CN105486034B - A kind of natural gas liquefaction and lighter hydrocarbons isolation integral integrated technique system and technique - Google Patents
A kind of natural gas liquefaction and lighter hydrocarbons isolation integral integrated technique system and technique Download PDFInfo
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- CN105486034B CN105486034B CN201610006986.2A CN201610006986A CN105486034B CN 105486034 B CN105486034 B CN 105486034B CN 201610006986 A CN201610006986 A CN 201610006986A CN 105486034 B CN105486034 B CN 105486034B
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- main heat
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- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 title claims abstract description 120
- 239000003345 natural gas Substances 0.000 title claims abstract description 43
- 229930195733 hydrocarbon Natural products 0.000 title claims abstract description 39
- 150000002430 hydrocarbons Chemical class 0.000 title claims abstract description 39
- 238000000034 method Methods 0.000 title claims abstract description 38
- 238000002955 isolation Methods 0.000 title claims abstract description 17
- 238000005201 scrubbing Methods 0.000 claims abstract description 112
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 claims abstract description 70
- 238000010992 reflux Methods 0.000 claims abstract description 67
- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 claims abstract description 51
- 239000001294 propane Substances 0.000 claims abstract description 35
- 239000007789 gas Substances 0.000 claims abstract description 31
- 239000007788 liquid Substances 0.000 claims abstract description 27
- 239000012071 phase Substances 0.000 claims abstract description 24
- 239000001273 butane Substances 0.000 claims abstract description 22
- OFBQJSOFQDEBGM-UHFFFAOYSA-N n-pentane Natural products CCCCC OFBQJSOFQDEBGM-UHFFFAOYSA-N 0.000 claims abstract description 22
- 238000000926 separation method Methods 0.000 claims abstract description 22
- IJDNQMDRQITEOD-UHFFFAOYSA-N n-butane Chemical compound CCCC IJDNQMDRQITEOD-UHFFFAOYSA-N 0.000 claims abstract description 21
- 238000004519 manufacturing process Methods 0.000 claims abstract description 19
- 239000007791 liquid phase Substances 0.000 claims abstract description 14
- 238000002156 mixing Methods 0.000 claims abstract description 8
- 238000000605 extraction Methods 0.000 claims abstract description 7
- 239000007792 gaseous phase Substances 0.000 claims abstract description 7
- 239000003507 refrigerant Substances 0.000 claims description 24
- 238000001816 cooling Methods 0.000 claims description 16
- 239000000203 mixture Substances 0.000 claims description 14
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 12
- 239000000463 material Substances 0.000 claims description 8
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 claims description 6
- 229910052782 aluminium Inorganic materials 0.000 claims description 6
- 238000005219 brazing Methods 0.000 claims description 6
- 238000005516 engineering process Methods 0.000 claims description 6
- 229910052757 nitrogen Inorganic materials 0.000 claims description 6
- 235000019628 coolness Nutrition 0.000 claims description 3
- 238000002347 injection Methods 0.000 claims description 3
- 239000007924 injection Substances 0.000 claims description 3
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 claims 1
- 239000003795 chemical substances by application Substances 0.000 claims 1
- 210000000038 chest Anatomy 0.000 description 110
- 239000000047 product Substances 0.000 description 38
- 239000004215 Carbon black (E152) Substances 0.000 description 19
- 238000005057 refrigeration Methods 0.000 description 10
- 238000005265 energy consumption Methods 0.000 description 7
- 150000001335 aliphatic alkanes Chemical class 0.000 description 5
- 238000012946 outsourcing Methods 0.000 description 4
- 239000000243 solution Substances 0.000 description 4
- 239000013589 supplement Substances 0.000 description 4
- 238000005406 washing Methods 0.000 description 4
- 238000007599 discharging Methods 0.000 description 3
- 230000009286 beneficial effect Effects 0.000 description 2
- 230000033228 biological regulation Effects 0.000 description 2
- 230000005540 biological transmission Effects 0.000 description 2
- 230000003139 buffering effect Effects 0.000 description 2
- 230000006835 compression Effects 0.000 description 2
- 238000007906 compression Methods 0.000 description 2
- 238000004821 distillation Methods 0.000 description 2
- 238000005457 optimization Methods 0.000 description 2
- 238000004781 supercooling Methods 0.000 description 2
- 208000033760 Device operational issues Diseases 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 230000018044 dehydration Effects 0.000 description 1
- 238000006297 dehydration reaction Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 239000007921 spray Substances 0.000 description 1
- 230000006641 stabilisation Effects 0.000 description 1
- 238000011105 stabilization Methods 0.000 description 1
- 238000003860 storage Methods 0.000 description 1
- 238000006467 substitution reaction Methods 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
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/0204—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the feed stream
- F25J3/0209—Natural gas or substitute 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
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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
- F25J1/003—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
-
- 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
- F25J1/0239—Purification or treatment step being integrated between two refrigeration cycles of a refrigeration cascade, i.e. first cycle providing feed gas cooling and second cycle providing overhead gas cooling
- F25J1/0241—Purification or treatment step being integrated between two refrigeration cycles of a refrigeration cascade, i.e. first cycle providing feed gas cooling and second cycle providing overhead gas cooling wherein the overhead cooling comprises providing reflux for a fractionation step
-
- 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
- F25J2200/00—Processes or apparatus using separation by rectification
- F25J2200/10—Processes or apparatus using separation by rectification in a quadruple, or more, column or pressure 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
- 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
Abstract
The present invention discloses a kind of natural gas liquefaction and lighter hydrocarbons isolation integral integrated technique system and technique, and the technique includes：Gas-liquid two-phase is extracted out from main heat exchange ice chest after natural gas is pre-cooled enters scrubbing tower, top gaseous phase is cooled down into main heat exchange ice chest, scrubbed tower return tank carries out gas-liquid separation again, and liquid phase is sent into scrubbing tower and provides cold reflux for scrubbing tower, and gas phase then returns to main heat exchange ice chest liquefaction stages；Enter dethanizer after scrubbing tower bottom of towe stream stock-traders' know-how expenditure and pressure, deethanizer overhead gas phase cools down into main heat exchange ice chest precooling zone, again gas-liquid separation is carried out through deethanizer reflux tank, on the one hand low temperature liquid phase ethane provides cold reflux for dethanizer, on the one hand stored using part extraction as ethane cryogen, remaining part delivers to main heat exchange ice chest liquefaction stages by pump pressurization；Propane and butane are pressurized through propane pump and butane pump respectively, and ice chest is delivered to after mixing, is extracted out after pre-cooled, methane and ethane stream stock is incorporated to after throttling, are returned again to main heat exchange ice chest and are together liquefied production LNG.
Description
Technical field
The present invention relates to the liquefaction of the hydrocarbon gas rich in methane and lighter hydrocarbons isolation integral integrated technique, more particularly to
Natural gas liquefaction is removed with condensate and the process system and method for ethane/propane cryogen production.
Background technology
Existing hydrocarbon isolation technics (patent CN 103031169), extracted out after raw natural gas is pre-cooled from main heat exchange ice chest,
Heavy hydrocarbon separation is carried out using heavy hydrocarbon knockout drum, isolates the heavier component such as propane, butane；It is or directly right using heavy hydrocarbon scrubbing tower
Raw natural gas carries out washing removing heavy hydrocarbon, and unstripped gas enters from bottom of towe, heavy hydrocarbon cleaning solution sprays from tower top, after removing heavy hydrocarbon
Gas phase enters back into main heat exchange ice chest and liquefied.First method separates hydrocarbon, and weight component separation degree is low, need to set heavy hydrocarbon again
Stabilization works solves heavy hydrocarbon storage problem, and can not produce cryogen；Second method, the direct washing material gas of scrubbing tower are right
The larger pressure loss can be caused in high pressure feed, causes natural gas liquefaction energy consumption can significant increase.
In addition, there is a kind of preposition light hydrocarbon separating method now.In natural gas by depickling, dehydration, demercuration purified treatment
Afterwards, by itself expansion/throttling refrigeration, domethanizing column carries out input and output material heat exchange, is pressurizeed again again after methane separation and is sent to liquefaction
Unit, heavier component enter back into downstream deethanization, depropanizing tower and debutanizing tower and carry out depth hydrocarbon separation.This method long flow path,
Equipment is more, control is complicated.
The content of the invention
The present invention provides a kind of natural gas liquefaction and lighter hydrocarbons isolation integral integrated technique system and technique, existing to overcome
There is the problems such as long flow path in technology, equipment are more, control is complicated.
To reach above-mentioned purpose, the invention provides a kind of natural gas liquefaction and lighter hydrocarbons isolation integral integrated technique system
System, including：MR1 chilldown systems equipment, MR2 liquefaction systems equipment, scrubber system equipment, dethanizer system equipment, de- third
Alkane Tower System equipment, debutanizing tower system equipment and the equipment of raw natural gas side, wherein：
MR1 chilldown system equipment includes：Centrifugal MR1 refrigerant compressors, the first compressor outlet cooler/cascade EDFA
Device, the first surge tank, first throttle valve or the first expanding machine, the first knockout drum；
MR2 liquefaction system equipment includes：Centrifugal MR2 refrigerant compressors, the second compressor outlet cooler/cascade EDFA
Device, the second surge tank, second throttle or the second expanding machine, the second knockout drum；
The equipment of raw natural gas side includes：Main heat exchange ice chest, scrubbing tower, scrubbing tower return tank, ethane return to pump, LPG
Return to pump, the 3rd choke valve or the 3rd expanding machine；
Scrubber system equipment includes：Scrubbing tower, scrubbing tower return tank, scrubbing tower reflux pump, scrubbing tower reboiler, the 4th
Choke valve or the 4th expanding machine；
Deethanization system equipment includes：Dethanizer, deethanizer reflux tank, deethanizer reflux pump, dethanizer are again
Boil device, ethane re-injection pump/product drawing pump, the 5th choke valve or the 5th expanding machine；
Depropanization system equipment includes：Depropanizing tower, depropanizing tower cooler, depropanizing tower return tank, depropanizing tower return
Flow pump, depropanizing tower reboiler, the 6th choke valve or the 6th expanding machine；
Debutanization system equipment includes：Debutanizing tower, debutanizing tower cooler, debutanizing tower return tank, debutanizing tower return
Flow pump, debutanizing tower reboiler, debutanizing tower bottom of towe cooler, the 7th choke valve or the 7th expanding machine；
Wherein, MR1 deep coolings refrigerant cycle loop includes flowing through MR1 compressors, MR1 condensers, MR1 outlets buffering successively
Tank, MR1 subcoolers, ice chest, first throttle valve return again to time of ice chest, two sections of entrance knockout drums of MR1 compressors, MR1 compressors
Road, and flow through MR1 compressors, MR1 condensers, MR1 outlets surge tank, MR1 subcoolers, ice chest, second throttle and return again to
Ice chest, one section of entrance knockout drum of MR1 compressors, the loop of MR1 compressors；
MR2 deep cooling refrigerant cycles loop includes flowing through MR2 compressors, MR2 compressor aftercoolers, ice chest, MR2 gas successively
Liquid knockout drum returns again to ice chest, the 3rd choke valve, ice chest, MR2 suctions port of compressor knockout drum, the loop of MR2 compressors, Yi Jiyi
Secondary MR2 compressors, MR2 compressor aftercoolers, ice chest, the MR2 knockout drums of flowing through returns again to ice chest, the 4th choke valve, cold
Case, MR2 suctions port of compressor knockout drum, the loop of MR2 compressors；
Lighter hydrocarbons separating technology path includes ice chest, scrubbing tower, dethanizer, depropanizing tower, the depropanizing tower being sequentially connected
Tower top cooler, depropanizing tower return tank, depropanizing tower reflux pump, the path of depropanizing tower, the ice chest being sequentially connected, washing
Tower, dethanizer, depropanizing tower, depropanizing tower tower top cooler, depropanizing tower return tank, depropanizing tower reflux pump, ice chest
Path, the ice chest being sequentially connected, scrubbing tower, dethanizer, depropanizing tower, debutanizing tower, the path of condensate reactor product cooler,
The ice chest that is sequentially connected, scrubbing tower, dethanizer, depropanizing tower, debutanizing tower, the path of condensate reactor product cooler, successively
Connected ice chest, scrubbing tower, dethanizer, depropanizing tower, debutanizing tower, debutanizing tower tower top cooler, debutanizing tower backflow
Tank, debutanizing tower reflux pump, the path of debutanizing tower, the ice chest being sequentially connected, scrubbing tower, dethanizer, depropanizing tower, de- fourth
Alkane tower, debutanizing tower tower top cooler, debutanizing tower return tank, debutanizing tower reflux pump, the path of ice chest, what is be sequentially connected is cold
Case, scrubbing tower, dethanizer, ice chest, deethanizer reflux tank, deethanizer reflux pump, the path of dethanizer, are sequentially connected
Ice chest, scrubbing tower, dethanizer, ice chest, deethanizer reflux tank, ethane delivery pump, the path of ice chest or holding vessel, successively
Connected ice chest, scrubbing tower, ice chest, scrubbing tower return tank, scrubbing tower reflux pump, the path of scrubbing tower, and be sequentially connected
Ice chest, scrubbing tower, ice chest, scrubbing tower return tank, ice chest, the path of LNG product holding vessel；
Gas-liquid two-phase is extracted out from main heat exchange ice chest after natural gas is pre-cooled enters scrubbing tower, and it is cold that top gaseous phase enters main heat exchange
Case is cooled down, then scrubbed tower return tank carries out gas-liquid separation, and liquid phase is sent into scrubbing tower and provides cold reflux, gas phase for scrubbing tower
Then return to main heat exchange ice chest liquefaction stages；
Enter dethanizer after scrubbing tower bottom of towe stream stock-traders' know-how expenditure and pressure, deethanizer overhead gas phase enters main heat exchange ice chest
Precooling zone cools down, then carries out gas-liquid separation through deethanizer reflux tank, on the one hand low temperature liquid phase ethane provides cold for dethanizer
Backflow, on the one hand stored using part extraction as ethane cryogen, remaining part delivers to main heat exchange ice chest liquefaction stages by pump pressurization；
Propane and butane are pressurized through propane pump and butane pump respectively, and main heat exchange ice chest is delivered to after mixing, is extracted out after pre-cooled,
Methane and ethane stream stock are incorporated to after throttling, return again to main heat exchange ice chest together liquefy production LNG.
Further, the main heat exchange ice chest uses vacuum brazing aluminum plate-fin heat exchanger.Can also be changed around tubular type
Hot device.
Further, the scrubbing tower operation with high pressure, pressure limit are 4.0~5.5MPaG.
Further, the MR1 azeotropes of the centrifugal MR1 refrigerant compressors and the centrifugal MR2 cryogens compression
The component of the MR2 azeotropes of machine is the mixture of methane, ethane, propane, two or more material in nitrogen.
Further, the pipe between the pipeline between the ice chest and scrubbing tower, the scrubbing tower and the dethanizer
The pipeline between pipeline, the depropanizing tower and the debutanizing tower between line, the dethanizer and the depropanizing tower,
Between pipeline, the depropanizing tower reflux pump and the ice chest between the debutanizing tower and the condensate reactor product cooler
Pipeline, the pipeline between the deethanizer reflux pump and the ice chest and the ice chest and the LNG product holding vessel
Between pipeline on be respectively arranged with control valve.
To reach above-mentioned purpose, present invention also offers one kind to be used for above-mentioned natural gas liquefaction and lighter hydrocarbons isolation integral collection
Into the technique of process system, comprise the following steps：
Gas-liquid two-phase is extracted out from main heat exchange ice chest after natural gas is pre-cooled enters scrubbing tower, and it is cold that top gaseous phase enters main heat exchange
Case is cooled down, then scrubbed tower return tank carries out gas-liquid separation, and liquid phase is sent into scrubbing tower and provides cold reflux, gas phase for scrubbing tower
Then return to main heat exchange ice chest liquefaction stages；
Enter dethanizer after scrubbing tower bottom of towe stream stock-traders' know-how expenditure and pressure, deethanizer overhead gas phase enters main heat exchange ice chest
Precooling zone cools down, then carries out gas-liquid separation through deethanizer reflux tank, on the one hand low temperature liquid phase ethane provides cold for dethanizer
Backflow, on the one hand stored using part extraction as ethane cryogen, remaining part delivers to main heat exchange ice chest liquefaction stages by pump pressurization；
Propane and butane are pressurized through propane pump and butane pump respectively, and ice chest is delivered to after mixing, is extracted out after pre-cooled, after throttling
Be incorporated to methane and ethane stream stock, return again to main heat exchange ice chest together liquefy production LNG.
Further, the main heat exchange ice chest uses vacuum brazing aluminum plate-fin heat exchanger.
Further, the scrubbing tower operation with high pressure, pressure limit are 4.0~5.5MPaG.
Further, the MR1 azeotropes of the centrifugal MR1 refrigerant compressors and the centrifugal MR2 cryogens compression
The component of the MR2 azeotropes of machine is the mixture of methane, ethane, propane, two or more material in nitrogen.
The invention provides the process system that the refrigeration natural gas liquefaction of solution azeotrope and lighter hydrocarbons isolation integral are integrated
And method, it is adapted to various Natural Gas Types, such as gas of gas reservoir, condensate gas, shale gas, coal bed gas, associated gas, avoids heavy hydrocarbon
Freeze to block Cryo Equipment, pipeline, valve, cause device operational issue or LNG product unqualified.Moreover, it is achieved that in production LNG
Cryogen ethane and propane (factory is personal or as international sale) and production LPG products are produced in product process simultaneously.
Brief description of the drawings
In order to illustrate more clearly about the embodiment of the present invention or technical scheme of the prior art, below will be to embodiment or existing
There is the required accompanying drawing used in technology description to be briefly described, it should be apparent that, drawings in the following description are only this
Some embodiments of invention, for those of ordinary skill in the art, on the premise of not paying creative work, can be with
Other accompanying drawings are obtained according to these accompanying drawings.
Fig. 1 is natural gas liquefaction and the lighter hydrocarbons isolation integral integrated technique system schematic of one embodiment of the invention.
Brief description of the drawings：
1-MR1 compressors, 2-MR1 condensers, 3-MR1 outlets surge tank, 4-MR1 quickly cooling units, one section of 5-MR1 compressors enter
Mouth knockout drum, two sections of entrance knockout drums of 6-MR1 compressors, 7-MR2 compressors, 8-MR2 compressor aftercoolers, 9-MR2 gas-liquids
Knockout drum, 10-MR2 suctions port of compressor knockout drum, 11- ice chests (plate-fin heat exchanger), 12- scrubbing towers (domethanizing column), 13- is washed
Wash tower reboiler, 14- scrubbing tower return tanks, 15- scrubbing tower reflux pumps, 16- dethanizers, 17- deethanizer reboilers, 18-
Deethanizer reflux tank, 19- deethanizer reflux pumps, 20- ethane delivery pumps, 21- depropanizing towers, 22- depropanizing tower reboilers,
23- depropanizing tower tower top coolers, 24- depropanizing tower return tanks, 25- depropanizing tower reflux pumps, 26- debutanizing towers, 27- take off fourth
Alkane tower reboiler, 28- debutanizing tower coolers, 29- debutanizing tower return tanks, 30- debutanizing tower reflux pumps, the production of 31- condensates
Product cooler, 32- first throttle valves (J-T valves), 33- second throttle (J-T valves), the choke valves of 34- the 3rd (J-T valves), 35-
Four choke valves (J-T valves), the controllers of 36- first, the control valves of 37- second, the control valves of 38- the 3rd, the control valves of 39- the 4th, 40-
Five control valves, the control valves of 41- the 6th, the control valves of 42- the 7th, the control valves of 43- the 8th, the control valves of 44- the 9th.
Embodiment
Below in conjunction with the accompanying drawing in the embodiment of the present invention, the technical scheme in the embodiment of the present invention is carried out clear, complete
Site preparation describes, it is clear that described embodiment is only part of the embodiment of the present invention, rather than whole embodiments.It is based on
Embodiment in the present invention, those of ordinary skill in the art are obtained every other under the premise of creative work is not paid
Embodiment, belong to the scope of protection of the invention.
Fig. 1 is natural gas liquefaction and the lighter hydrocarbons isolation integral integrated technique system schematic of one embodiment of the invention.
As illustrated, natural gas liquefaction includes with lighter hydrocarbons isolation integral integrated technique system：MR1 chilldown systems equipment, MR2 liquefaction system
System equipment, scrubber system equipment, dethanizer system equipment, depropanizing tower system equipment, debutanizing tower system equipment and original
Expect the equipment of natural gas side, wherein：
MR1 chilldown system equipment includes：Centrifugal MR1 refrigerant compressors, the first compressor outlet cooler/cascade EDFA
Device, the first surge tank, first throttle valve or the first expanding machine, the first knockout drum；
MR2 liquefaction system equipment includes：Centrifugal MR2 refrigerant compressors, the second compressor outlet cooler/cascade EDFA
Device, the second surge tank, second throttle or the second expanding machine, the second knockout drum；
The equipment of raw natural gas side includes：Main heat exchange ice chest, scrubbing tower, scrubbing tower return tank, ethane return to pump, LPG
Return to pump, the 3rd choke valve or the 3rd expanding machine；
Scrubber system equipment includes：Scrubbing tower, scrubbing tower return tank, scrubbing tower reflux pump, scrubbing tower reboiler, the 4th
Choke valve or the 4th expanding machine；
Deethanization system equipment includes：Dethanizer, deethanizer reflux tank, deethanizer reflux pump, dethanizer are again
Boil device, ethane re-injection pump/product drawing pump, the 5th choke valve or the 5th expanding machine；
Depropanization system equipment includes：Depropanizing tower, depropanizing tower cooler, depropanizing tower return tank, depropanizing tower return
Flow pump, depropanizing tower reboiler, the 6th choke valve or the 6th expanding machine；
Debutanization system equipment includes：Debutanizing tower, debutanizing tower cooler, debutanizing tower return tank, debutanizing tower return
Flow pump, debutanizing tower reboiler, debutanizing tower bottom of towe cooler, the 7th choke valve or the 7th expanding machine；
Wherein, MR1 deep coolings refrigerant cycle loop includes flowing through MR1 compressors, MR1 condensers, MR1 outlets buffering successively
Tank, MR1 subcoolers, ice chest, first throttle valve return again to time of ice chest, two sections of entrance knockout drums of MR1 compressors, MR1 compressors
Road, and flow through MR1 compressors, MR1 condensers, MR1 outlets surge tank, MR1 subcoolers, ice chest, second throttle and return again to
Ice chest, one section of entrance knockout drum of MR1 compressors, the loop of MR1 compressors；
MR2 deep cooling refrigerant cycles loop includes flowing through MR2 compressors, MR2 compressor aftercoolers, ice chest, MR2 gas successively
Liquid knockout drum returns again to ice chest, the 3rd choke valve, ice chest, MR2 suctions port of compressor knockout drum, the loop of MR2 compressors, Yi Jiyi
Secondary MR2 compressors, MR2 compressor aftercoolers, ice chest, the MR2 knockout drums of flowing through returns again to ice chest, the 4th choke valve, cold
Case, MR2 suctions port of compressor knockout drum, the loop of MR2 compressors；
Lighter hydrocarbons separating technology path includes ice chest, scrubbing tower, dethanizer, depropanizing tower, the depropanizing tower being sequentially connected
Tower top cooler, depropanizing tower return tank, depropanizing tower reflux pump, the path of depropanizing tower, the ice chest being sequentially connected, washing
Tower, dethanizer, depropanizing tower, depropanizing tower tower top cooler, depropanizing tower return tank, depropanizing tower reflux pump, ice chest
Path, the ice chest being sequentially connected, scrubbing tower, dethanizer, depropanizing tower, debutanizing tower, the path of condensate reactor product cooler,
The ice chest that is sequentially connected, scrubbing tower, dethanizer, depropanizing tower, debutanizing tower, the path of condensate reactor product cooler, successively
Connected ice chest, scrubbing tower, dethanizer, depropanizing tower, debutanizing tower, debutanizing tower tower top cooler, debutanizing tower backflow
Tank, debutanizing tower reflux pump, the path of debutanizing tower, the ice chest being sequentially connected, scrubbing tower, dethanizer, depropanizing tower, de- fourth
Alkane tower, debutanizing tower tower top cooler, debutanizing tower return tank, debutanizing tower reflux pump, the path of ice chest, what is be sequentially connected is cold
Case, scrubbing tower, dethanizer, ice chest, deethanizer reflux tank, deethanizer reflux pump, the path of dethanizer, are sequentially connected
Ice chest, scrubbing tower, dethanizer, ice chest, deethanizer reflux tank, ethane delivery pump, the path of ice chest or holding vessel, successively
Connected ice chest, scrubbing tower, ice chest, scrubbing tower return tank, scrubbing tower reflux pump, the path of scrubbing tower, and be sequentially connected
Ice chest, scrubbing tower, ice chest, scrubbing tower return tank, ice chest, the path of LNG product holding vessel；
(- 40~-60 DEG C) gas-liquid two-phase is extracted out from main heat exchange ice chest after natural gas is pre-cooled enters scrubbing tower, top gaseous phase
Cooled down into main heat exchange ice chest, then scrubbed tower return tank carries out gas-liquid separation, liquid phase is sent into scrubbing tower and carried for scrubbing tower
Cooling flows back, and gas phase then returns to main heat exchange ice chest liquefaction stages (≤- 45 DEG C)；
Enter dethanizer after scrubbing tower bottom of towe stream stock-traders' know-how expenditure and pressure, deethanizer overhead gas phase enters main heat exchange ice chest
Precooling zone cools down, then carries out gas-liquid separation through deethanizer reflux tank, on the one hand low temperature liquid phase ethane provides cold for dethanizer
Backflow, on the one hand stored using part extraction as ethane cryogen, remaining part delivers to main heat exchange ice chest liquefaction stages by pump pressurization；
Propane and butane are pressurized through propane pump and butane pump respectively, and ice chest is delivered to after mixing, is extracted out after pre-cooled, after throttling
Be incorporated to methane and ethane stream stock, return again to ice chest together liquefy production LNG (- 130~-160 DEG C).
In above-described embodiment, using Two-way Cycle azeotrope refrigeration system, there are two independent kind of refrigeration cycle MR1 and MR2,
Cold caused by MR1 kind of refrigeration cycle is used for cooling down MR2, raw natural gas and deethanization tower top return gas；MR2 kind of refrigeration cycle produces
Cold be used for liquefying raw natural gas, and provide cold for scrubbing tower (domethanizing column) cold reflux；Natural qi exhaustion hydrocarbon, which uses, to be washed
Tower (demethanation), dethanizer, depropanizing tower, debutanizing tower order rectifying are washed, the bottom of towe discharging of upper level tower is used as next stage
The charging of tower, centre is without heat exchange equipment；Scrubbing tower and the not individually designed cooler of deethanizer overhead, with main heat exchange ice chest
Carry out heat exchange matching.
For example, above-mentioned main heat exchange ice chest can use vacuum brazing aluminum plate-fin heat exchanger.It can also use around tubular type
Heat exchanger.
For example, above-mentioned scrubbing tower operates under high pressure, pressure limit is 4.0~5.5MPaG.
For example, the MR1 azeotropes of above-mentioned centrifugal MR1 refrigerant compressors and the MR2 of centrifugal MR2 refrigerant compressors are mixed
The component for closing cryogen can be the mixture of methane, ethane, propane, two or more material in nitrogen.
For example, pipeline, dethanizer and de- third between pipeline, scrubbing tower and dethanizer between ice chest and scrubbing tower
Between the pipeline between pipeline, depropanizing tower and debutanizing tower, debutanizing tower and condensate reactor product cooler between alkane tower
Pipeline between pipeline, deethanizer reflux pump and ice chest and ice chest between pipeline, depropanizing tower reflux pump and ice chest with
Control valve is respectively arranged with pipeline between LNG product holding vessel.
The above embodiment of the present invention realizes following beneficial effect：
Can be according to the composition of raw natural gas, temperature and pressure, ambient temperature, scrubbing tower (demethanation) using azeotrope
The proportioning of azeotrope is adjusted with factors such as deethanization refrigeration dutys, with determine be adapted to form and proportioning, so that it is determined that day
The cooling of right gas and condensing temperature, the separation temperature of heavy hydrocarbon, the composition of LNG product and temperature, matched with obtaining optimal cryogen,
The inlet and outlet pressure of refrigerant compressor so that efficiency highest, the energy consumption of refrigeration system are minimum, stable operation is reliable；
Scrubbing tower (demethanation), dethanizer, depropanizing tower, debutanizing tower order rectifying, the charging of optimization tower pressure and tower
Position, the discharging of tower bottom of towe is as without heat exchange, (saturation is fed or gas-liquid two-phase mixes after the charging throttling of next stage tower before realization
Close charging), process simplification simultaneously reduces the bottom of towe thermic load of each tower, so as to reduce overall system operation energy consumption；
Scrubbing tower operates (4.0~5.5MPaG) at elevated pressures, reduces the pressure loss of natural gas as far as possible, reduces day
Right gas returns to main heat exchange ice chest and carries out the required energy consumption that liquefies；
The cold reflux of scrubbing tower and the cold reflux of dethanizer are provided cold using azeotrope in main heat exchange ice chest
Measure, integrated heat exchange, heat transmission equipment quantity in reduction system；
Dethanizer supplements from tower top output ethane, ethane as azeotrope component, self-sufficient, nothing in realization device
Ethane cryogen outsourcing is needed, remaining low temperature ethane is pumped back into main heat exchange ice chest liquefaction area's production LNG product；
Depropanizing tower supplements from tower top output propane, propane as azeotrope component, self-sufficient, nothing in realization device
Need propane cryogen outsourcing；Remaining propane can mix with butane is used as LPG products, can also be pumped back into the production of main heat exchange ice chest
LNG product, increase LNG yield and regulation LNG product calorific value；
Debutanizing tower can also mix with propane separately as product from tower top output butane, butane and be used as LPG products, also
Main heat exchange ice chest can be pumped back into, methane and ethane stream stock are incorporated to after pre-cooled, the liquefaction supercooling production in main heat exchange ice chest
LNG product, play a part of increasing LNG yield and adjust LNG product calorific value；
Four tower hydrocarbon separation sequence distillation processes also remove condensate (C5 in addition to production ethane/propane cryogen and LPG products
+), natural gas is avoided in key equipments such as follow-up low-temperature liquefaction area frozen block main heat exchange ice chests, and reclaims a certain amount of condensate
(C5+) product.
It is adapted with said system embodiment, is separated present invention also offers one kind for above-mentioned natural gas liquefaction with lighter hydrocarbons
The technique of integrated process system, comprises the following steps：
Gas-liquid two-phase is extracted out from ice chest after natural gas is pre-cooled enters scrubbing tower, and top gaseous phase is carried out into main heat exchange ice chest
Cooling, then scrubbed tower return tank carry out gas-liquid separation, and liquid phase is sent into scrubbing tower and provides cold reflux for scrubbing tower, and gas phase then returns
Main heat exchange ice chest liquefaction stages；
Enter dethanizer after scrubbing tower bottom of towe stream stock-traders' know-how expenditure and pressure, deethanizer overhead gas phase enters main heat exchange ice chest
Precooling zone cools down, then carries out gas-liquid separation through deethanizer reflux tank, on the one hand low temperature liquid phase ethane provides cold for dethanizer
Backflow, on the one hand stored using part extraction as ethane cryogen, remaining part delivers to main heat exchange ice chest liquefaction stages by pump pressurization；
Propane and butane are pressurized through propane pump and butane pump respectively, and ice chest is delivered to after mixing, is extracted out after pre-cooled, after throttling
Be incorporated to methane and ethane stream stock, return again to main heat exchange ice chest together liquefy production LNG.
For example, above-mentioned main heat exchange ice chest can use vacuum brazing aluminum plate-fin heat exchanger.
For example, above-mentioned scrubbing tower operates under high pressure, pressure limit is 4.0~5.5MPaG.
For example, the MR1 azeotropes of above-mentioned centrifugal MR1 refrigerant compressors and the centrifugal MR2 refrigerant compressors
The component of MR2 azeotropes can be the mixture of methane, ethane, propane, two or more material in nitrogen.
The above embodiment of the present invention realizes following beneficial effect：
Can be according to the composition of raw natural gas, temperature and pressure, ambient temperature, scrubbing tower (demethanation) using azeotrope
The proportioning of azeotrope is adjusted with factors such as deethanization refrigeration dutys, with determine be adapted to form and proportioning, so that it is determined that day
The cooling of right gas and condensing temperature, the separation temperature of heavy hydrocarbon, the composition of LNG product and temperature, matched with obtaining optimal cryogen,
The inlet and outlet pressure of refrigerant compressor so that efficiency highest, the energy consumption of refrigeration system are minimum, stable operation is reliable；
Scrubbing tower (demethanation), dethanizer, depropanizing tower, debutanizing tower order rectifying, the charging of optimization tower pressure and tower
Position, the discharging of tower bottom of towe is as without heat exchange, (saturation is fed or gas-liquid two-phase mixes after the charging throttling of next stage tower before realization
Close charging), process simplification simultaneously reduces the bottom of towe thermic load of each tower, so as to reduce overall system operation energy consumption；
Scrubbing tower operates (4.0~5.5MPaG) at elevated pressures, reduces the pressure loss of natural gas as far as possible, reduces day
Right gas returns to main heat exchange ice chest and carries out the required energy consumption that liquefies；
The cold reflux of scrubbing tower and the cold reflux of dethanizer utilize the cold that azeotrope is provided in ice chest, integrate
Exchange heat, heat transmission equipment quantity in reduction system；
Dethanizer supplements from tower top output ethane, ethane as azeotrope component, self-sufficient, nothing in realization device
Ethane cryogen outsourcing is needed, remaining low temperature ethane is pumped back into main heat exchange ice chest liquefaction area's production LNG product；
Depropanizing tower supplements from tower top output propane, propane as azeotrope component, self-sufficient, nothing in realization device
Need propane cryogen outsourcing；Remaining propane can mix with butane is used as LPG products, can also be pumped back into the production of main heat exchange ice chest
LNG product, increase LNG yield and regulation LNG product calorific value；
Debutanizing tower can also mix with propane separately as product from tower top output butane, butane and be used as LPG products, also
Main heat exchange ice chest can be pumped back into, methane and ethane stream stock are incorporated to after pre-cooled, the liquefaction supercooling production in main heat exchange ice chest
LNG product, play a part of increasing LNG yield and adjust LNG product calorific value；
Four tower hydrocarbon separation sequence distillation processes also remove condensate (C5 in addition to production ethane/propane cryogen and LPG products
+), natural gas is avoided in key equipments such as follow-up low-temperature liquefaction area frozen block main heat exchange ice chests, and reclaims a certain amount of condensate
(C5+) product.
One of ordinary skill in the art will appreciate that：Accompanying drawing is the schematic diagram of one embodiment, module in accompanying drawing or
Flow is not necessarily implemented necessary to the present invention.
One of ordinary skill in the art will appreciate that：The module in device in embodiment can describe to divide according to embodiment
It is distributed in the device of embodiment, respective change can also be carried out and be disposed other than in one or more devices of the present embodiment.On
The module for stating embodiment can be merged into a module, can also be further split into multiple submodule.
Finally it should be noted that：The above embodiments are merely illustrative of the technical solutions of the present invention, rather than its limitations；Although
The present invention is described in detail with reference to the foregoing embodiments, it will be understood by those within the art that：It still may be used
To be modified to the technical scheme described in previous embodiment, or equivalent substitution is carried out to which part technical characteristic；And
These modifications are replaced, and the essence of appropriate technical solution is departed from the spirit and model of technical scheme of the embodiment of the present invention
Enclose.
Claims (8)
1. a kind of natural gas liquefaction and lighter hydrocarbons isolation integral integrated technique system, it is characterised in that including：MR1 chilldown systems
Equipment, MR2 liquefaction systems equipment, scrubber system equipment, dethanizer system equipment, depropanizing tower system equipment, debutanization
Tower System equipment and the equipment of raw natural gas side, wherein：
MR1 chilldown system equipment includes：Centrifugal MR1 refrigerant compressors, the first compressor outlet cooler/interstage cooler,
First surge tank, first throttle valve or the first expanding machine, the first knockout drum；
MR2 liquefaction system equipment includes：Centrifugal MR2 refrigerant compressors, the second compressor outlet cooler/interstage cooler,
Second surge tank, second throttle or the second expanding machine, the second knockout drum；
The equipment of raw natural gas side includes：Main heat exchange ice chest, scrubbing tower, scrubbing tower return tank, ethane returns to pump, LPG is returned
Pump, the 3rd choke valve or the 3rd expanding machine；
Scrubber system equipment includes：Scrubbing tower, scrubbing tower return tank, scrubbing tower reflux pump, scrubbing tower reboiler, the 4th throttling
Valve or the 4th expanding machine；
Deethanization system equipment includes：Dethanizer, deethanizer reflux tank, deethanizer reflux pump, deethanizer reboiler,
Ethane re-injection pump/product drawing pump, the 5th choke valve or the 5th expanding machine；
Depropanization system equipment includes：Depropanizing tower, depropanizing tower cooler, depropanizing tower return tank, depropanizing tower reflux pump,
Depropanizing tower reboiler, the 6th choke valve or the 6th expanding machine；
Debutanization system equipment includes：Debutanizing tower, debutanizing tower cooler, debutanizing tower return tank, debutanizing tower reflux pump,
Debutanizing tower reboiler, debutanizing tower bottom of towe cooler, the 7th choke valve or the 7th expanding machine；
Wherein, MR1 deep coolings refrigerant cycle loop includes flowing through MR1 compressors, MR1 condensers, MR1 outlets surge tank, MR1 successively
Subcooler, ice chest, first throttle valve return again to ice chest, two sections of entrance knockout drums of MR1 compressors, the loop of MR1 compressors, and
Flow through MR1 compressors, MR1 condensers, MR1 outlets surge tank, MR1 subcoolers, ice chest, second throttle and return again to ice chest, MR1
One section of entrance knockout drum of compressor, the loop of MR1 compressors；
MR2 deep cooling refrigerant cycles loop includes flowing through MR2 compressors, MR2 compressor aftercoolers, ice chest, MR2 gas-liquids point successively
From the loop that tank returns again to ice chest, the 3rd choke valve, ice chest, MR2 suctions port of compressor knockout drum, MR2 compressors, and flow successively
Through MR2 compressors, MR2 compressor aftercoolers, ice chest, MR2 knockout drums return again to ice chest, the 4th choke valve, ice chest,
MR2 suctions port of compressor knockout drum, the loop of MR2 compressors；
Lighter hydrocarbons separating technology path includes ice chest, scrubbing tower, dethanizer, depropanizing tower, the depropanizing tower tower top being sequentially connected
Cooler, depropanizing tower return tank, depropanizing tower reflux pump, the path of depropanizing tower, the ice chest being sequentially connected, scrubbing tower, take off
Ethane tower, depropanizing tower, depropanizing tower tower top cooler, depropanizing tower return tank, depropanizing tower reflux pump, the path of ice chest,
The ice chest that is sequentially connected, scrubbing tower, dethanizer, depropanizing tower, debutanizing tower, the path of condensate reactor product cooler, successively
Connected ice chest, scrubbing tower, dethanizer, depropanizing tower, debutanizing tower, the path of condensate reactor product cooler, are sequentially connected
Ice chest, scrubbing tower, dethanizer, depropanizing tower, debutanizing tower, debutanizing tower tower top cooler, debutanizing tower return tank, de-
Butane tower reflux pump, the path of debutanizing tower, the ice chest being sequentially connected, scrubbing tower, dethanizer, depropanizing tower, debutanizing tower,
Debutanizing tower tower top cooler, debutanizing tower return tank, debutanizing tower reflux pump, the path of ice chest, the ice chest being sequentially connected, are washed
Tower, dethanizer, ice chest, deethanizer reflux tank, deethanizer reflux pump, the path of dethanizer are washed, what is be sequentially connected is cold
Case, scrubbing tower, dethanizer, ice chest, deethanizer reflux tank, ethane delivery pump, the path of ice chest or holding vessel, are sequentially connected
Ice chest, scrubbing tower, ice chest, scrubbing tower return tank, scrubbing tower reflux pump, the path of scrubbing tower, and be sequentially connected ice chest,
Scrubbing tower, ice chest, scrubbing tower return tank, ice chest, the path of LNG product holding vessel；
Gas-liquid two-phase is extracted out from main heat exchange ice chest after natural gas is pre-cooled enters scrubbing tower, and top gaseous phase enters into main heat exchange ice chest
Row cooling, then scrubbed tower return tank carry out gas-liquid separation, and liquid phase is sent into scrubbing tower and provides cold reflux for scrubbing tower, and gas phase is then returned
Return main heat exchange ice chest liquefaction stages；
Enter dethanizer after scrubbing tower bottom of towe stream stock-traders' know-how expenditure and pressure, deethanizer overhead gas phase enters main heat exchange ice chest precooling
Section cooling, then gas-liquid separation is carried out through deethanizer reflux tank, on the one hand low temperature liquid phase ethane provides cold reflux for dethanizer,
On the one hand stored using part extraction as ethane cryogen, remaining part delivers to main heat exchange ice chest liquefaction stages by pump pressurization；
Propane and butane are pressurized through propane pump and butane pump respectively, and main heat exchange ice chest is delivered to after mixing, is extracted out after pre-cooled, throttling
After be incorporated to methane and ethane stream stock, return again to main heat exchange ice chest together liquefy production LNG；
The MR2 of the MR1 azeotropes of the centrifugal MR1 refrigerant compressors and centrifugal MR2 refrigerant compressors mixing is cold
The component of agent is the mixture of methane, ethane, propane, two or more materials in nitrogen.
2. natural gas liquefaction according to claim 1 and lighter hydrocarbons isolation integral integrated technique system, it is characterised in that institute
State main heat exchange ice chest and use vacuum brazing aluminum plate-fin heat exchanger.
3. natural gas liquefaction according to claim 1 and lighter hydrocarbons isolation integral integrated technique system, it is characterised in that institute
Scrubbing tower operation with high pressure is stated, pressure limit is 4.0~5.5MPaG.
4. natural gas liquefaction according to claim 1 and lighter hydrocarbons isolation integral integrated technique system, it is characterised in that institute
State pipeline, the dethanizer and the institute between pipeline between ice chest and scrubbing tower, the scrubbing tower and the dethanizer
State pipeline between pipeline between depropanizing tower, the depropanizing tower and the debutanizing tower, the debutanizing tower with it is described
The pipeline between pipeline, the depropanizing tower reflux pump and the ice chest, the deethanization between condensate reactor product cooler
Set respectively on the pipeline between pipeline and the ice chest and the LNG product holding vessel between tower reflux pump and the ice chest
It is equipped with control valve.
5. a kind of be used for natural gas liquefaction as claimed in claim 1 and the technique of lighter hydrocarbons isolation integral integrated technique system,
It is characterised in that it includes following steps：
Gas-liquid two-phase is extracted out from main heat exchange ice chest after natural gas is pre-cooled enters scrubbing tower, and top gaseous phase enters into main heat exchange ice chest
Row cooling, then scrubbed tower return tank carry out gas-liquid separation, and liquid phase is sent into scrubbing tower and provides cold reflux for scrubbing tower, and gas phase is then returned
Return main heat exchange ice chest liquefaction stages；
Enter dethanizer after scrubbing tower bottom of towe stream stock-traders' know-how expenditure and pressure, deethanizer overhead gas phase enters main heat exchange ice chest precooling
Section cooling, then gas-liquid separation is carried out through deethanizer reflux tank, on the one hand low temperature liquid phase ethane provides cold reflux for dethanizer,
On the one hand stored using part extraction as ethane cryogen, remaining part delivers to main heat exchange ice chest liquefaction stages by pump pressurization；
Propane and butane are pressurized through propane pump and butane pump respectively, and main heat exchange ice chest is delivered to after mixing, is extracted out after pre-cooled, throttling
After be incorporated to methane and ethane stream stock, return again to main heat exchange ice chest together liquefy production LNG.
6. technique according to claim 5, it is characterised in that the main heat exchange ice chest uses vacuum brazing aluminum plate-fin type
Heat exchanger.
7. technique according to claim 5, it is characterised in that the scrubbing tower operation with high pressure, pressure limit be 4.0~
5.5MPaG。
8. technique according to claim 5, it is characterised in that the MR1 azeotropes of the centrifugal MR1 refrigerant compressors
Component with the MR2 azeotropes of the centrifugal MR2 refrigerant compressors is two in methane, ethane or ethene, propane, nitrogen
The mixture of kind above material.
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| CN106753635B (en) * | 2016-12-06 | 2019-05-03 | 河北工业大学 | The production method and equipment of natural gas and condensate recycling liquefied gas and ethylene glycol are handled simultaneously |
| US10976103B2 (en) | 2017-12-15 | 2021-04-13 | Saudi Arabian Oil Company | Process integration for natural gas liquid recovery |
| CN108106325B (en) * | 2018-01-08 | 2024-01-19 | 中国寰球工程有限公司 | Natural gas liquefaction system suitable for sea |
| US10982898B2 (en) * | 2018-05-11 | 2021-04-20 | Air Products And Chemicals, Inc. | Modularized LNG separation device and flash gas heat exchanger |
| CN111777484B (en) * | 2020-07-08 | 2023-05-30 | 西安长庆科技工程有限责任公司 | Device and method for purifying propane by adopting depropanizer with built-in plate reboiler |
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