CN103868323B - A kind of natural gas expansion heavy hydrocarbon recovery system and technique being applicable to sea - Google Patents

A kind of natural gas expansion heavy hydrocarbon recovery system and technique being applicable to sea Download PDF

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Publication number
CN103868323B
CN103868323B CN201410080455.9A CN201410080455A CN103868323B CN 103868323 B CN103868323 B CN 103868323B CN 201410080455 A CN201410080455 A CN 201410080455A CN 103868323 B CN103868323 B CN 103868323B
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liquid
phase
gas
connects
separator
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CN103868323A (en
Inventor
谢彬
李玉星
喻西崇
廖红琴
王春升
王武昌
金海刚
朱建鲁
程兵
冯加果
李阳
王世圣
谢文会
王清
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China National Offshore Oil Corp CNOOC
CNOOC Research Institute Co Ltd
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China University of Petroleum East China
China National Offshore Oil Corp CNOOC
CNOOC Research Institute Co Ltd
Offshore Oil Engineering Co Ltd
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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
    • 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
    • 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
    • F25J3/0228—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 separated product stream
    • F25J3/0233—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 separated product stream separation of CnHm with 1 carbon atom or more
    • 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
    • F25J3/0228—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 separated product stream
    • F25J3/0238—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 separated product stream separation of CnHm with 2 carbon atoms or more
    • 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
    • F25J3/0228—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 separated product stream
    • F25J3/0242—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 separated product stream separation of CnHm with 3 carbon atoms or more
    • 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
    • F25J3/0228—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 separated product stream
    • F25J3/0247—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 separated product stream separation of CnHm with 4 carbon atoms or more
    • 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
    • F25J2200/02—Processes or apparatus using separation by rectification in a single pressure main column 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
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/40—Features relating to the provision of boil-up in the bottom of a column
    • 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
    • F25J2200/70—Refluxing the column with a condensed part of the feed stream, i.e. fractionator top is stripped or self-rectified
    • 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
    • F25J2205/00—Processes or apparatus using other separation and/or other processing means
    • F25J2205/02—Processes or apparatus using other separation and/or other processing means using simple phase separation in a vessel or drum
    • F25J2205/04—Processes or apparatus using other separation and/or other processing means using simple phase separation in a vessel or drum in the feed line, i.e. upstream of the 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
    • F25J2215/00—Processes characterised by the type or other details of the product stream
    • F25J2215/62—Ethane or ethylene
    • 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
    • F25J2215/00—Processes characterised by the type or other details of the product stream
    • F25J2215/64—Propane or propylene
    • 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
    • F25J2215/00—Processes characterised by the type or other details of the product stream
    • F25J2215/66—Butane or mixed butanes
    • 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
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/02—Internal refrigeration with liquid vaporising loop
    • 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
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/12—External refrigeration with liquid vaporising loop
    • 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
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/60—Closed external refrigeration cycle with single component refrigerant [SCR], e.g. C1-, C2- or C3-hydrocarbons
    • 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
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/90—External refrigeration, e.g. conventional closed-loop mechanical refrigeration unit using Freon or NH3, unspecified external refrigeration
    • F25J2270/902—Details about the refrigeration cycle used, e.g. composition of refrigerant, arrangement of compressors or cascade, make up sources, use of reflux exchangers etc.
    • 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
    • F25J2290/00—Other details not covered by groups F25J2200/00 - F25J2280/00
    • F25J2290/34—Details about subcooling of liquids

Abstract

The present invention relates to a kind of the natural gas expansion heavy hydrocarbon recovery system and the technique that are applicable to sea, it is characterized in that: it comprises an ice chest, a chilldown system and a heavy hydrocarbon piece-rate system; Chilldown system adopts three tier structure cold for processing natural gas in heavy hydrocarbon piece-rate system and LPG provides cold; Adopt this kind of technique can make full use of the cold of pre-cooling unit, and utilize the pressure energy of high-pressure natural gas self, fully reclaim the heavy hydrocarbon in natural gas, improve propane recovery, to reach good economy.Chilldown system of the present invention and heavy hydrocarbon piece-rate system internal unit is compact and simple, flow process valve member is few and be convenient to install, is therefore very easily applied to operation on the sea.Therefore, the present invention can be widely used in the heavy hydrocarbon recovery process of the high-pressure natural gas of ocean production environment.

Description

A kind of natural gas expansion heavy hydrocarbon recovery system and technique being applicable to sea
Technical field
The present invention relates to a kind of heavy hydrocarbon recovery system and technique, be particularly applicable to marine natural gas expansion heavy hydrocarbon recovery system and technique about a kind of.
Background technology
China coastal seas natural gas proved reserves are enriched, but quite a few is gas field, deep-sea, marginal gas field and low grade natural gas resource.For the exploitation of this type of source of the gas, adopt the mode such as traditional ocean platform and submerged pipeline then can be subject to the restriction of cost and technology, therefore usually LNG-FPSO(LiquefiedNaturalGas-FloatingProductionStoragean dOffloadingunit is adopted, liquefied natural gas-Floating Production storage handler).Liquefaction process is one of core technology of LNG-FPSO, and heavy hydrocarbon recovery process is the important step in liquefaction process.
In liquefaction process before natural gas liquefaction, need to carry out heavy hydrocarbon recovery process, otherwise may in liquefaction process because heavy hydrocarbon freezes occluding device.The following content of the general demand fulfillment of heavy hydrocarbon separating technology: before the natural gas 1) after de-heavy hydrocarbon enters liquefaction unit, the constituent content wherein more than ethane meets the requirement of liquefaction process; 2) process runs well, fluctuation is little; 3) to the strong adaptability of different source of the gas; 4) as far as possible many recovery heavy hydrocarbons, to improve the economy of device; 5) technique is simple, and equipment is as far as possible few, and floor space is little; 6) safe and reliable.Land liquefaction factory generally adopts the way of distillation to remove heavy hydrocarbon in pretreating process, adopts dethanizer and liquefied gas tower production fluid in next life liquefied oil gas, remains a small amount of heavy hydrocarbon and is separated removal at low-temperature space.Because land process equipment is various, flow process is complicated, floor space is installed greatly and not easily, therefore at sea applicability is poor, limits its use on Floating Production ship, is not suitable for marine environment.
Summary of the invention
For the problems referred to above, the object of this invention is to provide a kind of utilize the cold of chilldown system and natural gas self to expand cooling combines is applicable to marine natural gas expansion heavy hydrocarbon recovery system and technique.
For achieving the above object, the present invention takes following technical scheme: a kind of natural gas expansion heavy hydrocarbon recovery system being applicable to sea, is characterized in that: it comprises an ice chest, a chilldown system and a heavy hydrocarbon piece-rate system; Six pipelines for heat exchange are set in described ice chest; Described chilldown system comprises a low pressure separator, the entrance of described low pressure separator is connected the two ends of the 3rd pipeline in described ice chest with liquid-phase outlet, the gaseous phase outlet of described low pressure separator connects one first compressor, one first blender, one second compressor, one second blender, one the 3rd compressor, a water cooler, a first throttle valve and a high-pressure separator successively; The gaseous phase outlet of described high-pressure separator connects the gas phase entrance of described second blender, and the liquid-phase outlet of described high-pressure separator connects one first current divider; First outlet of described first current divider connects the entrance of described high-pressure separator by the first pipeline in described ice chest, and the second outlet of described first current divider connects a MP separator by a second throttle; The gaseous phase outlet of described MP separator connects the gas phase entrance of described first blender, and the liquid-phase outlet of described MP separator connects one second current divider; First outlet of described second current divider connects the entrance of described MP separator by the second pipeline in described ice chest, and the second outlet of described second current divider connects the entrance of described low pressure separator by one the 3rd choke valve; In described ice chest, the entrance of the 6th pipeline connects gas pipeline, exports the gas-liquid separator, a Natural gas expander and the contact tower that connect successively in described heavy hydrocarbon piece-rate system; The liquid-phase outlet of described gas-liquid separator is connected the lower entrances of described contact tower by one the 7th choke valve and the 4th pipeline in described ice chest, the gaseous phase outlet of described contact tower connects follow-up liquefaction unit, and the liquid-phase outlet of described contact tower connects the upper entrance of a dethanizer by one the 4th choke valve; The gaseous phase outlet of described dethanizer connects fuel gas for station, and the liquid-phase outlet of described dethanizer connects the upper entrance of one the 5th choke valve and a debutanizing tower successively; The liquid-phase outlet of described debutanizing tower connects a cooler, one the 6th choke valve and a NGL storage tank successively; The gaseous phase outlet of described debutanizing tower connects a condenser, and described condensator outlet one end connects back described debutanizing tower, and the other end is connected a LPG storage tank by the 5th pipeline in described ice chest with one the 8th choke valve.
The liquid-phase outlet of described dethanizer first connects one first reboiler, then connects described 5th choke valve by the liquid-phase outlet of described first reboiler; The gaseous phase outlet of described first reboiler connects back described dethanizer.
The liquid-phase outlet of described debutanizing tower first connects one second reboiler, then connects described cooler by the liquid-phase outlet of described second reboiler.
Described Natural gas expander is turbo-expander;
Described ice chest is plate-fin heat exchanger.
A kind of employing is applicable to the recovery process of marine natural gas expansion heavy hydrocarbon recovery system, it comprises the following steps: 1) in chilldown system, gas-liquid two-phase cold-producing medium is after low pressure separator is separated, gas phase enters the first blender after the first compressor boost, is mixed into the second compressor with the gas phase be separated from MP separator; After the second compressor boost, enter the second blender, be mixed into the 3rd compressor with the gas phase be separated from high-pressure separator; After the 3rd compressor boost, enter water cooler, become liquid phase through water cooler cooling, the cold-producing medium becoming gas-liquid two-phase through first throttle valve decrease temperature and pressure enters high-pressure separator; After high-pressure separator carries out gas-liquid separation, gas phase enters the second blender, and liquid phase enters the first current divider, through first current divider shunting a part of liquid phase via ice chest in the first pipeline cold is provided after enter high-pressure separator, formed the first order refrigeration; 2) MP separator is entered after another part liquid phase of the first current divider shunting becomes gas-liquid two-phase via second throttle decrease temperature and pressure; After MP separator carries out gas-liquid separation, gas phase enters the first blender, and liquid phase enters the second current divider, through second current divider shunting a part of liquid phase via ice chest in the second pipeline cold is provided after enter MP separator, formed the second level refrigeration; 3) low pressure separator is entered after another part liquid phase of the second current divider shunting becomes gas-liquid two-phase via the 3rd choke valve decrease temperature and pressure; After low pressure separator carries out gas-liquid separation, gas phase enters the first compressor, and liquid phase enters low pressure separator after the 3rd pipeline provides cold in ice chest, forms third level refrigeration; 4) in heavy hydrocarbon piece-rate system, natural gas via enters ice chest by the 6th pipeline of ice chest, becomes gas-liquid two-phase enter gas-liquid separator through ice chest precooling cooling; 5) liquid phase gone out through gas-liquid separator separates enters the 4th pipeline in ice chest after the 7th choke valve decrease temperature and pressure, and enter the lower entrances of contact tower after cooling, the gas phase gone out through gas-liquid separator separates enters Natural gas expander; 6) after Natural gas expander decrease temperature and pressure, form gas-liquid two-phase and enter contact tower, the natural gas obtaining removing heavy hydrocarbon at the gaseous phase outlet of contact tower enters follow-up liquefaction unit, and the liquid phase heavy hydrocarbon bottom contact tower enters dethanizer after the 4th choke valve step-down; 7) obtain removing the ethane of heavy hydrocarbon at the tower top of dethanizer and enter fuel gas for station, the liquid phase of dethanizer heats generation gas-liquid two-phase again through the first reboiler, gas phase is back in dethanizer carries out deethanization process again, and liquid phase stream enters debutanizing tower after the 5th choke valve step-down; 8) in the gas phase that the gaseous phase outlet of debutanizing tower obtains, be again back to debutanizing tower through condenser condenses part liquid phase, another part liquid phase enters after in ice chest, the 5th pipeline cools, and enters LPG storage tank and store after the 8th choke valve step-down process; The liquid phase of debutanizing tower bottom heats generation gas-liquid two-phase again through the second reboiler, and gas phase is back in debutanizing tower carries out debutanization process again, and liquid phase stream cools through cooler, enter NGL storage tank after the 6th choke valve step-down stores.
Cold-producing medium adopts propane.
Adopt seawater as cooling media in described water cooler.
The present invention is owing to taking above technical scheme, it has the following advantages: 1, the present invention utilizes chilldown system by ice chest for processing natural gas in heavy hydrocarbon piece-rate system and LPG provides three grades of colds, adopt this kind of technique can make full use of the cold of chilldown system, and in conjunction with the pressure energy of heavy hydrocarbon piece-rate system mesohigh natural gas self, make heavy hydrocarbon piece-rate system fully reclaim heavy hydrocarbon in natural gas, improve propane recovery to reach good economy.Heavy hydrocarbon piece-rate system of the present invention utilizes a gas-liquid separator, Natural gas expander, contact tower, dethanizer, a debutanizing tower are separated with the heavy hydrocarbon that five choke valves realize high-pressure natural gas, this heavy hydrocarbon piece-rate system facility compact, simple, flow process valve member is few, is therefore very easily applied on marine LNG-FPSO.2, adopt unitary system cryogen to carry out inner loop in the present invention in chilldown system, greatly reduce the start-up time of a lot of auxiliary equipment thus, and not only can save the operations such as cold-producing medium proportioning, relative control structure is simplified; And when running into typhoon when to work at sea, can stop rapidly and enhance productivity.3, present system is not only insensitive to the condition such as component, temperature, pressure of natural gas, and all meet existing standard by the product that present system refines, therefore the present invention can be widely used in the heavy hydrocarbon recovery process of the high-pressure natural gas of ocean production environment.
Accompanying drawing explanation
Fig. 1 is process flow diagram of the present invention
Fig. 2 is cold box interior schematic diagram of the present invention
Detailed description of the invention
Below in conjunction with drawings and Examples, the present invention is described in detail.
As shown in Figure 1, present system comprises ice chest 10, chilldown system 20 and a heavy hydrocarbon piece-rate system 40.
Six pipelines 11,12,13,14,15,16 for heat exchange are provided with in ice chest 10 of the present invention.
Chilldown system 20 of the present invention comprises low pressure separator 21, first compressor 22, first blender 23, second compressor 24, second blender 25, the 3rd compressor 26, water cooler 27, first throttle valve 28, high-pressure separator 29, first current divider 30, second throttle 31, MP separator 32, second current divider 33 and the 3rd choke valve 34.
The entrance of low pressure separator 21 is connected the two ends of the 3rd pipeline 13 in ice chest 10 with liquid-phase outlet, the gaseous phase outlet of low pressure separator 21 connects the first compressor 22, first blender 23, second compressor 24, second blender 25, the 3rd compressor 26, water cooler 27, first throttle valve 28 and high-pressure separator 29 successively; The gaseous phase outlet of high-pressure separator 29 connects the gas phase entrance of the second blender 25, and the liquid-phase outlet of high-pressure separator 29 connects the first current divider 30; First outlet of the first current divider 30 connects the entrance of high-pressure separator 29 by the first pipeline 11 in ice chest 10, and the second outlet of the first current divider 30 connects MP separator 32 by second throttle 31; The gaseous phase outlet of MP separator 32 connects the gas phase entrance of the first blender 23, and the liquid-phase outlet of MP separator 32 connects the second current divider 33; First outlet of the second current divider 33 connects the entrance of MP separator 32 by the second pipeline 12 in ice chest 10, and the second outlet of the second current divider 33 connects the entrance of low pressure separator 21 by the 3rd choke valve 34.
Heavy hydrocarbon piece-rate system 40 of the present invention comprises gas-liquid separator 41, Natural gas expander 42, contact tower 43, the 4th choke valve 44, dethanizer 45, the 5th choke valve 46, debutanizing tower 47, cooler 48, the 6th choke valve 49, NGL (NaturalGasLiquid, gas reducing liquid) storage tank 50, the 7th choke valve 51, the 8th choke valve 52 and LPG(LiquefiedPetroleumGas, liquefied petroleum gas) storage tank 53.
In ice chest 10, the entrance of the 6th pipeline 16 connects gas pipeline, and outlet connects gas-liquid separator 41, Natural gas expander 42 and contact tower 43 successively; The liquid-phase outlet of gas-liquid separator 41 is connected the lower entrances of contact tower 43 by the 7th choke valve 51 and the 4th pipeline 14 in ice chest 10, the gaseous phase outlet of contact tower 43 connects follow-up liquefaction unit, and the liquid-phase outlet of contact tower 43 connects the upper entrance of dethanizer 45 by the 4th choke valve 44; The gaseous phase outlet of dethanizer 45 connects fuel gas for station, and the liquid-phase outlet of dethanizer 45 connects the upper entrance of the 5th choke valve 46 and debutanizing tower 47 successively; The liquid-phase outlet of debutanizing tower 47 connects cooler 48, the 6th choke valve 49 and NGL storage tank 50 successively; The gaseous phase outlet of debutanizing tower 47 connects the condenser 54 of a routine, and condenser 54 exit end connects back debutanizing tower 47, and the other end is connected LPG storage tank 53 by the 5th pipeline 15 in ice chest 10 with the 8th choke valve 52.
In above-described embodiment, the liquid-phase outlet of dethanizer 45 first can connect one first reboiler 55, then connects back dethanizer 45 by the gaseous phase outlet of the first reboiler 55 liquid-phase outlet connection the 5th choke valve 46, first reboiler 55.The liquid-phase outlet of debutanizing tower 47 first can connect one second reboiler 56, then connects back debutanizing tower 47 by the gaseous phase outlet of the second reboiler 56 liquid-phase outlet connection cooler 48, second reboiler 56.
In above-described embodiment, ice chest 10 can adopt plate-fin heat exchanger, and propane can be adopted as cold-producing medium in chilldown system 20, seawater can be adopted in water cooler 27 as cooling media, and Natural gas expander 42 can adopt turbo-expander.First throttle valve 28, second throttle 31, the 3rd choke valve 34, the 4th choke valve 44, the 5th choke valve 46, the 6th choke valve 49, the 7th choke valve 51, the 8th choke valve 52 adopt J-T valve (Joule-Thomson throttle expansion valve).
A kind of natural gas expansion heavy hydrocarbon recovery process being applicable to sea of the present invention comprises the following steps:
1) in chilldown system 20, gas-liquid two-phase cold-producing medium is after low pressure separator 21 is separated, and gas phase enters the first blender 23 after the first compressor 22 supercharging, is mixed into the second compressor 24 with the gas phase be separated from MP separator 32; After the second compressor 24 supercharging, enter the second blender 25, be mixed into the 3rd compressor 26 with the gas phase be separated from high-pressure separator 29; After the 3rd compressor 26 supercharging, enter water cooler 27, become liquid phase through water cooler 27 cooling, the cold-producing medium becoming gas-liquid two-phase through first throttle valve 28 decrease temperature and pressure enters high-pressure separator 29; After high-pressure separator 29 carries out gas-liquid separation, gas phase enters the second blender 25, liquid phase enters the first current divider 30, through first current divider 30 shunt a part of liquid phase via ice chest 10 in the first pipeline 11 cold is provided after enter high-pressure separator 29, be the first order refrigeration;
2) MP separator 32 is entered after another part liquid phase that the first current divider 30 is shunted becomes gas-liquid two-phase via second throttle 31 decrease temperature and pressure; After MP separator 32 carries out gas-liquid separation, gas phase enters the first blender 23, liquid phase enters the second current divider 33, through second current divider 33 shunt a part of liquid phase via ice chest 10 in the second pipeline 12 cold is provided after enter MP separator 32, be the second level refrigeration;
3) low pressure separator 21 is entered after another part liquid phase that the second current divider 33 is shunted becomes gas-liquid two-phase via the 3rd choke valve 34 decrease temperature and pressure; After low pressure separator 21 carries out gas-liquid separation, gas phase enters the first compressor 22, and liquid phase enters low pressure separator 21 after the 3rd pipeline 13 provides cold in ice chest 10, is third level refrigeration;
4) in heavy hydrocarbon piece-rate system 40, natural gas via enters ice chest 10 by the 6th pipeline 16 of ice chest 10, becomes gas-liquid two-phase enter gas-liquid separator 41 through ice chest 10 precooling cooling;
5) after the 7th choke valve 51 decrease temperature and pressure, enter the 4th pipeline 14 in ice chest 10 through the isolated liquid phase of gas-liquid separator 41, after cooling, enter the lower entrances of contact tower 43, enter Natural gas expander 42 through the isolated gas phase of gas-liquid separator 41;
6) after Natural gas expander 42 decrease temperature and pressure, form gas-liquid two-phase and enter contact tower 43, the natural gas obtaining removing heavy hydrocarbon at the gaseous phase outlet of contact tower 43 enters follow-up liquefaction unit, and the liquid phase heavy hydrocarbon bottom contact tower 43 enters dethanizer 45 after the 4th choke valve 44 step-down;
7) obtain removing the ethane of heavy hydrocarbon at the tower top of dethanizer 45 and enter fuel gas for station, the liquid phase of dethanizer 45 heats generation gas-liquid two-phase again through the first reboiler 55, gas phase is back in dethanizer 45 carries out deethanization process again, and liquid phase stream enters debutanizing tower 47 after the 5th choke valve 46 step-down;
8) gas phase obtained at the gaseous phase outlet of debutanizing tower 47 is back in debutanizing tower 47 again through condenser 54 condensation part liquid phase carries out debutanization process again, another part liquid phase enters after in ice chest 10, the 5th pipeline 15 cools, and enters LPG storage tank 53 and store after the 8th choke valve 52 step-down process.The liquid phase of debutanizing tower 47 bottom again heats through the second reboiler 56 and generates gas-liquid two-phase, and gas phase is back in debutanizing tower 47 carries out debutanization process again, and liquid phase stream cools through cooler 48, enter NGL storage tank 50 after the 6th choke valve 49 step-down stores.
As shown in Figure 2, in ice chest 10 schematic internal view, 61 ~ 62 is the one-level process of refrigerastion of natural gas and LPG of freezing in ice chest 10 after cold-producing medium throttling.63 ~ 64 secondary process of refrigerastions that are freeze in ice chest 10 after cold-producing medium throttling natural gas and LPG.65 ~ 66 cold processes of three tier structure that are freeze in ice chest 10 after cold-producing medium throttling natural gas and LPG.67 ~ 68 is the process of refrigerastion of liquid natural gas after the 7th choke valve 51 decrease temperature and pressure in ice chest 10 be separated through gas-liquid separator 41.69 ~ 70 is the process that natural gas is cooled in ice chest 10.71 ~ 72 is the process that LPG is cooled in ice chest 10.
Enumerate a specific embodiment below:
1) in chilldown system 20, cold-producing medium adopts propane.The propane of gas-liquid two-phase is after low pressure separator 21 is separated, and gas phase is pressurized to-5.2 DEG C through the first compressor 22, enters the first blender 23 after 0.29MPa, is mixed into the second compressor 24 with the gas phase be separated from MP separator 32; Be pressurized to 15.9 DEG C through the second compressor 24, enter the second blender 25 after 0.55MPa, after the gas phase be separated mixes, enter the 3rd compressor 26 with from high-pressure separator 29; Be pressurized to 52.2 DEG C through the 3rd compressor 26, enter water cooler 27 after 1.36MPa, cool after 31 DEG C through water cooler 27, propane all liquefies, and the gas-liquid two-phase propane through first throttle valve 28 decrease temperature and pressure to 5 DEG C, 0.55MPa enters high-pressure separator 29; After high-pressure separator 29 carries out gas-liquid separation, gas phase enters the second blender 25, liquid phase enters the first current divider 30, through first current divider 30 shunt a part of liquid phase via ice chest 10 in the first pipeline 11 cold is provided after enter high-pressure separator 29, be the first order refrigeration;
2) another part liquid phase of shunting of the first current divider 30 via second throttle 31 decrease temperature and pressure to-15 DEG C, the gas-liquid two-phase of 0.29MPa enters MP separator 32; After MP separator 32 carries out gas-liquid separation, gas phase enters the first blender 23, liquid phase enters the second current divider 33, through second current divider 33 shunt a part of liquid phase via ice chest 10 in the second pipeline 12 cold is provided after enter MP separator 32, be the second level refrigeration;
3) another part liquid phase of shunting of the second current divider 33 via the 3rd choke valve 34 decrease temperature and pressure to-36 DEG C, the gas-liquid two-phase of 0.13MPa enters low pressure separator 21; After low pressure separator 21 carries out gas-liquid separation, gas phase enters the first compressor 22, and liquid phase enters low pressure separator 21 after the 3rd pipeline 13 provides cold in ice chest 10, is third level refrigeration;
4) in heavy hydrocarbon piece-rate system, latter 36 DEG C of depickling dehydration, 7.17MPa natural gas via enters ice chest 10 by the 6th pipeline 16 of ice chest 10, becomes-32 DEG C, the gas-liquid two-phase of 7.12MPa enters gas-liquid separator 41 through ice chest 10 precooling cooling;
5) after the 7th choke valve 51 decrease temperature and pressure extremely-40.24 DEG C, 4.7MPa, the 4th pipeline 14 in ice chest 10 is entered through the isolated liquid phase of gas-liquid separator 41, carry out cooling temperature after rewarming rise to 31 DEG C, be depressurized to 4.65MPa after enter the lower entrances of contact tower 43, enter Natural gas expander 42 through the isolated gas phase of gas-liquid separator 41;
6) after Natural gas expander 42 decrease temperature and pressure-55.54 DEG C, 4.5MPa formed gas-liquid two-phase enter contact tower 43, obtain-56.26 DEG C at the gaseous phase outlet of contact tower 43, the 4.4MPa natural gas that removes heavy hydrocarbon enters follow-up liquefaction unit ,-20.45 DEG C bottom contact tower 43,4.45MPa liquid phase heavy hydrocarbon enters dethanizer 45 after the 4th choke valve 44 step-down 2.95MPa;
7) obtain removing the ethane of heavy hydrocarbon at the tower top of dethanizer 45 and enter fuel gas for station, the liquid phase of dethanizer 45 heats generation gas-liquid two-phase again through the first reboiler 55, gas phase is back in dethanizer 45 carries out deethanization process again, 128.2 DEG C, the liquid phase stream of 2.9MPa enters debutanizing tower 47 after the 5th choke valve 46 is depressurized to 0.65MPa;
8) in the gas phase that the gaseous phase outlet of debutanizing tower 47 obtains, debutanizing tower 47 is again back to through condenser 54 condensation part liquid phase, another part 18.11 DEG C, 0.55MPa liquid phase enter the 5th pipeline 15 in ice chest 10 and cool to-32 DEG C, enter LPG storage tank 53 and store after the 8th choke valve 52 is depressurized to 0.12MPa.The liquid phase of debutanizing tower 47 bottom heats generation gas-liquid two-phase again through the second reboiler 56, gas phase is back in debutanizing tower 47 carries out debutanization process again, 125 DEG C, the liquid phase stream of 0.6MPa through cooler 48 cooling down to-32 DEG C, the 6th choke valve 49 enters NGL storage tank 50 after being depressurized to 0.12MPa and stores.
The various embodiments described above are only for illustration of the present invention; wherein the structure of each parts, connected mode and manufacture craft etc. all can change to some extent; every equivalents of carrying out on the basis of technical solution of the present invention and improvement, all should not get rid of outside protection scope of the present invention.

Claims (10)

1. be applicable to a marine natural gas expansion heavy hydrocarbon recovery system, it is characterized in that: it comprises an ice chest, a chilldown system and a heavy hydrocarbon piece-rate system;
Six pipelines for heat exchange are set in described ice chest;
Described chilldown system comprises a low pressure separator, the entrance of described low pressure separator is connected the two ends of the 3rd pipeline in described ice chest with liquid-phase outlet, the gaseous phase outlet of described low pressure separator connects one first compressor, one first blender, one second compressor, one second blender, one the 3rd compressor, a water cooler, a first throttle valve and a high-pressure separator successively; The gaseous phase outlet of described high-pressure separator connects the gas phase entrance of described second blender, and the liquid-phase outlet of described high-pressure separator connects one first current divider; First outlet of described first current divider connects the entrance of described high-pressure separator by the first pipeline in described ice chest, and the second outlet of described first current divider connects a MP separator by a second throttle; The gaseous phase outlet of described MP separator connects the gas phase entrance of described first blender, and the liquid-phase outlet of described MP separator connects one second current divider; First outlet of described second current divider connects the entrance of described MP separator by the second pipeline in described ice chest, and the second outlet of described second current divider connects the entrance of described low pressure separator by one the 3rd choke valve;
In described ice chest, the entrance of the 6th pipeline connects gas pipeline, exports the gas-liquid separator, a Natural gas expander and the contact tower that connect successively in described heavy hydrocarbon piece-rate system; The liquid-phase outlet of described gas-liquid separator is connected the lower entrances of described contact tower by one the 7th choke valve and the 4th pipeline in described ice chest, the gaseous phase outlet of described contact tower connects follow-up liquefaction unit, and the liquid-phase outlet of described contact tower connects the upper entrance of a dethanizer by one the 4th choke valve; The gaseous phase outlet of described dethanizer connects fuel gas for station, and the liquid-phase outlet of described dethanizer connects the upper entrance of one the 5th choke valve and a debutanizing tower successively; The liquid-phase outlet of described debutanizing tower connects a cooler, one the 6th choke valve and a NGL storage tank successively; The gaseous phase outlet of described debutanizing tower connects a condenser, and described condensator outlet one end connects back described debutanizing tower, and the other end is connected a LPG storage tank by the 5th pipeline in described ice chest with one the 8th choke valve.
2. be a kind ofly as claimed in claim 1 applicable to marine natural gas expansion heavy hydrocarbon recovery system, it is characterized in that: the liquid-phase outlet of described dethanizer first connects one first reboiler, then connect described 5th choke valve by the liquid-phase outlet of described first reboiler; The gaseous phase outlet of described first reboiler connects back described dethanizer.
3. be a kind ofly as claimed in claim 1 applicable to marine natural gas expansion heavy hydrocarbon recovery system, it is characterized in that: the liquid-phase outlet of described debutanizing tower first connects one second reboiler, then connects described cooler by the liquid-phase outlet of described second reboiler.
4. be a kind ofly as claimed in claim 2 applicable to marine natural gas expansion heavy hydrocarbon recovery system, it is characterized in that: the liquid-phase outlet of described debutanizing tower first connects one second reboiler, then connects described cooler by the liquid-phase outlet of described second reboiler.
5. as claimed in claim 1 or 2 or 3 or 4 a kind of is applicable to marine natural gas expansion heavy hydrocarbon recovery system, it is characterized in that: described Natural gas expander is turbo-expander;
6. as claimed in claim 1 or 2 or 3 or 4 a kind of is applicable to marine natural gas expansion heavy hydrocarbon recovery system, it is characterized in that: described ice chest is plate-fin heat exchanger.
7. be a kind ofly as claimed in claim 5 applicable to marine natural gas expansion heavy hydrocarbon recovery system, it is characterized in that: described ice chest is plate-fin heat exchanger.
8. adopt the recovery process being applicable to marine natural gas expansion heavy hydrocarbon recovery system as described in any one of claim 1 ~ 7, it comprises the following steps:
1) in chilldown system, gas-liquid two-phase cold-producing medium is after low pressure separator is separated, and gas phase enters the first blender after the first compressor boost, is mixed into the second compressor with the gas phase be separated from MP separator; After the second compressor boost, enter the second blender, be mixed into the 3rd compressor with the gas phase be separated from high-pressure separator; After the 3rd compressor boost, enter water cooler, become liquid phase through water cooler cooling, the cold-producing medium becoming gas-liquid two-phase through first throttle valve decrease temperature and pressure enters high-pressure separator; After high-pressure separator carries out gas-liquid separation, gas phase enters the second blender, and liquid phase enters the first current divider, through first current divider shunting a part of liquid phase via ice chest in the first pipeline cold is provided after enter high-pressure separator, formed the first order refrigeration;
2) MP separator is entered after another part liquid phase of the first current divider shunting becomes gas-liquid two-phase via second throttle decrease temperature and pressure; After MP separator carries out gas-liquid separation, gas phase enters the first blender, and liquid phase enters the second current divider, through second current divider shunting a part of liquid phase via ice chest in the second pipeline cold is provided after enter MP separator, formed the second level refrigeration;
3) low pressure separator is entered after another part liquid phase of the second current divider shunting becomes gas-liquid two-phase via the 3rd choke valve decrease temperature and pressure; After low pressure separator carries out gas-liquid separation, gas phase enters the first compressor, and liquid phase enters low pressure separator after the 3rd pipeline provides cold in ice chest, forms third level refrigeration;
4) in heavy hydrocarbon piece-rate system, natural gas via enters ice chest by the 6th pipeline of ice chest, becomes gas-liquid two-phase enter gas-liquid separator through ice chest precooling cooling;
5) liquid phase gone out through gas-liquid separator separates enters the 4th pipeline in ice chest after the 7th choke valve decrease temperature and pressure, and enter the lower entrances of contact tower after cooling, the gas phase gone out through gas-liquid separator separates enters Natural gas expander;
6) after Natural gas expander decrease temperature and pressure, form gas-liquid two-phase and enter contact tower, the natural gas obtaining removing heavy hydrocarbon at the gaseous phase outlet of contact tower enters follow-up liquefaction unit, and the liquid phase heavy hydrocarbon bottom contact tower enters dethanizer after the 4th choke valve step-down;
7) obtain removing the ethane of heavy hydrocarbon at the tower top of dethanizer and enter fuel gas for station, the liquid phase of dethanizer heats generation gas-liquid two-phase again through the first reboiler, gas phase is back in dethanizer carries out deethanization process again, and liquid phase stream enters debutanizing tower after the 5th choke valve step-down;
8) in the gas phase that the gaseous phase outlet of debutanizing tower obtains, be again back to debutanizing tower through condenser condenses part liquid phase, another part liquid phase enters after in ice chest, the 5th pipeline cools, and enters LPG storage tank and store after the 8th choke valve step-down process; The liquid phase of debutanizing tower bottom heats generation gas-liquid two-phase again through the second reboiler, and gas phase is back in debutanizing tower carries out debutanization process again, and liquid phase stream cools through cooler, enter NGL storage tank after the 6th choke valve step-down stores.
9. be a kind ofly as claimed in claim 8 applicable to marine natural gas expansion heavy hydrocarbon recovery process, it is characterized in that: cold-producing medium adopts propane.
10. be a kind ofly as claimed in claim 9 applicable to marine natural gas expansion heavy hydrocarbon recovery process, it is characterized in that: in described water cooler, adopt seawater as cooling media.
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