CN103868322A - Pre-cooling type heavy hydrocarbon recycling system and technology for offshore natural gas extraction - Google Patents

Pre-cooling type heavy hydrocarbon recycling system and technology for offshore natural gas extraction Download PDF

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Publication number
CN103868322A
CN103868322A CN201410080453.XA CN201410080453A CN103868322A CN 103868322 A CN103868322 A CN 103868322A CN 201410080453 A CN201410080453 A CN 201410080453A CN 103868322 A CN103868322 A CN 103868322A
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China
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liquid
phase
gas
heavy hydrocarbon
separator
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CN201410080453.XA
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CN103868322B (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
    • F25J3/0228—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
    • 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
    • F25J3/0242—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
    • 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
    • F25J2200/04—Processes or apparatus using separation by rectification in a dual 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
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/78—Refluxing the column with a liquid stream originating from an upstream or downstream fractionator 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
    • 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
    • F25J2215/64—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 invention relates to a pre-cooling type heavy hydrocarbon recycling system and technology for offshore natural gas extraction. The pre-cooling type heavy hydrocarbon recycling system is characterized by comprising a refrigerator, a pre-cooling system and a heavy hydrocarbon separation system, wherein three-level cooling is adopted by the pre-cooling system for supplying cooling energy to the heavy hydrocarbon separation system for processing natural gas and LPG (Liquefied Petroleum Gas). According to the technology, the cooling energy of a pre-cooling unit and the pressure of the high-pressure natural gas can be fully utilized to fully recycle heavy hydrocarbon in the natural gas, so that the propane recovery rate is increased, and better economical efficiency is achieved. The backflow of top gas phase to a contact tower is adopted by a deethanizer of the pre-cooling type heavy hydrocarbon recycling system, so that the heavy hydrocarbon is more fully removed from the natural gas in the heavy hydrocarbon separation system, and the efficiency of removing the heavy hydrocarbon from the natural gas is effectively increased. The inner equipment of the pre-cooling system and the heavy hydrocarbon separation system is compact and simple, process valves are fewer, and the mounting is convenient, so that the pre-cooling type heavy hydrocarbon recycling system is easily applied to the offshore operation. The pre-cooling type heavy hydrocarbon recycling system provided by the invention can be widely applied to a heavy hydrocarbon recycling technology for the high-pressure natural gas under an ocean production environment.

Description

A kind of pre-cooling type heavy hydrocarbon recovery system and technique for offshore natural gas exploitation
Technical field
The present invention relates to a kind of heavy hydrocarbon recovery system and technique, particularly about a kind of pre-cooling type heavy hydrocarbon recovery system and technique for offshore natural gas exploitation.
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 seabed relation can be subject to the restriction of cost and technology, therefore conventionally adopt LNG-FPSO(Liquefied natural gas-Floating Production Storage and Offloading, liquefied natural gas-Floating Production storage handler), this device has the migration of being convenient to, flexible configuration, reusable, production efficiency advantages of higher, the needs that can meet gas field, deep-sea, marginal gas field and the exploitation of low grade natural gas, make full use of petroleum resources.Therefore LNG-FPSO is widely used in especially gas field, deep-sea, the small-sized gas field development of China marine site.
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 component more than C6+(6 carbon hydrocarbon) constituent content meets liquefaction process requirement; 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 installing, and be not suitable for heavy hydrocarbon in the upper natural gas of LNG-FPSO and remove.
Summary of the invention
For the problems referred to above, the object of this invention is to provide the precooling of a kind of combination cold-producing medium, natural gas self expansion process and remove pre-cooling type heavy hydrocarbon recovery system and the technique for offshore natural gas exploitation that heavy hydrocarbon in high-pressure natural gas and deethanization top gaseous phase reflux.
For achieving the above object, the present invention takes following technical scheme: a kind of pre-cooling type heavy hydrocarbon recovery system for offshore natural gas exploitation, is characterized in that: it comprises an ice chest, a chilldown system and a heavy hydrocarbon piece-rate system; Seven 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 7th 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 connects the upper entrance of described contact tower successively by the 4th pipeline, one the 3rd blender in one the 4th choke valve, described ice chest; The gaseous phase outlet of described contact tower connects fuel gas for station by one the 4th blender, and liquid-phase outlet connects the upper entrance of a dethanizer by one the 5th choke valve; The gaseous phase outlet of described dethanizer connects described gas-liquid separator by the 5th pipeline in one the 4th compressor, described ice chest successively; The liquid-phase outlet of described gas-liquid separator also connects the upper entrance of contact tower by described the 3rd blender, gaseous phase outlet also connects fuel gas for station by described the 4th blender; The liquid-phase outlet of described dethanizer connects the upper entrance of one the 6th choke valve and a debutanizing tower successively; The liquid-phase outlet of described debutanizing tower connects a cooler, one the 7th choke valve and a NGL storage tank successively; The gaseous phase outlet of described debutanizing tower connects a condenser, and outlet one end of described condenser connects back described debutanizing tower, and the other end is connected a LPG storage tank by the 6th 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 for the recovery process of the pre-cooling type heavy hydrocarbon recovery system of offshore natural gas exploitation, 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) another part liquid phase that the second current divider is shunted becomes gas-liquid two-phase via the 3rd choke valve decrease temperature and pressure and enters low pressure separator; After low pressure separator carries out gas-liquid separation and goes out, 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 7th 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 4th choke valve decrease temperature and pressure, carries out after cooling entering the upper entrance of contact tower by the 3rd blender, 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 the 4th blender; The liquid phase heavy hydrocarbon of contact tower bottom enters dethanizer after the 5th choke valve step-down; 7) gas phase that obtains removing ethane at the tower top of dethanizer is after the 4th compressor compresses, enter in ice chest and to become gas-liquid two-phase after the 5th pipeline cooling and enter gas-liquid separator, through the liquid phase of gas-liquid separator separates with enter the 3rd blender through the cooling natural gas of the 4th pipeline, after mixing, enter the upper entrance of contact tower; Through mixing by the 4th blender with the gas phase of discharging from the gaseous phase outlet of contact tower, the gas phase of gas-liquid separator separates enters follow-up liquefaction unit; The liquid phase of dethanizer heats generation gas-liquid two-phase again through the first reboiler, and gas phase is back in dethanizer carries out deethanization processing again, and liquid phase stream enters debutanizing tower after the 6th choke valve step-down; 8) gas phase obtaining at the gaseous phase outlet of debutanizing tower, again be back to and in debutanizing tower, again carry out debutanization processing through condenser condenses part liquid phase, another part liquid phase enters in ice chest after the 6th 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 7th 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, in conjunction with the pressure energy of heavy hydrocarbon piece-rate system mesohigh natural gas self, and dethanizer adopts top gas phase to be back to contact tower, make the natural gas in heavy hydrocarbon piece-rate system can more fully remove heavy hydrocarbon, effectively improve the efficiency that removes heavy hydrocarbon from natural gas, reached good economy.The heavy hydrocarbon that heavy hydrocarbon piece-rate system of the present invention mainly utilizes gas-liquid separator, Natural gas expander, contact tower, dethanizer and debutanizing tower to realize high-pressure natural gas separates, this heavy hydrocarbon piece-rate system facility compact, simple, flow process valve member is few, is therefore highly suitable for removing of heavy hydrocarbon in FPSO high-pressure natural gas.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.
Accompanying drawing explanation
Fig. 1 is process flow diagram of the present invention
Fig. 2 is ice chest schematic internal view of the present invention
The specific embodiment
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 seven pipelines 11,12,13,14,15,16,17 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, the 3rd blender 45, the 4th blender 46, the 5th choke valve 47, dethanizer 48, the 4th compressor 49, gas-liquid separator 50, the 6th choke valve 51, debutanizing tower 52, cooler 53, the 7th choke valve 54, NGL (Natural Gas Liquid, gas reducing liquid) storage tank 55, the 8th choke valve 56 and LPG(Liquefied Petroleum Gas, liquefied petroleum gas) storage tank 57.
In ice chest 10, the entrance of the 7th pipeline 17 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 connects the upper entrance of contact tower 43 successively by the 4th pipeline 14, the 3rd blender 45 in the 4th choke valve 44, ice chest 10.The gaseous phase outlet of contact tower 43 connects fuel gas for station by the 4th blender 46, and liquid-phase outlet connects the upper entrance of dethanizer 48 by the 5th choke valve 47.The gaseous phase outlet of dethanizer 48 connects gas-liquid separator 50 by the 5th pipeline 15 in the 4th compressor 49, ice chest 10 successively.The liquid-phase outlet of gas-liquid separator 50 also connects the upper entrance of contact tower 43 by the 3rd blender 45, gaseous phase outlet also connects fuel gas for station by the 4th blender 46.The liquid-phase outlet of dethanizer 48 connects the upper entrance of the 6th choke valve 51 and debutanizing tower 52 successively.The liquid-phase outlet of debutanizing tower 52 connects cooler 53, the 7th choke valve 54 and NGL storage tank 55 successively; The gaseous phase outlet of debutanizing tower 52 connects a condenser 58, and outlet one end of condenser 58 connects back debutanizing tower 52, and the other end is connected LPG storage tank 57 by the 6th pipeline 16 in ice chest 10 with the 8th choke valve 56.
In above-described embodiment, the liquid-phase outlet of dethanizer 48 can first connect one first reboiler 59, then connects back dethanizer 48 by the gaseous phase outlet of the first reboiler 59 liquid-phase outlets connection the 6th choke valve 51, the first reboilers 59.The liquid-phase outlet of debutanizing tower 52 can first connect one second reboiler 60, then connects back debutanizing tower 52 by the gaseous phase outlet of the second reboiler 60 liquid-phase outlets connection cooler 53, the second reboilers 60.
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 47, the 6th choke valve 51, the 7th choke valve 54, the 8th choke valve 56 adopt J-T valve (joule-Thomson throttle expansion valve).
A kind of pre-cooling type heavy hydrocarbon recovery process for offshore natural gas exploitation 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 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 becomes gas-liquid two-phase via the 3rd choke valve 34 decrease temperature and pressure and enters low pressure separator 21; After low pressure separator 21 carries out gas-liquid separation and goes out, 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 7th pipeline 17 of ice chest 10, becomes gas-liquid two-phase enter gas-liquid separator 41 through ice chest 10 precooling coolings;
5) after the 4th choke valve 44 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 after cooling entering the upper entrance of contact tower 43 by the 3rd blender 45, 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 the 4th blender 46; The liquid phase heavy hydrocarbon of contact tower 43 bottoms enters dethanizer 48 after the 5th choke valve 47 step-downs;
7) gas phase that obtains removing ethane at the tower top of dethanizer 48 is after the 4th compressor 49 compressions, enter in ice chest 10 and to become gas-liquid two-phase after the 5th pipeline 15 coolings and enter gas-liquid separator 50, the liquid phase separating through gas-liquid separator 50 with enter the 3rd blender 45 through the cooling natural gas of the 4th pipeline 14, after mixing, enter the upper entrance of contact tower 43; The gas phase separating through gas-liquid separator 50 enters follow-up liquefaction unit mixing by the 4th blender 46 with the gas phase of discharging from the gaseous phase outlet of contact tower 43; The liquid phase of dethanizer 48 again heats and generates gas-liquid two-phase through the first reboiler 59, and gas phase is back in dethanizer 48 carries out deethanization processing again, and liquid phase stream enters debutanizing tower 52 after the 6th choke valve 51 step-downs;
8) gas phase obtaining at the gaseous phase outlet of debutanizing tower 52, again be back to and in debutanizing tower 47, again carry out debutanization processing through condenser 58 condensations parts liquid phases, another part liquid phase enters in ice chest 10 after the 6th pipeline 16 cools, and enters LPG storage tank 57 and store after the 8th choke valve 56 step-downs are processed.The liquid phase of debutanizing tower 52 bottoms again heats and generates gas-liquid two-phase through the second reboiler 60, and gas phase is back to carries out debutanization processing again in debutanizing tower 52, and liquid phase stream cools, enters NGL storage tank 55 after the 7th choke valve 54 step-downs and store through cooler 53.
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 for the liquid natural gas that separates through gas-liquid separator 41 after the 4th choke valve 44 decrease temperature and pressure in ice chest 10 process of refrigerastion.69～70 is the dethanizer 47 top reflux process that is cooled in ice chest 10.71～72 is the natural gas process that is cooled in ice chest 10.73～74 is the LPG process that is cooled in ice chest 10.
Enumerate a specific embodiment below:
1) in chilldown system 20, gas-liquid two-phase propane is after low pressure separator 21 separates, and gas phase enters the first blender 23 after the first compressor 22 is pressurized to 0.29MPa, 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 is pressurized to 1.36MPa, enter water cooler 27, be cooled to 31 ℃ through water cooler 27 and become after liquid phase, enter high-pressure separator 29 through the gas-liquid two-phase of first throttle valve 28 decrease temperature and pressure to 5 ℃, 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) after the gas-liquid two-phase of another part liquid phase that the first current divider 30 is shunted via extremely-15 ℃ of the second choke valve 31 decrease temperature and pressure, 0.29MPa, enter MP separator 32; 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 ℃ of the 3rd choke valve 34 decrease temperature and pressure, 0.13MPa; After low pressure separator 21 carries out gas-liquid separation and goes out, 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, after depickling processed 36 ℃, 7.14MPa natural gas via enter ice chest 10 by the 7th pipeline 17 of ice chest 10, become-32 ℃, the gas-liquid two-phase of 7.09MPa enter gas-liquid separator 41 through ice chest 10 precoolings coolings;
5) enter the 4th pipeline 14 in ice chest 10 through the isolated liquid phase of gas-liquid separator 41-40.14 ℃, 7.4MPa after the 4th choke valve 44 decrease temperature and pressure, carry out the upper entrance that temperature after cooling rewarming rises to 31 ℃, is depressurized to 4.65MPa and enters by the 3rd blender 45 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-55.35 ℃, 4.5MPa gas-liquid two-phase and enter contact tower 43, obtain removing 51.21 ℃ of heavy hydrocarbon, 4.4MPa natural gas at the gaseous phase outlet of contact tower 43 and enter the 4th blender 46;-55.44 ℃ of contact tower 43 bottoms, 4.45MPa liquid phase heavy hydrocarbon enter dethanizer 48 after the 5th choke valve 47 is depressurized to 2.95MPa;
7) obtain removing-23.15 ℃ of ethane, 2.85MPa gas phase after the 4th compressor 49 is compressed to 7.7 ℃, 4.45MPa at the tower top of dethanizer 48, entering in ice chest 10 the 5th pipeline 15 is down to and becomes gas-liquid two-phase after-32 ℃, 4.4MPa and enter gas-liquid separator 50, the liquid phase that gas-liquid separator 50 separates and the upper entrance that enters contact tower 43 after cooling natural gas via the 3rd blender 45 of the 4th pipeline 14 in ice chest 10 mixes;-52.74 ℃ of formation separate through gas-liquid separator 50 51.21 ℃, 4.4MPa gas phase mix by the 4th blender 46 with the gas phase of discharging from the gaseous phase outlet of contact tower 43,4.4MPa enter follow-up liquefaction unit; The liquid phase of dethanizer 48 again heats and generates gas-liquid two-phase through the first reboiler 59, and gas phase is back to carries out deethanization processing again in dethanizer 48, and 115 ℃, the liquid phase stream of 2.9MPa enter debutanizing tower 52 after the 6th choke valve 51 is depressurized to 0.65MPa;
8) gas phase obtaining at the gaseous phase outlet of debutanizing tower 52, again be back to and in debutanizing tower 47, again carry out debutanization processing through condenser 58 condensations parts liquid phases, the liquid phase of 15.04 ℃ of another part, 0.55MPa enters the 6th pipeline 16 in ice chest 10 and cools after-32 ℃, enters LPG storage tank 57 and store after the 8th choke valve 56 is depressurized to 0.12MPa.120 ℃ of debutanizing tower 52 bottoms, 0.6MPa liquid phase again heat and generate gas-liquid two-phase through the second reboiler 60, gas phase is back to carries out debutanization processing again in debutanizing tower 52, liquid phase stream cools to-32 ℃, the 7th choke valve 54 and after being depressurized to 0.12MPa, enters NGL storage tank 55 and store through cooler 53.
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. for a pre-cooling type heavy hydrocarbon recovery system for offshore natural gas exploitation, it is characterized in that: it comprises an ice chest, a chilldown system and a heavy hydrocarbon piece-rate system;
Seven 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 7th 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 connects the upper entrance of described contact tower successively by the 4th pipeline, one the 3rd blender in one the 4th choke valve, described ice chest; The gaseous phase outlet of described contact tower connects fuel gas for station by one the 4th blender, and liquid-phase outlet connects the upper entrance of a dethanizer by one the 5th choke valve; The gaseous phase outlet of described dethanizer connects described gas-liquid separator by the 5th pipeline in one the 4th compressor, described ice chest successively; The liquid-phase outlet of described gas-liquid separator also connects the upper entrance of contact tower by described the 3rd blender, gaseous phase outlet also connects fuel gas for station by described the 4th blender; The liquid-phase outlet of described dethanizer connects the upper entrance of one the 6th choke valve and a debutanizing tower successively; The liquid-phase outlet of described debutanizing tower connects a cooler, one the 7th choke valve and a NGL storage tank successively; The gaseous phase outlet of described debutanizing tower connects a condenser, and outlet one end of described condenser connects back described debutanizing tower, and the other end is connected a LPG storage tank by the 6th pipeline in described ice chest with one the 8th choke valve.
2. a kind of pre-cooling type heavy hydrocarbon recovery system for offshore natural gas exploitation 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 pre-cooling type heavy hydrocarbon recovery system for offshore natural gas exploitation as claimed in claim 1, it is characterized in that: the liquid-phase outlet of described debutanizing tower first connects one second reboiler, then connect described cooler by the liquid-phase outlet of described the second reboiler.
4. a kind of pre-cooling type heavy hydrocarbon recovery system for offshore natural gas exploitation as claimed in claim 2, it is characterized in that: the liquid-phase outlet of described debutanizing tower first connects one second reboiler, then connect described cooler by the liquid-phase outlet of described the second reboiler.
5. a kind of pre-cooling type heavy hydrocarbon recovery system for offshore natural gas exploitation as claimed in claim 1 or 2 or 3 or 4, is characterized in that: described Natural gas expander is turbo-expander.
6. a kind of pre-cooling type heavy hydrocarbon recovery system for offshore natural gas exploitation as claimed in claim 1 or 2 or 3 or 4, is characterized in that: described ice chest is plate-fin heat exchanger.
7. a kind of pre-cooling type heavy hydrocarbon recovery system for offshore natural gas exploitation as claimed in claim 5, is characterized in that: described ice chest is plate-fin heat exchanger.
8. a recovery process for the pre-cooling type heavy hydrocarbon recovery system for offshore natural gas exploitation 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) another part liquid phase that the second current divider is shunted becomes gas-liquid two-phase via the 3rd choke valve decrease temperature and pressure and enters low pressure separator; After low pressure separator carries out gas-liquid separation and goes out, 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 7th 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 4th choke valve decrease temperature and pressure, carries out after cooling entering the upper entrance of contact tower by the 3rd blender, 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 the 4th blender; The liquid phase heavy hydrocarbon of contact tower bottom enters dethanizer after the 5th choke valve step-down;
7) gas phase that obtains removing ethane at the tower top of dethanizer is after the 4th compressor compresses, enter in ice chest and to become gas-liquid two-phase after the 5th pipeline cooling and enter gas-liquid separator, through the liquid phase of gas-liquid separator separates with enter the 3rd blender through the cooling natural gas of the 4th pipeline, after mixing, enter the upper entrance of contact tower; Through mixing by the 4th blender with the gas phase of discharging from the gaseous phase outlet of contact tower, the gas phase of gas-liquid separator separates enters follow-up liquefaction unit; The liquid phase of dethanizer heats generation gas-liquid two-phase again through the first reboiler, and gas phase is back in dethanizer carries out deethanization processing again, and liquid phase stream enters debutanizing tower after the 6th choke valve step-down;
8) gas phase obtaining at the gaseous phase outlet of debutanizing tower, again be back to and in debutanizing tower, again carry out debutanization processing through condenser condenses part liquid phase, another part liquid phase enters in ice chest after the 6th 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 7th choke valve step-down through cooler.
9. a kind of pre-cooling type heavy hydrocarbon recovery process for offshore natural gas exploitation as claimed in claim 8, is characterized in that: cold-producing medium adopts propane.
10. a kind of pre-cooling type heavy hydrocarbon recovery process for offshore natural gas exploitation as claimed in claim 9, is characterized in that: in described water cooler, adopt seawater as cooling media.
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