cryogen cooler I, 6 gas-liquid separator I, 7 secondary precooling cryogen compressors, 8 precooling cryogen cooler II, 9 gas-liquid separator II, 10 pipeline I, 11 pipeline II, 12 surge tank II, 13 liquefaction cryogen compressors, 14 liquefaction cryogen coolers, 15 pipeline III, 16 gas-liquid separator III, 17 pipeline IV, 18 pipeline V, 19 feed gas chiller.
The specific embodiment
Below in conjunction with accompanying drawing, the utility model is described further, but the utility model is not limited to following examples.
Embodiment 1,
As shown in Figure 1, two azeotrope liquefaction systems of providing of the utility model comprise precool heat exchanger device 1, liquefaction heat exchanger 2, precooling azeotrope kind of refrigeration cycle mechanism and liquefaction azeotrope kind of refrigeration cycle mechanism; Precool heat exchanger device 1 and liquefaction heat exchanger 2 are wound tube heat exchanger.Wherein precooling azeotrope kind of refrigeration cycle mechanism comprises surge tank I 3, one-level precooling cryogen compressor 4, precooling cryogen cooler I 5, gas-liquid separator I 6, secondary precooling cryogen compressor 7, precooling cryogen cooler II 8 and the gas-liquid separator II 9 be communicated with successively; This surge tank I 3 is connected with the bottom of precool heat exchanger device 1; The liquid-phase outlet of gas-liquid separator I 6 is connected with the bottom of precool heat exchanger device 1; The liquid-phase outlet of gas-liquid separator II 9 is connected with the bottom of precool heat exchanger device 1.The gaseous phase outlet of gas-liquid separator II 9 is connected with the bottom of precool heat exchanger device 1 by pipeline I 10, and this pipeline I 10 extends to the top of precool heat exchanger device 1, then from this Base top contact, is connected with precool heat exchanger device 1 by throttling; The liquid-phase outlet of gas-liquid separator II 9 is connected with the bottom of precool heat exchanger device 1 by pipeline II 11, and this pipeline II 11 extends to the middle part of precool heat exchanger device 1, then from this middle part, draws by throttling and is connected with precool heat exchanger device 1; The azeotrope kind of refrigeration cycle that wherein liquefies mechanism comprises surge tank II 12, liquefaction cryogen compressor 13 and the liquefaction cryogen cooler 14 be communicated with successively; This surge tank II 12 is connected with the bottom of precool heat exchanger device 1; The outlet of liquefaction cryogen cooler 14 is connected with the bottom of precool heat exchanger device 1 by pipeline III 15, and pipeline III 15 is from being connected with gas-liquid separator III 16 after the Base top contact of precool heat exchanger device 1; The gaseous phase outlet of this gas-liquid separator III 16 is connected with the bottom of liquefaction heat exchanger 2 by pipeline IV 17, and this pipeline IV 17 extends to the top of liquefaction heat exchanger 2, then from this Base top contact, is connected with liquefaction heat exchanger 2 by throttling; The liquid-phase outlet of gas-liquid separator III 16 is connected with the bottom of liquefaction heat exchanger 2 by pipeline V 18, and this pipeline V 18 extends to the middle part of liquefaction heat exchanger 2, then from this middle part, draws by throttling and is connected with liquefaction heat exchanger 2.
Use the raw natural gas liquefaction of above-mentioned liquefaction system to certain overseas certain gas field, feed gas composition is 98.68% methane, 0.33% ethene, 0.27% propane, butane 0.16%, iso-butane 0.22%, 0.11% isopentane, 0.11% pentane and 0.11% nitrogen.Wherein the precooling azeotrope is comprised of 13.86% methane, 40.39% ethane, 18.77% propane, 6.55% iso-butane, 6.11% butane and 14.31% isopentane; The liquefaction azeotrope is comprised of 42.86% methane, 41.07% ethane, 5.36% propane and 10.71% nitrogen, is mass fraction.Can carry out according to following step:
Natural gas (the 7.9MPag that pretreatment is qualified, 40 ℃) at first enter in precool heat exchanger device 1 and flow from bottom to top, after being cooled to-57 ℃, extracting out and be separated into two strands, wherein the cooling deutomerite of BOG heat exchange in one and LNG storage tank flow to 0.15MPag ,-160 ℃, another thigh enter in liquefaction heat exchanger 2, continue cooling, after being cooled to-150 ℃, extract throttling out to 0.15MPag ,-160 ℃, enter the LNG storage tank after these two strands of natural gases mix.
From the gas phase azeotrope after 1 heat exchange of precool heat exchanger device enter compressor (one-level precooling cryogen compressor 4 and secondary precooling cryogen compressor 7) through two stages of compression to 1.9MPag, enter cooler and be cooled to 40 ℃, through gas-liquid separator I 6, being divided into liquid phase flows respectively from bottom to top from bottom enters the heat exchanger tube of precool heat exchanger device 1, the liquid phase azeotrope returns to the shell side of precool heat exchanger device 1 after from the middle part of precool heat exchanger device 1, extracting throttling out, the gas phase azeotrope returns to heat exchanger shell pass after from the heat exchanger top, extracting throttling out, flow evaporation provides cold for precool heat exchanger device 1 from the top down respectively.Precooling cryogen after evaporation (0.19MPag, 34.25 ℃) enters compressor and carries out two stages of compression and cooling, completes a circulation.
From the gas phase azeotrope after 2 heat exchange of liquefaction heat exchanger, enter liquefaction cryogen compressor 13 and be compressed to 3.95MPag, after being cooled to 40 ℃, enter in precool heat exchanger device 1, be chilled in advance-57 ℃ and extract and be separated into liquid phase out, from entering the heat exchanger tube of liquefaction heat exchanger 2, the bottom of liquefaction heat exchanger 2 flows from bottom to top respectively, wherein the liquid phase azeotrope returns to the shell side of liquefaction heat exchanger 2 after from the middle part of liquefaction heat exchanger 2, extracting throttling out, the gas phase azeotrope returns to the shell side of liquefaction heat exchanger 2 after from the top of liquefaction heat exchanger 2, extracting throttling out, flow evaporation provides cold for heat exchanger from the top down respectively.Liquefaction cryogen (0.24MPag-64.38 ℃) after evaporation enters compressor and carries out two stages of compression and cooling, completes a circulation.
Embodiment 2,
The unstripped gas liquefaction of liquefaction system in use embodiment 1 to the third typical LNG component in GB19204,
Feed gas composition is methane 87.2%, ethane 8.61%, propane 2.74%, butane 0.65%, iso-butane 0.42%, pentane 0.02% and nitrogen 0.36%; The composition of precooling azeotrope used and liquefaction azeotrope.
Basic identical in concrete steps and embodiment 1, because in feed gas composition, heavy constituent increases, therefore the outlet of precooling azeotrope kind of refrigeration cycle mechanism need to remove the heavy hydrocarbon that condensation in unstripped gas goes out, and through calculating, the azeotrope component proportion of precooling, liquefaction unit needs to optimize.
Through in precooling azeotrope kind of refrigeration cycle mechanism unstripped gas, removing the heavy hydrocarbon amount, be 20t/h.In flow process, all the other parameters are identical with example 1, and the product liquefied fraction obtained is 91%.
Embodiment 3,
Use the liquefaction system in embodiment 1 to certain cold marine site, the raw natural gas of certain component to be liquefied, for cooling ocean temperature, it is 13 ℃, as shown in Figure 2, because the coolant media temperature is lower, at precool heat exchanger device 1 imported raw material gas, set up feed gas chiller 19 and unstripped gas has been carried out cooling, the cooler outlet temperature in precooling in addition, liquefaction azeotrope circulation is reduced to 25 ℃.
Feed gas composition is 98.68% methane, 0.33% ethene, 0.27% propane, butane 0.16%, iso-butane 0.22%, 0.11% isopentane, 0.11% pentane, 0.11% nitrogen.Main implementation step is as follows:
Natural gas (the 7.9MPag that pretreatment is qualified, 25 ℃) at first enter in precool heat exchanger device 1 and flow from bottom to top, after being cooled to-60 ℃, extracting out and be separated into two strands, wherein the cooling deutomerite of BOG heat exchange in one and LNG storage tank flow to 0.15MPag ,-160 ℃, another thigh enter in liquefaction heat exchanger 2, continue cooling, after being cooled to-150 ℃, extract throttling out to 0.15MPag ,-160 ℃, enter the LNG storage tank after these two strands of natural gases mix.
From the gas phase azeotrope after 1 heat exchange of precool heat exchanger device enter compressor (one-level precooling cryogen compressor 4 and secondary precooling cryogen compressor 7) through two stages of compression to 1.9MPag, enter cooler and be cooled to 25 ℃, through gas-liquid separator I 6, being divided into liquid phase flows respectively from bottom to top from bottom enters the heat exchanger tube of precool heat exchanger device 1, the liquid phase cryogen returns to heat exchanger shell pass after from precool heat exchanger device 1 middle part, extracting throttling out, the gas phase cryogen returns to heat exchanger shell pass after from precool heat exchanger device 1 top, extracting throttling out, and flow evaporation provides cold for heat exchanger from the top down respectively.Precooling cryogen after evaporation (0.19MPag, 22.06 ℃) enters compressor and carries out two stages of compression and cooling, completes a circulation.
From the gas phase cryogen after 2 heat exchange of liquefaction heat exchanger, enter liquefaction cryogen compressor 13 and be compressed to 3.95MPag, after being cooled to 25 ℃, enter precool heat exchanger device 1, be chilled in advance-60 ℃ and extract and be separated into liquid phase out, from entering the heat exchanger tube of liquefaction heat exchanger 2, bottom flows from bottom to top respectively, the liquid phase cryogen returns to heat exchanger shell pass after from liquefaction heat exchanger 2 middle parts, extracting throttling out, the gas phase cryogen returns to heat exchanger shell pass after from liquefaction heat exchanger 2 tops, extracting throttling out, and flow evaporation provides cold for heat exchanger from the top down respectively.Liquefaction cryogen (0.24MPag-62.98 ℃) after evaporation enters compressor and carries out two stages of compression and cooling, completes a circulation.
The precooling azeotrope that this embodiment adopts is comprised of 2.5% methane, 47.9% ethane, 22.7% propane, 6.25% iso-butane, 6.25% butane and 14.4% isopentane; The liquefaction azeotrope is comprised of 42.6% methane, 39.7% ethane, 4.0% propane and 13.7% nitrogen.
Claims (2)
1. two azeotrope liquefaction systems that are applied to base lotus type natural gas liquefaction plant is characterized in that: described liquefaction system comprises precool heat exchanger device, liquefaction heat exchanger, precooling azeotrope kind of refrigeration cycle mechanism and liquefaction azeotrope kind of refrigeration cycle mechanism;
Described precooling azeotrope kind of refrigeration cycle mechanism comprises surge tank I, one-level precooling cryogen compressor, precooling cryogen cooler I, gas-liquid separator I, secondary precooling cryogen compressor, precooling cryogen cooler II and the gas-liquid separator II be communicated with successively; Described surge tank I is connected with the bottom of described precool heat exchanger device; The liquid-phase outlet of described gas-liquid separator I is connected with the bottom of described precool heat exchanger device; The liquid-phase outlet of described gas-liquid separator II is connected with the bottom of described precool heat exchanger device;
The gaseous phase outlet of described gas-liquid separator II is connected with the bottom of described precool heat exchanger device by the pipeline I, and described pipeline I extends to the top of described precool heat exchanger device, then from described Base top contact, is connected with described precool heat exchanger device by throttling;
The liquid-phase outlet of described gas-liquid separator II is connected with the bottom of described precool heat exchanger device by the pipeline II, and described pipeline II extends to the middle part of described precool heat exchanger device, then from described middle part, draws by throttling and is connected with described precool heat exchanger device;
Described liquefaction azeotrope kind of refrigeration cycle mechanism comprises surge tank II, liquefaction cryogen compressor and the liquefaction cryogen cooler be communicated with successively; Described surge tank II is connected with the bottom of described precool heat exchanger device; The outlet of described liquefaction cryogen cooler is connected with the bottom of described precool heat exchanger device by the pipeline III, and described pipeline III is from being connected with the gas-liquid separator III after the Base top contact of described precool heat exchanger device; The gaseous phase outlet of described gas-liquid separator III is connected with the bottom of described liquefaction heat exchanger by the pipeline IV, and described pipeline IV extends to the top of described liquefaction heat exchanger, then from described Base top contact, is connected with described liquefaction heat exchanger by throttling; The liquid-phase outlet of described gas-liquid separator III is connected with the bottom of described liquefaction heat exchanger by the pipeline V, and described pipeline V extends to the middle part of described liquefaction heat exchanger, then from described middle part, draws by throttling and is connected with described liquefaction heat exchanger.
2. according to claim 1 pair of azeotrope liquefaction system, it is characterized in that: described precool heat exchanger device and described liquefaction cooler are wound tube heat exchanger.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2013202310164U CN203310202U (en) | 2013-05-02 | 2013-05-02 | Dual-mixed-refrigerant liquefying system applied to base load type natural gas liquefaction factory |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2013202310164U CN203310202U (en) | 2013-05-02 | 2013-05-02 | Dual-mixed-refrigerant liquefying system applied to base load type natural gas liquefaction factory |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN203310202U true CN203310202U (en) | 2013-11-27 |
Family
ID=49616406
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2013202310164U Expired - Lifetime CN203310202U (en) | 2013-05-02 | 2013-05-02 | Dual-mixed-refrigerant liquefying system applied to base load type natural gas liquefaction factory |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN203310202U (en) |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103234326A (en) * | 2013-05-02 | 2013-08-07 | 中国海洋石油总公司 | Double-mixed-refrigerant liquefying system applied to base-load type natural gas liquefying plant |
| 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 |
| CN108775770A (en) * | 2018-05-30 | 2018-11-09 | 科霖恩新能源科技（江苏）有限公司 | A kind of brazing plate type heat exchanger natural gas liquefaction system using mixed-refrigerant cycle |
| CN110044131A (en) * | 2019-05-06 | 2019-07-23 | 郑州轻工业学院 | A kind of multi-stage compression propane pre-cooling natural gas liquefaction system and its liquifying method |
-
2013
- 2013-05-02 CN CN2013202310164U patent/CN203310202U/en not_active Expired - Lifetime
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103234326A (en) * | 2013-05-02 | 2013-08-07 | 中国海洋石油总公司 | Double-mixed-refrigerant liquefying system applied to base-load type natural gas liquefying plant |
| CN103234326B (en) * | 2013-05-02 | 2015-11-25 | 中国海洋石油总公司 | Be applied to two azeotrope liquefaction systems of base lotus type natural gas liquefaction plant |
| 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 |
| CN108775770A (en) * | 2018-05-30 | 2018-11-09 | 科霖恩新能源科技（江苏）有限公司 | A kind of brazing plate type heat exchanger natural gas liquefaction system using mixed-refrigerant cycle |
| CN110044131A (en) * | 2019-05-06 | 2019-07-23 | 郑州轻工业学院 | A kind of multi-stage compression propane pre-cooling natural gas liquefaction system and its liquifying method |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN202371968U (en) | Boil-off gas liquefaction recovery device for liquefied natural gas receiving station | |
| CN101858683A (en) | System for producing liquefied natural gas by utilizing liquid nitrogen cold energy | |
| CN103363778B (en) | Minitype skid-mounted single-level mixed refrigerant natural gas liquefaction system and method thereof | |
| CN101625190A (en) | Mixed refrigerant re-circulated liquefaction process for precooling coalbed methane (CBM) by residual pressure of pressure swing adsorption (PSA) | |
| CN105444523A (en) | Reliquefaction system and technique for compressing expanded liquified BOG through BOG | |
| CN102538390B (en) | Novel natural gas liquefaction system and natural gas liquefaction method | |
| CN102538391B (en) | Multi-level single-component refrigeration natural gas liquefaction system and multi-level single-component refrigeration natural gas liquefaction method | |
| CN203310202U (en) | Dual-mixed-refrigerant liquefying system applied to base load type natural gas liquefaction factory | |
| CN102564059A (en) | Twin-stage multi-component mixed refrigerant refrigeration natural gas liquefaction system and method | |
| CN102927791A (en) | Dual compounding cryogen refrigeration system with a precooling function and method | |
| CN102748918A (en) | Natural gas liquefying system by vurtue of double-stage mixed-refrigerant circulation | |
| CN202813975U (en) | Unconventional natural gas liquefaction system based on winding tubular heat exchanger | |
| CN216620451U (en) | LNG reforming hydrogen production and LNG cold energy liquefied hydrogen integrated system | |
| CN102628634B (en) | Ternary-cycle cascade refrigeration natural gas liquefaction system and method thereof | |
| CN102564057A (en) | Propane pre-cooling mixed refrigerant liquefaction system applied to base-load type natural gas liquefaction factory | |
| CN100441990C (en) | Small-scaled natural gas liquification device using air separation refrigeration system | |
| CN103175379B (en) | Utilize pipeline pressure can prepare device and the using method of liquefied natural gas | |
| CN104019626B (en) | The cold method and device preparing liquefied natural gas of a kind of azeotrope two-stage system | |
| CN102620460B (en) | Hybrid refrigeration cycle system and method with propylene pre-cooling | |
| CN102653692A (en) | Method for preparing liquefied natural gas from coke oven gas | |
| CN101614464A (en) | Method for liquefying natural gas through double-expansion of high-temperature and low-temperature nitrogen gas | |
| CN102645084B (en) | Method and device for preparing liquefied natural gas by using mixed refrigerant three-level refrigeration | |
| CN106500458B (en) | Pre-cooling type natural gas liquefaction process and system | |
| CN102564061B (en) | Two-stage mixed refrigerant circulation liquefaction system applied to base load type natural gas liquefaction factory | |
| CN202692600U (en) | Two-stage mixing refrigerant cycle gas liquification system |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| AV01 | Patent right actively abandoned |
Granted publication date: 20131127 Effective date of abandoning: 20151125 |
|
| AV01 | Patent right actively abandoned |
Granted publication date: 20131127 Effective date of abandoning: 20151125 |
|
| C25 | Abandonment of patent right or utility model to avoid double patenting |