CN111964353B - Natural gas liquefaction and condensate recovery integrated device and method - Google Patents

Natural gas liquefaction and condensate recovery integrated device and method Download PDF

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Publication number
CN111964353B
CN111964353B CN202010841396.8A CN202010841396A CN111964353B CN 111964353 B CN111964353 B CN 111964353B CN 202010841396 A CN202010841396 A CN 202010841396A CN 111964353 B CN111964353 B CN 111964353B
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China
Prior art keywords
heavy hydrocarbon
enters
cold box
pipeline
demethanizer
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CN202010841396.8A
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Chinese (zh)
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CN111964353A (en
Inventor
王科
韩淑怡
李莹珂
郑春来
蒋志明
蒲黎明
周璇
尹奎
汪贵
田静
陈运强
赵雨亮
李嘉迪
杨苗
陈凯文
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China National Petroleum Corp
China Petroleum Engineering and Construction Corp
China Petroleum Engineering Co Ltd
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China National Petroleum Corp
China Petroleum Engineering and Construction Corp
China Petroleum Engineering Co Ltd
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Priority to CN202010841396.8A priority Critical patent/CN111964353B/en
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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
    • F25J3/0247—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
    • F25J3/08—Separating gaseous impurities from gases or gaseous mixtures or from liquefied gases or liquefied gaseous mixtures
    • 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
    • F25J2200/74—Refluxing the column with at least a part of the partially condensed overhead gas
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/76—Refluxing the column with condensed overhead gas being cycled in a quasi-closed loop refrigeration cycle
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • 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
    • 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
    • F25J2215/04—Recovery of liquid products
    • 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
    • F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
    • F25J2230/60—Processes or apparatus involving steps for increasing the pressure of gaseous process streams the fluid being hydrocarbons or a mixture of 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
    • F25J2240/00—Processes or apparatus involving steps for expanding of process streams
    • F25J2240/02—Expansion of a process fluid in a work-extracting turbine (i.e. isentropic expansion), e.g. of the feed stream
    • 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
    • F25J2260/00—Coupling of processes or apparatus to other units; Integrated schemes
    • F25J2260/20—Integration in an installation for liquefying or solidifying a fluid stream
    • 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
    • F25J2270/66—Closed external refrigeration cycle with multi component refrigerant [MCR], e.g. mixture of hydrocarbons

Abstract

The invention discloses an integrated device and a method for liquefying natural gas and recycling condensate, comprising a liquefied cold box, a heavy hydrocarbon removal tower reflux tank and a condensate recycling unit, wherein the liquefied cold box is connected with a natural gas pipeline and the heavy hydrocarbon removal tower, a top gas phase outlet of the heavy hydrocarbon removal tower is connected with the liquefied cold box, the liquefied cold box is connected with the heavy hydrocarbon removal tower reflux tank, a liquid phase outlet of the heavy hydrocarbon removal tower reflux tank is connected with the upper part of the heavy hydrocarbon removal tower through a pipeline provided with a heavy hydrocarbon removal tower reflux pump, and the condensate recycling unit is used for further recycling heavy hydrocarbon from the natural gas after heavy hydrocarbon removal and sending the treated natural gas back to a condensing section of the liquefied cold box. The invention adopts the heavy hydrocarbon removal tower to remove C in the natural gas 5 + Heavy hydrocarbon components to avoid equipment and pipeline freezing blockage in the natural gas liquefaction process, and the natural gas subjected to heavy hydrocarbon removal is subjected to extraction of ethane, propane, butane and the like through a condensate recovery unit. The invention is applicable to one or more hydrocarbon mixtures such as coal bed gas, coke oven gas and the like besides natural gas.

Description

Natural gas liquefaction and condensate recovery integrated device and method
Technical Field
The invention belongs to the technical field of natural gas liquefaction and natural gas condensate recovery, and particularly relates to a natural gas liquefaction and condensate recovery integrated device and method.
Background
Methane in natural gas is the vast majority, and small amounts of ethane, propane and butane, and trace amounts of pentane, hexane and other components. The natural gas condensate recovery means that ethane, propane, butane, pentane and the like in the natural gas are separated from the natural gas, and the recovered condensate is used for chemical raw materials, so that the natural gas condensate has good economic benefit. The natural gas liquefaction is to produce liquefied natural gas after the purification treatment is condensed and liquefied at low temperature. Because natural gas contains heavy hydrocarbon components, the heavy hydrocarbon components refer to C 5 + Hydrocarbons, which are condensed and frozen in a low temperature environment to block pipelines and equipment due to the low melting point of heavy hydrocarbons,therefore, the heavy hydrocarbon components contained in the natural gas must be removed in the liquefaction process, so as to avoid the natural gas from being frozen and blocked in the liquefaction process, and the natural gas after the heavy hydrocarbon removal is further condensed and liquefied to produce liquefied natural gas.
In addition, the natural gas liquefaction plant needs to supplement refrigerants such as ethane, propane and the like, so a condensate recovery unit can be arranged after the heavy hydrocarbon removal tower to extract components such as ethane, propane and the like from the natural gas for refrigerant supplementation. Meanwhile, the established natural gas liquefaction engineering can extract ethane, propane, butane and the like at the lowest marginal cost by reducing the high-order heating value (HHV) in the liquefied natural gas product, and can be added with a condensate recovery device after a heavy hydrocarbon removal tower to produce the ethane, propane, butane and the like at the lowest cost with the minimum investment.
Disclosure of Invention
The invention aims at: aiming at the problems, the integrated device and the method for natural gas liquefaction and condensate recovery can avoid equipment and pipeline freezing blockage in the natural gas liquefaction process and extract ethane, propane, butane and the like from natural gas subjected to heavy hydrocarbon removal.
The technical scheme adopted by the invention is as follows: the utility model provides a natural gas liquefaction and lime set recovery integrated device which characterized in that: including the liquefaction cold box, take off the heavy hydrocarbon tower, take off heavy hydrocarbon tower reflux drum and condensate recovery unit, the one-level precooling section entrance point and the natural gas inlet pipeline of liquefaction cold box are connected, and its exit end passes through the pipeline and takes off the heavy hydrocarbon tower and be connected, liquid hydrocarbon after taking off the heavy hydrocarbon tower separation gets into the back process through the bottom pipeline, the top gaseous phase export of taking off the heavy hydrocarbon tower passes through the pipeline and is connected with the second grade precooling section entrance point in the liquefaction cold box, the exit end of second grade precooling section passes through the pipeline and takes off the heavy hydrocarbon tower reflux drum and is connected, the liquid phase export of taking off the heavy hydrocarbon tower reflux drum is through being provided with the pipeline of taking off heavy hydrocarbon tower reflux pump and take off heavy hydrocarbon tower upper portion connection, the gaseous phase export of taking off the heavy hydrocarbon tower reflux drum divide into two-way, the pipeline through being provided with first choke is connected with the condensate section entrance point in the liquefaction cold box all the way, the exit end of condensate section passes through the pipeline to the back process, and another way passes through the pipeline and is connected with condensate recovery unit, condensate recovery unit is used for further retrieving the liquefied natural gas after the heavy hydrocarbon to take off the heavy hydrocarbon to be treated condensate back to the condensate recovery unit.
The invention relates to an integrated device for liquefying natural gas and recycling condensate, wherein a liquefied cold box is connected with a refrigerant refrigerating unit, the refrigerant refrigerating unit comprises a first cooler and a refrigerant compressor, the first cooler is connected with a cooling section in the liquefied cold box, the cooling section is connected with a reheating section in the liquefied cold box through a pipeline provided with a second throttle valve, the reheating section is connected with the refrigerant compressor through a pipeline, and the refrigerant compressor is connected with the first cooler through a pipeline to form a refrigerant refrigerating cycle loop.
The invention discloses a natural gas liquefaction and condensate recovery integrated device, which comprises a heavy hydrocarbon recovery cold box, a low-temperature separator and a demethanizer, wherein one path of gas phase of a heavy hydrocarbon removal tower reflux tank is connected with the inlet end of a first-stage precooling section in the heavy hydrocarbon recovery cold box through a pipeline, the outlet end of the first-stage precooling section in the heavy hydrocarbon recovery cold box is connected with the low-temperature separator through a pipeline, the bottom liquid phase outlet of the low-temperature separator is connected with the demethanizer through a pipeline provided with a third throttle valve, the top gas phase outlet of the low-temperature separator is divided into two paths, one path of gas phase is connected with the inlet end of a second-stage precooling section in the heavy hydrocarbon recovery cold box through a pipeline, the outlet end of the second-stage precooling section in the heavy hydrocarbon recovery cold box is connected with the upper part of the demethanizer through a pipeline provided with a fourth throttle valve, the other path of gas phase outlet of the heavy hydrocarbon recovery cold box is connected with the inlet end of a recovery cold section in the heavy hydrocarbon recovery cold box through a pipeline after expansion machine, and the gas phase outlet of the heavy hydrocarbon recovery cold box is further connected with the cooling section through a compressor and the cooling section of the cooling section in turn, and the cooling section of the cooling tower is further connected with the cooling section of the heavy hydrocarbon recovery cold box through a cooling section.
According to the natural gas liquefaction and condensate recovery integrated device, the gas phase at the top of the demethanizer is divided into two paths after being cooled by the second cooler, one path of the gas phase is sent back to the heavy hydrocarbon recovery cold box, the other path of the gas phase is connected with the inlet end of the cooling section in the heavy hydrocarbon recovery cold box through a pipeline, and the outlet end of the cooling section in the heavy hydrocarbon recovery cold box is connected with the upper part of the demethanizer through a pipeline provided with a fifth throttle valve.
The liquid phase outlet in the middle of the demethanizer is connected with the inlet end of a heating section in a heavy hydrocarbon recovery cold box through a pipeline, and the outlet end of the heating section in the heavy hydrocarbon recovery cold box is connected with the liquid phase inlet in the middle of the demethanizer through a pipeline.
The invention relates to an integrated device for liquefying natural gas and recycling condensate, wherein a liquid phase outlet at the lower part of a demethanizer is connected with a liquid phase inlet at the lower part of the demethanizer through a pipeline provided with a reboiler of the demethanizer.
The integrated method for liquefying natural gas and recovering condensate is characterized by comprising the following steps of: the method comprises the following steps:
firstly, natural gas from a natural gas inlet pipeline enters a liquefaction cold box for precooling to-25 to-45 ℃, then enters a heavy hydrocarbon removal tower for separation, liquid hydrocarbon at the bottom of the heavy hydrocarbon removal tower enters a next process for treatment, gas phase at the top of the heavy hydrocarbon removal tower enters the liquefaction cold box for precooling to-50 to-65 ℃, then enters a heavy hydrocarbon removal tower reflux tank for gas-liquid separation, wherein: the liquid phase is pressurized by a heavy hydrocarbon removal tower reflux pump and then enters the top of the heavy hydrocarbon removal tower, the gas phase is divided into two paths according to any proportion, one path is throttled to be 350-5500 kPa.a by a first throttle valve, enters a liquefaction cooling box and is further condensed to be between-150 and-162 ℃, and then enters the next working procedure for treatment; the other path enters a heavy hydrocarbon recovery cold box for precooling to-50 to-70 ℃ and then further recovering the heavy hydrocarbon;
secondly, entering a heavy hydrocarbon recovery cold box for precooling to-50 to-70 ℃, and then entering a low-temperature separator for gas-liquid separation, wherein: the liquid phase is throttled to 1000 kPa.a-3500kPa.a by a third throttle valve and then enters the middle part of the demethanizer, the gas phase is divided into two paths, one path of 1-30% material flow enters a heavy hydrocarbon recovery cold box to be cooled to minus 95-minus 125 ℃, enters a fourth throttle valve to be throttled to 1000 kPa.a-3500kPa.a and then enters the upper part of the demethanizer, and the other path of 70-99% material flow enters an expansion machine to be expanded to 1000 kPa.a-3500kPa.a and then enters the upper part of the demethanizer; the gas phase at the top outlet of the demethanizer enters a heavy hydrocarbon recovery cold box for reheating to 25-40 ℃, is pressurized by an expander, enters a dry gas compressor for pressurizing to 4000 kPa.a-6000 kPa.a, enters a second cooler for cooling to 40-50 ℃, enters a heavy hydrocarbon recovery cold box for cooling to-20 to-40 ℃, and enters a liquefaction cold box for liquefaction;
and thirdly, the refrigerant from the first cooler enters the liquefaction cooling tank to be cooled to-150 to-162 ℃, enters the second throttling valve through a pipeline to be throttled to 300-500 kPa.a, enters the liquefaction cooling tank to be reheated to 35-45 ℃, enters the refrigerant compressor through the pipeline to be pressurized to 350 kPa.a-5000 kPa.a, enters the first cooler to be cooled to 40-50 ℃ and then enters the liquefaction cooling tank, and the refrigerant refrigeration cycle is formed to provide the required cooling capacity for the liquefaction cooling tank.
In the second step, the gas phase at the top outlet of the demethanizer is cooled by a second cooler and then is divided into two paths, wherein 80-95% of the gas phase enters a heavy hydrocarbon recovery cold box for cooling to-20 to-40 ℃, then enters a liquefaction cold box for liquefaction, and the other 5-20% of the gas phase enters a heavy hydrocarbon recovery cold box for cooling to-95 to-125 ℃, enters a fifth throttle valve for throttling to 1000kPa.a to 3500kPa.a and then enters the top of the demethanizer.
In the second step, the liquid phase in the middle of the demethanizer enters a heavy hydrocarbon recovery cold box to be heated and then returns to the middle inlet of the demethanizer, so that the cold in the demethanizer is recovered.
In the second step, the liquid phase at the bottom of the demethanizer enters a reboiler of the demethanizer and is heated and then returns to an inlet at the bottom of the demethanizer, so that the content of methane in the liquid phase at the bottom of the demethanizer is controlled, and the liquid phase at the bottom of the demethanizer enters the next working procedure for treatment.
Compared with the prior art, the invention has the following positive effects: removal of C in natural gas by heavy hydrocarbon removal tower 5 + Heavy hydrocarbon composition to avoid equipment and pipeline freezing and blocking in the natural gas liquefaction process, and the composition of extracting ethane, propane, butane and the like from the natural gas subjected to heavy hydrocarbon removal by arranging a condensate recovery unit, wherein the condensate recovery unit is used for recovering the condensateThe natural gas after the element is further condensed and liquefied to produce liquefied natural gas, and the flexible switching of the natural gas liquefaction under the condition of the presence or absence of a condensate recovery unit can be realized. The invention is applicable to one or more hydrocarbon mixtures such as coal bed gas, coke oven gas and the like besides natural gas.
Drawings
The invention will be described by way of specific embodiments and with reference to the accompanying drawings in which
Fig. 1 is a schematic diagram of embodiment 1 of the present invention.
Fig. 2 is a schematic diagram of embodiment 2 of the present invention.
The marks in the figure: 1 is a natural gas inlet pipeline, 2 is a liquefaction cold box, 4 is a heavy hydrocarbon removal tower, 7 is a heavy hydrocarbon removal tower reflux drum, 9 is a heavy hydrocarbon removal tower reflux pump, 12 is a first throttle valve, 18 is a second throttle valve, 21 is a refrigerant compressor, 23 is a first cooler, 25 is a heavy hydrocarbon recovery cold box, 27 is a low-temperature separator, 29 is a third throttle valve, 31 is a demethanizer, 33 is an expander, 37 is a fourth throttle valve, 42 is a dry gas compressor, 44 is a second cooler, 49 is a fifth throttle valve, and 54 is a demethanizer reboiler.
Detailed Description
For the purpose of making the objects, technical solutions and advantages of the embodiments of the present invention more apparent, the technical solutions of the embodiments of the present invention will be clearly and completely described below with reference to the accompanying drawings in the embodiments of the present invention, and it is apparent that the described embodiments are some embodiments of the present invention, but not all embodiments of the present invention. The components of the embodiments of the present invention generally described and illustrated in the figures herein may be arranged and designed in a wide variety of different configurations.
Thus, the following detailed description of the embodiments of the invention, as presented in the figures, is not intended to limit the scope of the invention, as claimed, but is merely representative of selected embodiments of the invention. All other embodiments, which can be made by those skilled in the art based on the embodiments of the invention without making any inventive effort, are intended to be within the scope of the invention.
It should be noted that, without conflict, the embodiments of the present invention and features of the embodiments may be combined with each other.
It should be noted that: like reference numerals and letters denote like items in the following figures, and thus once an item is defined in one figure, no further definition or explanation thereof is necessary in the following figures.
In the description of the embodiments of the present invention, it should be noted that, the indicated orientation or positional relationship is based on the orientation or positional relationship shown in the drawings, or the orientation or positional relationship conventionally put in use of the product of the present invention as understood by those skilled in the art, merely for convenience of describing the present invention and simplifying the description, and is not indicative or implying that the apparatus or element to be referred to must have a specific orientation, be configured and operated in a specific orientation, and therefore should not be construed as limiting the present invention. Furthermore, the terms "first," "second," and the like, are used merely for distinguishing between descriptions and not for understanding as indicating or implying a relative importance.
In the description of the embodiments of the present invention, it should also be noted that, unless explicitly specified and limited otherwise, the terms "disposed," "connected," and "connected" are to be construed broadly, and may be, for example, fixedly connected, detachably connected, or integrally connected; may be directly connected or indirectly connected through an intermediate medium. The specific meaning of the above terms in the present invention will be understood in detail by those skilled in the art; the accompanying drawings, which are included to provide a further understanding of the invention and are incorporated in and constitute a part of this specification, illustrate embodiments of the invention and together with the description serve to explain the principles of the invention. The components of the embodiments of the present invention generally described and illustrated in the figures herein may be arranged and designed in a wide variety of different configurations.
Example 1:
as shown in fig. 1, an integrated device is retrieved to natural gas liquefaction and lime set, including liquefaction cold box 2, take off heavy hydrocarbon tower 4, take off heavy hydrocarbon tower reflux drum 7 and lime set recovery unit, the one-level precooling section entrance point in the liquefaction cold box 2 is connected with natural gas admission line 1, and its exit end passes through the pipeline and takes off heavy hydrocarbon tower 4 and is connected, and liquid hydrocarbon after taking off heavy hydrocarbon tower 4 separation passes through the bottom pipeline and gets into the back process, take off the gaseous phase export in the top of heavy hydrocarbon tower 4 and pass through the pipeline and be connected with the second grade precooling section entrance point in the liquefaction cold box 2, the exit end of second grade precooling section is connected through pipeline and take off heavy hydrocarbon tower reflux drum 7, take off the liquid phase export of heavy hydrocarbon tower reflux drum 7 through be provided with take off heavy hydrocarbon tower reflux drum 9 the pipeline and take off heavy hydrocarbon tower 4 upper portion and be connected, take off heavy hydrocarbon tower reflux drum 7's gaseous phase export divide into two routes, be connected with the condensation section entrance point in the cold box 2 through the pipeline that is provided with first choke 12, the exit end of condensation section passes through pipeline to the back process, another route passes through pipeline and is connected with lime set recovery unit for the gas recovery unit to take off heavy hydrocarbon 2 after the gas recovery unit.
The liquefied cooling tank 2 is connected with a refrigerant refrigerating unit, the refrigerant refrigerating unit comprises a first cooler 23 and a refrigerant compressor 21, the first cooler 23 is connected with a cooling section in the liquefied cooling tank 2, the cooling section is connected with a reheating section in the liquefied cooling tank 2 through a pipeline provided with a second throttle valve 18, the reheating section is connected with the refrigerant compressor 21 through a pipeline, and the refrigerant compressor 21 is connected with the first cooler 23 through a pipeline to form a refrigerant refrigerating cycle loop.
In this embodiment, the condensate recovery unit includes heavy hydrocarbon recovery cold box 25, low temperature separator 27 and demethanizer 31, the gaseous phase of one way of heavy hydrocarbon recovery cold box 25 is connected with the one-level precooling section entrance point in the heavy hydrocarbon recovery cold box 25 through the pipeline, the one-level precooling section exit end in the heavy hydrocarbon recovery cold box 25 passes through the pipeline and is connected with low temperature separator 27, the bottom liquid phase export of low temperature separator 27 is connected with demethanizer 31 through the pipeline that is provided with third choke 29, the gaseous phase export in the top of low temperature separator 27 divide into two ways, and the gaseous phase export of one way is connected with the second grade precooling section entrance point in the heavy hydrocarbon recovery cold box 25 through the pipeline, the second grade precooling section exit end in the heavy hydrocarbon recovery cold box 25 is connected with demethanizer 31 upper portion through the pipeline that is provided with fourth choke 37, and is connected with demethanizer 31 through pipeline after the expansion of expander 33, the top export of demethanizer 31 passes through the pipeline and is connected with the multiplex section in the cold box 25, the gaseous phase of the pipeline is connected with the second grade cooling section entrance point in proper order through the compressor and the second cooling section 2, and the second cooling section is connected with the heavy hydrocarbon recovery cold box 2 in proper order through the pipeline and the compressor cooling section cooling end of the second cooling section cooling tank 2.
The middle liquid phase outlet of the demethanizer 31 is connected with the inlet end of the heating section in the heavy hydrocarbon recovery cold box 25 through a pipeline, and the outlet end of the heating section in the heavy hydrocarbon recovery cold box 25 is connected with the middle liquid phase inlet of the demethanizer 31 through a pipeline; the lower liquid phase outlet of the demethanizer 31 is connected to the lower liquid phase inlet of the demethanizer 31 by a conduit provided with a demethanizer reboiler 54.
Based on the integrated device for natural gas liquefaction and condensate recovery, the invention also provides a method for natural gas liquefaction and condensate recovery integration, which comprises the following steps:
firstly, natural gas from a natural gas inlet pipeline is led into a liquefaction cold box for precooling to minus 25 ℃ to minus 45 ℃ and then is led into the lower part of a heavy hydrocarbon removal tower for separation, liquid hydrocarbon at the bottom of the heavy hydrocarbon removal tower is led into the next process for treatment, gas phase at the top of the heavy hydrocarbon removal tower is led into the liquefaction cold box for precooling to minus 50 ℃ to minus 65 ℃ and then is led into a heavy hydrocarbon removal tower reflux tank for gas-liquid separation, wherein: the liquid phase enters the top of the heavy hydrocarbon removal tower after being pressurized by a heavy hydrocarbon removal tower reflux pump, and the gas phase is divided into two paths according to any proportion, so that flexible switching of natural gas liquefaction and condensate recovery can be realized, and when condensate recovery is not needed, the gas phase completely enters a liquefaction cold box through a first throttle valve; when condensate recovery is needed, the gas phase can be controlled to fully enter or partially enter a heavy hydrocarbon recovery cold box according to the requirement, specifically, one path of the gas phase is throttled to be 350-5500 kPa.a by a first throttle valve and enters a liquefaction cold box to be further condensed to be between-150 and-162 ℃ and then enters the next working procedure for treatment; the other path enters a heavy hydrocarbon recovery cold box for precooling to-50 to-70 ℃ and then further recovering the heavy hydrocarbon.
Secondly, entering a heavy hydrocarbon recovery cold box for precooling to-50 to-70 ℃, and then entering a low-temperature separator for gas-liquid separation, wherein: the liquid phase is throttled to 1000 kPa.a-3500kPa.a by a third throttle valve and then enters the middle part of the demethanizer, the gas phase is divided into two paths, one path of 1-30% material flow enters a heavy hydrocarbon recovery cold box to be cooled to minus 95-minus 125 ℃, enters a fourth throttle valve to be throttled to 1000 kPa.a-3500kPa.a and then enters the upper part of the demethanizer, and the other path of 70-99% material flow enters an expansion machine to be expanded to 1000 kPa.a-3500kPa.a and then enters the upper part of the demethanizer; the gas phase at the top outlet of the demethanizer enters a heavy hydrocarbon recovery cold box for reheating to 25-40 ℃, is pressurized by an expander, enters a dry gas compressor for pressurizing to 4000 kPa.a-6000 kPa.a, enters a second cooler for cooling to 40-50 ℃, enters a heavy hydrocarbon recovery cold box for cooling to-20 to-40 ℃, and enters a liquefaction cold box for liquefaction.
The liquid phase in the middle of the demethanizer enters the heavy hydrocarbon recovery cold box and returns to the inlet in the middle of the demethanizer after being heated, the cold in the demethanizer is recovered, the liquid phase in the lower part of the demethanizer enters the reboiler of the demethanizer and returns to the inlet in the lower part of the demethanizer after being heated, the content of methane in the liquid phase at the bottom of the demethanizer is controlled, and the liquid phase at the bottom of the demethanizer enters the next process for treatment.
And thirdly, the refrigerant from the first cooler enters the liquefaction cooling tank to be cooled to-150 to-162 ℃, enters the second throttling valve through a pipeline to be throttled to 300-500 kPa.a, enters the liquefaction cooling tank to be reheated to 35-45 ℃, enters the refrigerant compressor through the pipeline to be pressurized to 350 kPa.a-5000 kPa.a, enters the first cooler to be cooled to 40-50 ℃ and then enters the liquefaction cooling tank, and the refrigerant refrigeration cycle is formed to provide the required cooling capacity for the liquefaction cooling tank.
Example 2:
as shown in fig. 2, embodiment 2 is substantially the same as embodiment 1, with the main difference that: the gaseous phase at demethanizer 31 top is divided into two after the cooling of second cooler 44, and heavy hydrocarbon recovery cold box 25 is returned to one way, and another way passes through the pipeline and is connected with the cooling section entrance point in the heavy hydrocarbon recovery cold box 25, the cooling section exit end in the heavy hydrocarbon recovery cold box 25 is connected with demethanizer 31 upper portion through the pipeline that is provided with fifth choke valve 49.
Based on the difference of the structural design, the natural gas liquefaction and condensate recovery integration method is mainly different in that: in the second step, the gas phase at the outlet of the top of the demethanizer is cooled by a second cooler and then is divided into two paths, wherein 80-95% of the gas phase enters a heavy hydrocarbon recovery cold box to be cooled to minus 20-minus 40 ℃ and then enters a liquefaction cold box to be liquefied, and the other 5-20% of the gas phase enters the heavy hydrocarbon recovery cold box to be cooled to minus 95-minus 125 ℃, enters a fifth throttle valve to be throttled to 1000 kPa.a-2500 kPa.a and then enters the top of the demethanizer.
The invention is not limited to the specific embodiments described above. The invention extends to any novel one, or any novel combination, of the features disclosed in this specification, as well as to any novel one, or any novel combination, of the steps of the method or process disclosed.

Claims (7)

1. The utility model provides a natural gas liquefaction and lime set recovery integrated device which characterized in that: including liquefied cold box (2), take off heavy hydrocarbon tower (4), take off heavy hydrocarbon tower reflux drum (7) and condensate recovery unit, the one-level precooling section entrance point in liquefied cold box (2) is connected with natural gas admission line (1), and the one-level precooling section exit end in liquefied cold box (2) is connected with take off heavy hydrocarbon tower (4) through the pipeline, and liquid hydrocarbon after taking off heavy hydrocarbon tower (4) separation gets into the back process through the bottom pipeline, the top gaseous phase export of taking off heavy hydrocarbon tower (4) is connected with the second grade precooling section entrance point in liquefied cold box (2) through the pipeline, the exit end of second grade precooling section is connected with take off heavy hydrocarbon tower reflux drum (7) through the pipeline, the liquid phase export of taking off heavy hydrocarbon tower reflux drum (7) is connected with take off heavy hydrocarbon tower (4) upper portion through the pipeline that is provided with take off heavy hydrocarbon tower reflux pump (9), and the gas phase export of taking off heavy hydrocarbon tower reflux drum (7) divide into two routes, one way is through the pipeline that is provided with first choke valve (12) and condensate tank (2) in the condensate recovery unit, the condensate is connected with the condensate recovery unit through the pipeline to the back of condensate recovery unit;
the condensate recovery unit comprises a heavy hydrocarbon recovery cold box (25), a low-temperature separator (27) and a demethanizer (31), one path of gas phase of a heavy hydrocarbon removal tower reflux tank (7) is connected with the inlet end of a first-stage precooling section in the heavy hydrocarbon recovery cold box (25) through a pipeline, the outlet end of the first-stage precooling section in the heavy hydrocarbon recovery cold box (25) is connected with the low-temperature separator (27) through a pipeline, the bottom liquid phase outlet of the low-temperature separator (27) is connected with the demethanizer (31) through a pipeline provided with a third throttle valve (29), the top gas phase outlet of the low-temperature separator (27) is divided into two paths, one path of gas phase is connected with the inlet end of a second-stage precooling section in the heavy hydrocarbon recovery cold box (25) through a pipeline, the outlet end of the second-stage precooling section in the heavy hydrocarbon recovery cold box (25) is connected with the upper part of the demethanizer (31) through a pipeline provided with a fourth throttle valve (37), the other path of gas phase is connected with the demethanizer (31) through a pipeline after being expanded through an expander (33), the gas phase outlet of the low-temperature separator (27) is connected with the top of the heavy hydrocarbon recovery cold box (25) through a compressor (42) and the inlet end of the second-stage precooling section, the heavy hydrocarbon recovery cold box (25) is further connected with the heavy hydrocarbon recovery cold box (25) through the compressor (42), the cooled gas phase is connected with the inlet end of a condensing section in the liquefaction cooling box (2) through a pipeline;
the gas phase at the top of the demethanizer (31) is divided into two paths after being cooled by a second cooler (44), one path is sent back to the heavy hydrocarbon recovery cold box (25), the other path is connected with the inlet end of a cooling section in the heavy hydrocarbon recovery cold box (25) through a pipeline, and the outlet end of the cooling section in the heavy hydrocarbon recovery cold box (25) is connected with the upper part of the demethanizer (31) through a pipeline provided with a fifth throttle valve (49);
the liquid phase outlet in the middle of the demethanizer (31) is connected with the inlet end of the heating section in the heavy hydrocarbon recovery cold box (25) through a pipeline, and the outlet end of the heating section in the heavy hydrocarbon recovery cold box (25) is connected with the liquid phase inlet in the middle of the demethanizer (31) through a pipeline.
2. The integrated natural gas liquefaction and condensate recovery device of claim 1, wherein: the utility model discloses a refrigerating system, including liquefaction cold box (2), refrigerant refrigerating unit, liquefaction cold box (2) are connected with refrigerant refrigerating unit, refrigerant refrigerating unit includes first cooler (23) and refrigerant compressor (21), first cooler (23) are connected with the cooling section in liquefaction cold box (2), the cooling section is connected with the reheat section in liquefaction cold box (2) through the pipeline that is provided with second choke valve (18), the reheat section is connected with refrigerant compressor (21) through the pipeline, refrigerant compressor (21) are connected with first cooler (23) through the pipeline, form refrigerant refrigeration cycle return circuit.
3. The integrated natural gas liquefaction and condensate recovery device of claim 1, wherein: the lower liquid phase outlet of the demethanizer (31) is connected with the lower liquid phase inlet of the demethanizer (31) through a pipeline provided with a demethanizer reboiler (54).
4. A method for natural gas liquefaction and condensate recovery integration, which adopts the natural gas liquefaction and condensate recovery integration device as claimed in any one of claims 1 to 3, and is characterized in that: the method comprises the following steps:
firstly, natural gas from a natural gas inlet pipeline enters a liquefaction cold box for precooling to-25 to-45 ℃, then enters a heavy hydrocarbon removal tower for separation, liquid hydrocarbon at the bottom of the heavy hydrocarbon removal tower enters a next process for treatment, gas phase at the top of the heavy hydrocarbon removal tower enters the liquefaction cold box for precooling to-50 to-65 ℃, then enters a heavy hydrocarbon removal tower reflux tank for gas-liquid separation, wherein: the liquid phase is pressurized by a heavy hydrocarbon removal tower reflux pump and then enters the top of the heavy hydrocarbon removal tower, the gas phase is divided into two paths according to any proportion, one path is throttled to be 350-5500 kPa.a by a first throttle valve, enters a liquefaction cooling box and is further condensed to be between-150 and-162 ℃, and then enters the next working procedure for treatment; the other path enters a heavy hydrocarbon recovery cold box for precooling to-50 to-70 ℃ and then further recovering the heavy hydrocarbon;
secondly, entering a heavy hydrocarbon recovery cold box for precooling to-50 to-70 ℃, and then entering a low-temperature separator for gas-liquid separation, wherein: the liquid phase is throttled to 1000 kPa.a-3500kPa.a by a third throttle valve and then enters the middle part of the demethanizer, the gas phase is divided into two paths, one path of 1-30% material flow enters a heavy hydrocarbon recovery cold box to be cooled to minus 95-minus 125 ℃, enters a fourth throttle valve to be throttled to 1000 kPa.a-3500kPa.a and then enters the upper part of the demethanizer, and the other path of 70-99% material flow enters an expansion machine to be expanded to 1000 kPa.a-3500kPa.a and then enters the upper part of the demethanizer; the gas phase at the top outlet of the demethanizer enters a heavy hydrocarbon recovery cold box for reheating to 25-40 ℃, is pressurized by an expander, enters a dry gas compressor for pressurizing to 4000 kPa.a-6000 kPa.a, enters a second cooler for cooling to 40-50 ℃, enters a heavy hydrocarbon recovery cold box for cooling to-20 to-40 ℃, and enters a liquefaction cold box for liquefaction;
and thirdly, the refrigerant from the first cooler enters the liquefaction cooling tank to be cooled to-150 to-162 ℃, enters the second throttling valve through a pipeline to be throttled to 300-500 kPa.a, enters the liquefaction cooling tank to be reheated to 35-45 ℃, enters the refrigerant compressor through the pipeline to be pressurized to 350 kPa.a-5000 kPa.a, enters the first cooler to be cooled to 40-50 ℃ and then enters the liquefaction cooling tank, and the refrigerant refrigeration cycle is formed to provide the required cooling capacity for the liquefaction cooling tank.
5. The integrated natural gas liquefaction and condensate recovery method of claim 4, wherein: in the second step, the gas phase at the outlet of the top of the demethanizer is cooled by a second cooler and then is divided into two paths, wherein 80-95% of the gas phase enters a heavy hydrocarbon recovery cold box to be cooled to minus 20-minus 40 ℃ and then enters a liquefaction cold box to be liquefied, and the other 5-20% of the gas phase enters the heavy hydrocarbon recovery cold box to be cooled to minus 95-minus 125 ℃, enters a fifth throttle valve to be throttled to 1000 kPa.a-2500 kPa.a and then enters the top of the demethanizer.
6. The integrated natural gas liquefaction and condensate recovery method of claim 5, wherein: in the second step, the liquid phase in the middle part of the demethanizer enters a heavy hydrocarbon recovery cold box to be heated and then returns to the middle part of the demethanizer to be inlet, so that the cold energy in the demethanizer is recovered.
7. The integrated natural gas liquefaction and condensate recovery method of claim 5, wherein: in the second step, the liquid phase at the bottom of the demethanizer enters a reboiler of the demethanizer and returns to the inlet at the bottom of the demethanizer after being heated, so that the content of methane in the liquid phase at the bottom of the demethanizer is controlled, and the liquid phase at the bottom of the demethanizer enters the next working procedure for treatment.
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