CN103868323A - Seaborne natural gas expansion heavy hydrocarbon recovery system and process - Google Patents

Seaborne natural gas expansion heavy hydrocarbon recovery system and process Download PDF

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Publication number
CN103868323A
CN103868323A CN201410080455.9A CN201410080455A CN103868323A CN 103868323 A CN103868323 A CN 103868323A CN 201410080455 A CN201410080455 A CN 201410080455A CN 103868323 A CN103868323 A CN 103868323A
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China
Prior art keywords
liquid
phase
gas
connects
heavy hydrocarbon
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CN201410080455.9A
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CN103868323B (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

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  • Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Mechanical Engineering (AREA)
  • Thermal Sciences (AREA)
  • General Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Separation By Low-Temperature Treatments (AREA)

Abstract

The invention relates to a seaborne natural gas expansion heavy hydrocarbon recovery system and a natural gas expansion heavy hydrocarbon recovery process. The system is characterized by comprising a cold box, a pre-cooling system and a heavy hydrocarbon separation system, wherein the pre-cooling system adopts three-stage refrigeration for providing cold quantity for natural gas and LPG (liquefied petroleum gas) processing in a heavy hydrocarbon separation system. When the process is adopted, the cold quantity of a pre-cooling unit can be sufficiently utilized, in addition, the self pressure energy of the high-pressure natural gas is utilized, heavy hydrocarbon in the natural gas is sufficiently recovered, the propane recovery rate is improved, and better economic performance can be reached. The internal equipment of the pre-cooling system and the heavy hydrocarbon separation system is compact and simple, flow process valve elements are fewer, and the installation is convenient, so the system and the process can be easily applied to seaborne operation. Therefore the system and the process provided by the invention can be widely applied to the heavy hydrocarbon recovery process of high-pressure natural gas of the ocean production environment.

Description

A kind ofly be applicable to marine natural gas expansion heavy hydrocarbon recovery system and technique
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 abundant, 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 traditional mode such as ocean platform and submerged pipeline can be subject to the restriction of cost and technology, therefore conventionally adopt LNG-FPSO(Liquefied Natural Gas-Floating Production Storage andOffloading unit, 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 be because heavy hydrocarbon freezes occluding device in liquefaction process.Heavy hydrocarbon separating technology generally need to meet following content: before 1) natural gas after de-heavy hydrocarbon enters liquefaction unit, wherein constituent content more than ethane meets the requirement of liquefaction process; 2) process operation is stable, and fluctuation is little; 3) strong adaptability to different sources of the gas; 4) many recovery heavy hydrocarbon as far as possible, 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 separates and remove at low-temperature space.Because land process equipment is various, flow process is complicated, floor space is large and be difficult for installation, therefore at sea applicability is poor, has limited 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 cold that utilizes chilldown system and natural gas self marine natural gas expansion heavy hydrocarbon recovery system and the technique of being applicable to that cooling combines that expands.
For achieving the above object, the present invention takes following technical scheme: be a kind ofly applicable to 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 the second blender, and the liquid-phase outlet of described high-pressure separator connects one first current divider; The first outlet of described the first current divider connects the entrance of described high-pressure separator by the first pipeline in described ice chest, the second outlet of described the first current divider connects a MP separator by one second choke valve; The gaseous phase outlet of described MP separator connects the gas phase entrance of described the first blender, and the liquid-phase outlet of described MP separator connects one second current divider; The first outlet of described the second current divider connects the entrance of described MP separator by the second pipeline in described ice chest, the second outlet of described the 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, and outlet connects a gas-liquid separator, a Natural gas expander and the contact tower in described heavy hydrocarbon piece-rate system successively; The liquid-phase outlet of described gas-liquid separator is connected the bottom entrance 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 the 5th choke valve by the liquid-phase outlet of described the first reboiler; The gaseous phase outlet of described the 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 the 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 separates, gas phase enters the first blender after the first compressor boost, is mixed into the second compressor with the gas phase separating from MP separator; After the second compressor boost, enter the second blender, be mixed into the 3rd compressor with the gas phase separating from high-pressure separator; After the 3rd compressor boost, enter water cooler, through water cooler, cooling becomes liquid phase, and the cold-producing medium that becomes gas-liquid two-phase through first throttle valve decrease temperature and pressure enters high-pressure separator; High-pressure separator carries out after gas-liquid separation, and gas phase enters the second blender, and liquid phase enters the first current divider, enters high-pressure separator through a part of liquid phase of the first current divider shunting via the first pipeline in ice chest after cold is provided, and forms first order refrigeration; 2) after another part liquid phase of the first current divider shunting becomes gas-liquid two-phase via the second choke valve decrease temperature and pressure, enter MP separator; MP separator carries out after gas-liquid separation, and gas phase enters the first blender, and liquid phase enters the second current divider, enters MP separator through a part of liquid phase of the second current divider shunting via the second pipeline in ice chest after cold is provided, and forms second level refrigeration; 3) 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, enter low pressure separator; Low pressure separator carries out after gas-liquid separation, and 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 going out through gas-liquid separator separates enters the 4th pipeline in ice chest after the 7th choke valve decrease temperature and pressure, carries out entering after cooling the bottom entrance of contact tower, and the gas phase going 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 that obtains removing heavy hydrocarbon at the gaseous phase outlet of contact tower enters follow-up liquefaction unit, and the liquid phase heavy hydrocarbon of contact tower bottom enters dethanizer after the 4th choke valve step-down; 7) ethane that obtains removing heavy hydrocarbon at the tower top of dethanizer enters 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 processing again, and liquid phase stream enters debutanizing tower after the 5th choke valve step-down; 8) gas phase obtaining at the gaseous phase outlet of debutanizing tower, is back to debutanizing tower again through condenser condenses part liquid phase, and another part liquid phase enters in ice chest after the 5th pipeline cools, and after the 8th choke valve step-down is processed, enters LPG storage tank stores; The liquid phase of debutanizing tower bottom heats generation gas-liquid two-phase again through the second reboiler, and gas phase is back to carries out debutanization processing again in debutanizing tower, and liquid phase stream cools, enters NGL storage tank stores after the 6th choke valve step-down through cooler.
Cold-producing medium adopts propane.
In described water cooler, adopt seawater as cooling media.
The present invention is owing to taking above technical scheme, it has the following advantages: 1, the present invention utilizes chilldown system to provide three grades of colds by ice chest for processing natural gas and LPG in heavy hydrocarbon piece-rate system, 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 the heavy hydrocarbon in natural gas, improved propane recovery to reach good economy.The heavy hydrocarbon that heavy hydrocarbon piece-rate system of the present invention utilizes a gas-liquid separator, Natural gas expander, contact tower, dethanizer, debutanizing tower to realize high-pressure natural gas with five choke valves separates, 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, in the present invention, in chilldown system, adopt unitary system cryogen to carry out inner loop, greatly reduced thus the start-up time of a lot of auxiliary equipment, and not only can save the operations such as cold-producing medium proportioning, relative control structure is simplified; And while running into typhoon when working at sea, can stop and enhance productivity rapidly.3, not only the condition such as the component to natural gas, temperature, pressure is insensitive for system of the present invention, and the product refining by system of the present invention all meets existing standard, therefore the present invention can be widely used in the heavy hydrocarbon recovery process of the high-pressure natural gas of ocean production environment.
Brief description of the drawings
Fig. 1 is process flow diagram of the present invention
Fig. 2 is ice chest schematic internal view 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, system of the present invention comprises an ice chest 10, a chilldown system 20 and a heavy hydrocarbon piece-rate system 40.
In ice chest 10 of the present invention, be provided with six pipelines 11,12,13,14,15,16 for heat exchange.
Chilldown system 20 of the present invention comprises low pressure separator 21, the first compressor 22, the first blender 23, the second compressor 24, the second blender 25, the 3rd compressor 26, water cooler 27, first throttle valve 28, high-pressure separator 29, the first current divider 30, the second choke valve 31, MP separator 32, the 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, the first blender 23, the second compressor 24, the 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; The 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, the second outlet of the first current divider 30 connects MP separator 32 by the second choke valve 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; The first outlet of the second current divider 33 connects the entrance of MP separator 32 by the second pipeline 12 in ice chest 10, 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 (Natural Gas Liquid, gas reducing liquid) storage tank 50, the 7th choke valve 51, the 8th choke valve 52 and LPG(Liquefied Petroleum Gas, 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 bottom entrance 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 exports one end and 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 can first connect one first reboiler 55, then connects back dethanizer 45 by the gaseous phase outlet of the first reboiler 55 liquid-phase outlets connection the 5th choke valve 46, the first reboilers 55.The liquid-phase outlet of debutanizing tower 47 can first connect one second reboiler 56, then connects back debutanizing tower 47 by the gaseous phase outlet of the second reboiler 56 liquid-phase outlets connection cooler 48, the second reboilers 56.
In above-described embodiment, ice chest 10 can adopt plate-fin heat exchanger, and the interior propane that can adopt of chilldown system 20, as cold-producing medium, can adopt seawater as cooling media in water cooler 27, and Natural gas expander 42 can adopt turbo-expander.First throttle valve 28, the second choke valve 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).
The present invention is a kind of to be applicable to marine natural gas expansion heavy hydrocarbon recovery process and to comprise the following steps:
1) in chilldown system 20, gas-liquid two-phase cold-producing medium is after low pressure separator 21 separates, and gas phase enters the first blender 23 after the first compressor 22 superchargings, is mixed into the second compressor 24 with the gas phase separating from MP separator 32; After the second compressor 24 superchargings, enter the second blender 25, be mixed into the 3rd compressor 26 with the gas phase separating from high-pressure separator 29; After the 3rd compressor 26 superchargings, enter water cooler 27, through water cooler, 27 coolings become liquid phase, and the cold-producing medium that becomes gas-liquid two-phase through first throttle valve 28 decrease temperature and pressure enters high-pressure separator 29; High-pressure separator 29 carries out after gas-liquid separation, gas phase enters the second blender 25, liquid phase enters the first current divider 30, and a part of liquid phase of shunting through the first current divider 30 enters high-pressure separator 29 via the first pipeline 11 in ice chest 10 after cold is provided, and is first order refrigeration;
2) another part liquid phase that the first current divider 30 is shunted enters MP separator 32 after becoming gas-liquid two-phase via the second choke valve 31 decrease temperature and pressure; MP separator 32 carries out after gas-liquid separation, gas phase enters the first blender 23, liquid phase enters the second current divider 33, and a part of liquid phase of shunting through the second current divider 33 enters MP separator 32 via the second pipeline 12 in ice chest 10 after cold is provided, and is second level refrigeration;
3) another part liquid phase that the second current divider 33 is shunted enters low pressure separator 21 after becoming gas-liquid two-phase via the 3rd choke valve 34 decrease temperature and pressure; Low pressure separator 21 carries out after gas-liquid separation, and gas phase enters the first compressor 22, and liquid phase enters low pressure separator 21 via the 3rd pipeline 13 in ice chest 10 after cold is provided, and 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 coolings;
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, carry out entering after cooling the bottom entrance 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 that obtains removing heavy hydrocarbon at the gaseous phase outlet of contact tower 43 enters follow-up liquefaction unit, and the liquid phase heavy hydrocarbon of contact tower 43 bottoms enters dethanizer 45 after the 4th choke valve 44 step-downs;
7) ethane that obtains removing heavy hydrocarbon at the tower top of dethanizer 45 enters fuel gas for station, the liquid phase of dethanizer 45 again heats and generates gas-liquid two-phase through the first reboiler 55, gas phase is back in dethanizer 45 carries out deethanization processing again, and liquid phase stream enters debutanizing tower 47 after the 5th choke valve 46 step-downs;
8) gas phase obtaining at the gaseous phase outlet of debutanizing tower 47 is again back to and in debutanizing tower 47, again carries out debutanization processing through condenser 54 condensations parts liquid phases, another part liquid phase enters in ice chest 10 after the 5th pipeline 15 cools, and enters LPG storage tank 53 and store after the 8th choke valve 52 step-downs are processed.The liquid phase of debutanizing tower 47 bottoms again heats and generates gas-liquid two-phase through the second reboiler 56, and gas phase is back to carries out debutanization processing again in debutanizing tower 47, and liquid phase stream cools, enters NGL storage tank 50 after the 6th choke valve 49 step-downs and store through cooler 48.
As shown in Figure 2, in ice chest 10 schematic internal view, 61～62 one-level process of refrigerastions for freeze in ice chest 10 after cold-producing medium throttling natural gas and LPG.63～64 secondary process of refrigerastions for freeze in ice chest 10 after cold-producing medium throttling natural gas and LPG.65～66 cold processes of three tier structure for freeze in ice chest 10 after cold-producing medium throttling natural gas and LPG.67～68 is the liquid natural gas process of refrigerastion in ice chest 10 after the 7th choke valve 51 decrease temperature and pressure separating through gas-liquid separator 41.69～70 processes that are cooled in ice chest 10 for natural gas.71～72 processes that are cooled in ice chest 10 for LPG.
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 separates, and gas phase enters the first blender 23 after the first compressor 22 is pressurized to-5.2 DEG C, 0.29MPa, is mixed into the second compressor 24 with the gas phase separating from MP separator 32; After the second compressor 24 is pressurized to 15.9 DEG C, 0.55MPa, enter the second blender 25, mixing with the gas phase separating from high-pressure separator 29, enter the 3rd compressor 26; After the 3rd compressor 26 is pressurized to 52.2 DEG C, 1.36MPa, enter water cooler 27, cool after 31 DEG C through water cooler 27, propane all liquefies, and enters high-pressure separator 29 through the gas-liquid two-phase propane of first throttle valve 28 decrease temperature and pressure to 5 DEG C, 0.55MPa; High-pressure separator 29 carries out after gas-liquid separation, gas phase enters the second blender 25, liquid phase enters the first current divider 30, and a part of liquid phase of shunting through the first current divider 30 enters high-pressure separator 29 via the first pipeline 11 in ice chest 10 after cold is provided, and is first order refrigeration;
2) another part liquid phase that the first current divider 30 is shunted enters MP separator 32 via the gas-liquid two-phase of extremely-15 DEG C of the second choke valve 31 decrease temperature and pressure, 0.29MPa; MP separator 32 carries out after gas-liquid separation, gas phase enters the first blender 23, liquid phase enters the second current divider 33, and a part of liquid phase of shunting through the second current divider 33 enters MP separator 32 via the second pipeline 12 in ice chest 10 after cold is provided, and is second level refrigeration;
3) another part liquid phase that the second current divider 33 is shunted enters low pressure separator 21 via the gas-liquid two-phase of extremely-36 DEG C of the 3rd choke valve 34 decrease temperature and pressure, 0.13MPa; Low pressure separator 21 carries out after gas-liquid separation, and gas phase enters the first compressor 22, and liquid phase enters low pressure separator 21 via the 3rd pipeline 13 in ice chest 10 after cold is provided, and is third level refrigeration;
4) in heavy hydrocarbon piece-rate system, dewater latter 36 DEG C, 7.17MPa natural gas via of depickling enter ice chest 10 by the 6th pipeline 16 of ice chest 10, become-32 DEG C, the gas-liquid two-phase of 7.12MPa enter gas-liquid separator 41 through ice chest 10 precoolings coolings;
5) after extremely-40.24 DEG C of the 7th choke valve 51 decrease temperature and pressure, 4.7MPa, enter the 4th pipeline 14 in ice chest 10 through the isolated liquid phase of gas-liquid separator 41, carry out temperature after cooling rewarming and rise to 31 DEG C, be depressurized to the bottom entrance that enters contact tower 43 after 4.65MPa, 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 form gas-liquid two-phase and enter contact tower 43, gaseous phase outlet at contact tower 43 obtains the natural gas that-56.26 DEG C, 4.4MPa remove heavy hydrocarbon and enters follow-up liquefaction unit, and-20.45 DEG C of contact tower 43 bottoms, 4.45MPa liquid phase heavy hydrocarbon enter dethanizer 45 after the 4th choke valve 44 step-down 2.95MPa;
7) ethane that obtains removing heavy hydrocarbon at the tower top of dethanizer 45 enters fuel gas for station, the liquid phase of dethanizer 45 again heats and generates gas-liquid two-phase through the first reboiler 55, gas phase is back to carries out deethanization processing again in dethanizer 45,128.2 DEG C, the liquid phase stream of 2.9MPa enter debutanizing tower 47 after the 5th choke valve 46 is depressurized to 0.65MPa;
8) gas phase obtaining at the gaseous phase outlet of debutanizing tower 47, again be back to debutanizing tower 47 through condenser 54 condensation part liquid phases, 18.11 DEG C of another part, 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 bottoms again heats and generates gas-liquid two-phase through the second reboiler 56, gas phase is back to carries out debutanization processing again in debutanizing tower 47,125 DEG C, the liquid phase stream of 0.6MPa enter NGL storage tank 50 after being depressurized to 0.12MPa and store through cooler 48 cooling downs to-32 DEG C, the 6th choke valve 49.
The various embodiments described above are only for illustrating 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 the second blender, and the liquid-phase outlet of described high-pressure separator connects one first current divider; The first outlet of described the first current divider connects the entrance of described high-pressure separator by the first pipeline in described ice chest, the second outlet of described the first current divider connects a MP separator by one second choke valve; The gaseous phase outlet of described MP separator connects the gas phase entrance of described the first blender, and the liquid-phase outlet of described MP separator connects one second current divider; The first outlet of described the second current divider connects the entrance of described MP separator by the second pipeline in described ice chest, the second outlet of described the 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, and outlet connects a gas-liquid separator, a Natural gas expander and the contact tower in described heavy hydrocarbon piece-rate system successively; The liquid-phase outlet of described gas-liquid separator is connected the bottom entrance 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. a kind of marine natural gas expansion heavy hydrocarbon recovery system that is applicable to as claimed in claim 1, it is characterized in that: the liquid-phase outlet of described dethanizer first connects one first reboiler, then connect described the 5th choke valve by the liquid-phase outlet of described the first reboiler; The gaseous phase outlet of described the first reboiler connects back described dethanizer.
3. a kind of marine natural gas expansion heavy hydrocarbon recovery system that is applicable to as claimed in claim 1, 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 the second reboiler.
4. a kind of marine natural gas expansion heavy hydrocarbon recovery system that is applicable to as claimed in claim 2, 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 the 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. a kind of marine natural gas expansion heavy hydrocarbon recovery system that is applicable to as claimed in claim 5, is characterized in that: described ice chest is plate-fin heat exchanger.
8. the recovery process that be applicable to marine natural gas expansion heavy hydrocarbon recovery system of employing as described in claim 1～7 any one, it comprises the following steps:
1) in chilldown system, gas-liquid two-phase cold-producing medium is after low pressure separator separates, and gas phase enters the first blender after the first compressor boost, is mixed into the second compressor with the gas phase separating from MP separator; After the second compressor boost, enter the second blender, be mixed into the 3rd compressor with the gas phase separating from high-pressure separator; After the 3rd compressor boost, enter water cooler, through water cooler, cooling becomes liquid phase, and the cold-producing medium that becomes gas-liquid two-phase through first throttle valve decrease temperature and pressure enters high-pressure separator; High-pressure separator carries out after gas-liquid separation, and gas phase enters the second blender, and liquid phase enters the first current divider, enters high-pressure separator through a part of liquid phase of the first current divider shunting via the first pipeline in ice chest after cold is provided, and forms first order refrigeration;
2) after another part liquid phase of the first current divider shunting becomes gas-liquid two-phase via the second choke valve decrease temperature and pressure, enter MP separator; MP separator carries out after gas-liquid separation, and gas phase enters the first blender, and liquid phase enters the second current divider, enters MP separator through a part of liquid phase of the second current divider shunting via the second pipeline in ice chest after cold is provided, and forms second level refrigeration;
3) 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, enter low pressure separator; Low pressure separator carries out after gas-liquid separation, and 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 going out through gas-liquid separator separates enters the 4th pipeline in ice chest after the 7th choke valve decrease temperature and pressure, carries out entering after cooling the bottom entrance of contact tower, and the gas phase going 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 that obtains removing heavy hydrocarbon at the gaseous phase outlet of contact tower enters follow-up liquefaction unit, and the liquid phase heavy hydrocarbon of contact tower bottom enters dethanizer after the 4th choke valve step-down;
7) ethane that obtains removing heavy hydrocarbon at the tower top of dethanizer enters 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 processing again, and liquid phase stream enters debutanizing tower after the 5th choke valve step-down;
8) gas phase obtaining at the gaseous phase outlet of debutanizing tower, is back to debutanizing tower again through condenser condenses part liquid phase, and another part liquid phase enters in ice chest after the 5th pipeline cools, and after the 8th choke valve step-down is processed, enters LPG storage tank stores; The liquid phase of debutanizing tower bottom heats generation gas-liquid two-phase again through the second reboiler, and gas phase is back to carries out debutanization processing again in debutanizing tower, and liquid phase stream cools, enters NGL storage tank stores after the 6th choke valve step-down through cooler.
9. a kind of marine natural gas expansion heavy hydrocarbon recovery process that is applicable to as claimed in claim 8, is characterized in that: cold-producing medium adopts propane.
10. a kind of marine natural gas expansion heavy hydrocarbon recovery process that is applicable to as claimed in claim 9, is characterized in that: in described water cooler, adopt seawater as cooling media.
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