CN111964353A - Natural gas liquefaction and condensate recovery integrated device and method - Google Patents

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

Info

Publication number
CN111964353A
CN111964353A CN202010841396.8A CN202010841396A CN111964353A CN 111964353 A CN111964353 A CN 111964353A CN 202010841396 A CN202010841396 A CN 202010841396A CN 111964353 A CN111964353 A CN 111964353A
Authority
CN
China
Prior art keywords
heavy hydrocarbon
cold box
enters
liquefaction
pipeline
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Granted
Application number
CN202010841396.8A
Other languages
Chinese (zh)
Other versions
CN111964353B (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
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
China National Petroleum Corp
China Petroleum Engineering and Construction Corp
China Petroleum Engineering Co Ltd
Original Assignee
China Petroleum Engineering and Construction Corp
China Petroleum Engineering Co Ltd
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by China Petroleum Engineering and Construction Corp, China Petroleum Engineering Co Ltd filed Critical China Petroleum Engineering and Construction Corp
Priority to CN202010841396.8A priority Critical patent/CN111964353B/en
Publication of CN111964353A publication Critical patent/CN111964353A/en
Application granted granted Critical
Publication of CN111964353B publication Critical patent/CN111964353B/en
Active legal-status Critical Current
Anticipated expiration legal-status Critical

Links

Images

Classifications

    • 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

Landscapes

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

Abstract

The invention discloses a natural gas liquefaction and condensate recovery integrated device and method, which comprises a liquefaction cold box, a heavy hydrocarbon removal tower reflux tank and a condensate recovery unit, wherein the liquefaction cold box is connected with a natural gas pipeline and a heavy hydrocarbon removal tower, a top gas phase outlet of the heavy hydrocarbon removal tower is connected with the liquefaction cold box, the liquefaction 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 recovery unit is used for further recovering heavy hydrocarbon from the natural gas after heavy hydrocarbon removal and sending the treated natural gas back to a condensation section of the liquefaction cold box. The invention adopts a heavy hydrocarbon removal tower to remove C in natural gas5 +Heavy hydrocarbon composition to avoid natural gas liquefaction in-process equipment and pipeline to freeze stifled, draw through condensate recovery unit to the natural gas after taking off the heavy hydrocarbon moreover and constitute such as ethane, propane, butane. The invention is applicable to natural gas as well as natural gasThe additive is used for one or more hydrocarbon mixtures such as coal bed gas, coke oven gas and the like.

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
The natural gas contains most of methane, and small amounts of ethane, propane and butane, and trace amounts of pentane, hexane and other components. Natural gas liquid recoveryThe recovery means that components such as ethane, propane, butane and pentane in the natural gas are separated from the natural gas, and the recovered condensate is used as a chemical raw material, so that the economic benefit is better. The natural gas liquefaction is to produce liquefied natural gas after the purified natural gas is subjected to low-temperature condensation and liquefaction. Because the natural gas contains heavy hydrocarbon components, the heavy hydrocarbon components refer to C5 +Hydrocarbons, because of heavy hydrocarbon melts the boiling point low, condensation, freeze and block up pipeline and equipment under low temperature environment, consequently the natural gas must desorption heavy hydrocarbon component that contains at liquefaction in-process to avoid the natural gas to arouse at the liquefaction in-process and freeze stifled, the natural gas further condensation behind the desorption heavy hydrocarbon, liquefaction production liquefied natural gas.
In addition, since the natural gas liquefaction plant needs to supplement refrigerants such as ethane and propane, a condensate recovery unit may be provided after the heavy hydrocarbon removal column to extract components such as ethane and propane from the natural gas for the refrigerant supplement. Meanwhile, the built natural gas liquefaction project can extract components such as ethane, propane and butane with the lowest marginal cost by reducing the high calorific value (HHV) in the liquefied natural gas product, and a condensate recovery device can be added after a heavy hydrocarbon removal tower, so that products such as ethane, propane and butane can be produced with the lowest cost and the lowest investment.
Disclosure of Invention
The invention aims to: aiming at the problems, the device and the method for integrating natural gas liquefaction and condensate recovery can avoid freezing and blocking of equipment and pipelines in the natural gas liquefaction process and can extract ethane, propane, butane and the like from the natural gas after heavy hydrocarbon removal.
The technical scheme adopted by the invention is as follows: the utility model provides a natural gas liquefaction and condensate recovery integrated device which characterized in that: the device comprises a liquefaction cold box, a heavy hydrocarbon removal tower reflux tank and a condensate recovery unit, wherein a primary precooling section inlet end in the liquefaction cold box is connected with a natural gas inlet pipeline, an outlet end of the primary precooling section inlet end is connected with the heavy hydrocarbon removal tower through a pipeline, liquid hydrocarbon separated by the heavy hydrocarbon removal tower enters a post-process through a bottom pipeline, a top gas phase outlet of the heavy hydrocarbon removal tower is connected with a secondary precooling section inlet end in the liquefaction cold box through a pipeline, an outlet end of the secondary precooling section is connected with the heavy hydrocarbon removal tower reflux tank through a pipeline, 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, a gas phase outlet of the heavy hydrocarbon removal tower reflux tank is divided into two paths, one path is connected with a condensation section inlet end in the liquefaction cold box through a pipeline provided with a, and the other path is connected with a condensate recovery unit through a pipeline, the condensate recovery unit is used for further recovering heavy hydrocarbon from the natural gas after heavy hydrocarbon removal, and the treated natural gas is sent back to the condensation section of the liquefaction cold box.
According to the integrated device for natural gas liquefaction and condensate recovery, the liquefaction cold box is connected with the refrigerant refrigeration unit, the refrigerant refrigeration unit comprises a first cooler and a refrigerant compressor, the first cooler is connected with the cooling section in the liquefaction cold box, the cooling section is connected with the reheating section in the liquefaction cold box through a pipeline provided with a second throttling 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 refrigeration circulation loop.
The natural gas liquefaction and condensate recovery integrated device comprises a heavy hydrocarbon recovery cold box, a cryogenic separator and a demethanizer, wherein one path of gas phase of a heavy hydrocarbon removal tower reflux tank is connected with a primary precooling section inlet end in the heavy hydrocarbon recovery cold box through a pipeline, a primary precooling section outlet end in the heavy hydrocarbon recovery cold box is connected with the cryogenic separator through a pipeline, a bottom liquid phase outlet of the cryogenic separator is connected with the demethanizer through a pipeline provided with a third throttle valve, a top gas phase outlet of the cryogenic separator is divided into two paths, one path of gas phase is connected with a secondary precooling section inlet end in the heavy hydrocarbon recovery cold box through a pipeline, a secondary precooling section outlet end 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, and the other path of gas phase is connected with the demethanizer through a pipeline after being expanded by an expander, the top gaseous phase export of demethanizer passes through the reheat section entrance connection in pipeline and the heavy hydrocarbon recovery cold box, the reheat section exit end in the heavy hydrocarbon recovery cold box passes through the pipeline and is connected with expander and dry gas compressor in proper order to send back the further cooling of heavy hydrocarbon recovery cold box after the second cooler cooling, gaseous phase after the cooling passes through pipeline and the condensation section entrance connection in the liquefaction cold box.
According to the natural gas liquefaction and condensate recovery integrated device, gas phase at the top of the demethanizer is cooled by the second cooler and then divided into two paths, one path of gas phase is sent back to the heavy hydrocarbon recovery cold box, the other path of 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 throttling valve.
According to the natural gas liquefaction and condensate recovery integrated device, a liquid phase outlet in the middle of the demethanizer is connected with an inlet end of a heating section in a heavy hydrocarbon recovery cold box through a pipeline, and an outlet end of the heating section in the heavy hydrocarbon recovery cold box is connected with a liquid phase inlet in the middle of the demethanizer through a pipeline.
According to the integrated device for natural gas liquefaction and condensate recovery, the lower liquid phase outlet of the demethanizer is connected with the lower liquid phase inlet of the demethanizer through the pipeline provided with the demethanizer reboiler.
A method for integrating natural gas liquefaction and condensate recovery is characterized by comprising the following steps: the method comprises the following steps:
the first step, the natural gas that comes from the natural gas admission line gets into the liquefaction cold box precooling and gets into after-25- ~ -45 ℃ and takes off heavy hydrocarbon tower lower part and separate, takes off heavy hydrocarbon tower bottom liquid hydrocarbon and gets into next process and handle, takes off heavy hydrocarbon tower top gas phase and gets into after the liquefaction cold box precooling and-50- ~ -65 ℃ and get into and take off heavy hydrocarbon tower reflux tank and carry out 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, the gas phase is divided into two paths according to any proportion, one path of the gas phase is throttled to 3500 kPa.a-5500 kPa.a by a first throttling valve, enters a liquefaction cooling box and is further condensed to-150 to-162 ℃, and then enters the next step of processing; the other path of heavy hydrocarbon enters a heavy hydrocarbon recovery cold box and is pre-cooled to-50 to-70 ℃, and then heavy hydrocarbon is further recovered;
and secondly, entering a heavy hydrocarbon recovery cold box, precooling to-50-70 ℃, and then entering a low-temperature separator for gas-liquid separation, wherein: the liquid phase is throttled to 1000 kPa.a-3500 kPa.a by a third throttling 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-95-125 ℃, enters a fourth throttling valve to be throttled to 1000 kPa.a-3500 kPa.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-3500 kPa.a and then enters the middle upper part of the demethanizer; the gas phase at the outlet of the top of the demethanizer enters a heavy hydrocarbon recovery cold box to be reheated to 25-40 ℃, enters a dry gas compressor to be pressurized to 4000 kPa.a-6000 kPa.a after being pressurized by an expander, enters a second cooler to be cooled to 40-50 ℃, enters a cooled gas phase into a heavy hydrocarbon recovery cold box to be cooled to-20-40 ℃ and then enters a liquefaction cold box to be liquefied;
and thirdly, the refrigerant from the first cooler enters a liquefaction cold box to be cooled to-150 to-162 ℃, enters a second throttling valve through a pipeline to be throttled to 300-500 kPa.a, enters the liquefaction cold box to be reheated to 35-45 ℃, enters a refrigerant compressor through a pipeline to be pressurized to 3500 kPa.a-5000 kPa.a, enters the first cooler to be cooled to 40-50 ℃ and then enters the liquefaction cold box to form refrigerant refrigeration cycle to provide the required cold energy for the liquefaction cold box.
In the second step, the gas phase at the outlet of the top of the demethanizer is cooled by a second cooler and then divided into two paths, wherein one path of 80-95% of material flow enters a heavy hydrocarbon recovery cold box to be cooled to-20 to-40 ℃ and then enters a liquefaction cold box to be liquefied, the other path of 5-20% of material flow enters a heavy hydrocarbon recovery cold box to be cooled to-95 to-125 ℃, enters a fifth throttle valve to be throttled to 1000 kPa.a-3500 kPa.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 inlet in the middle of the demethanizer, so that the cold energy in the demethanizer is recovered.
In the second step, the liquid phase at the lower part of the demethanizer enters a demethanizer reboiler to be heated and then returns to the inlet at the lower part of the demethanizer to control the content of methane in the liquid phase at the bottom of the demethanizer, 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: removing C in natural gas by heavy hydrocarbon removing tower5 +Heavy hydrocarbon constitutes to avoid natural gas liquefaction in-process equipment and pipeline to freeze stifled, draw the natural gas after taking off heavy hydrocarbon through setting up the condensate recovery unit moreover and constitute such as ethane, propane, butane, the natural gas after the condensate recovery unit further condenses the liquefaction and produces liquefied natural gas, and can realize that the natural gas liquefaction is nimble under the condition that has or not condensate recovery unit and switch. The invention is applicable to natural gas, and also applicable to one or more hydrocarbon mixtures such as coal bed gas, coke oven gas and the like.
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 view of the principle of embodiment 1 of the present invention.
Fig. 2 is a schematic diagram of embodiment 2 of the present invention.
The labels in the figure are: 1 is the natural gas inlet line, 2 is the liquefaction cold box, 4 is taking off the heavy hydrocarbon tower, 7 is taking off the heavy hydrocarbon tower reflux tank, 9 is taking off the heavy hydrocarbon tower reflux pump, 12 is first choke valve, 18 is the second choke valve, 21 is the refrigerant compressor, 23 is first cooler, 25 is the heavy hydrocarbon recovery cold box, 27 is the cryogenic separation ware, 29 is the third choke valve, 31 is removing the methane tower, 33 is the expander, 37 is the fourth choke valve, 42 is the dry gas compressor, 44 is the second cooler, 49 is the fifth choke valve, 54 is removing the methane tower reboiler.
Detailed Description
In order to make the objects, technical solutions and advantages of the embodiments of the present invention clearer, the technical solutions in the embodiments of the present invention will be clearly and completely described below with reference to the drawings in the embodiments of the present invention, and it is obvious that the described embodiments are some, but not all, embodiments of the present invention. The components of 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 present invention, 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 derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention.
It should be noted that the embodiments and features of the embodiments may be combined with each other without conflict.
It should be noted that: like reference numbers and letters refer to like items in the following figures, and thus, once an item is defined in one figure, it need not be further defined and explained in subsequent figures.
In the description of the embodiments of the present invention, it should be noted that the indication of the orientation or the positional relationship is based on the orientation or the positional relationship shown in the drawings, or the orientation or the positional relationship which is usually placed when the product of the present invention is used, or the orientation or the positional relationship which is usually understood by those skilled in the art, or the orientation or the positional relationship which is usually placed when the product of the present invention is used, and is only for the convenience of describing the present invention and simplifying the description, but does not indicate or imply that the indicated device or element must have a specific orientation, be constructed in a specific orientation, and be operated, and therefore, cannot be understood as limiting the present invention. Furthermore, the terms "first" and "second" are used merely to distinguish one description from another, and are not to be construed as indicating or implying relative importance.
In the description of the embodiments of the present invention, it should be further noted that the terms "disposed" and "connected" are to be interpreted broadly, and may be, for example, fixedly connected, detachably connected, or integrally connected, unless explicitly stated or limited otherwise; may be directly connected or indirectly connected through an intermediate. The specific meanings of the above terms in the present invention can be understood in specific cases by those skilled in the art; the drawings in the embodiments are used for clearly and completely describing the technical scheme in the embodiments of the invention, and obviously, the described embodiments are a part of the embodiments of the invention, but not all of the embodiments. The components of 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 figure 1, a natural gas liquefaction and condensate recovery integrated device comprises a liquefaction cold box 2, a heavy hydrocarbon removal tower 4, a heavy hydrocarbon removal tower reflux tank 7 and a condensate recovery unit, wherein a primary precooling section inlet end in the liquefaction cold box 2 is connected with a natural gas inlet pipeline 1, an outlet end of the primary precooling section inlet end is connected with the heavy hydrocarbon removal tower 4 through a pipeline, liquid hydrocarbons separated by the heavy hydrocarbon removal tower 4 enter a post-process through a bottom pipeline, a top gas phase outlet of the heavy hydrocarbon removal tower 4 is connected with a secondary precooling section inlet end in the liquefaction cold box 2 through a pipeline, an outlet end of the secondary precooling section is connected with the heavy hydrocarbon removal tower reflux tank 7 through a pipeline, a liquid phase outlet of the heavy hydrocarbon removal tower reflux tank 7 is connected with the upper part of the heavy hydrocarbon removal tower 4 through a pipeline provided with a heavy hydrocarbon removal tower reflux pump 9, a gas phase outlet of the heavy hydrocarbon removal tower reflux tank 7 is divided into two paths, one path is connected with a condensing section inlet end in the liquefaction cold box, the exit end of condensation section passes through pipeline to back process, and another sweetgum fruit is passed through the pipeline and is connected with condensate recovery unit, condensate recovery unit is used for further retrieving the heavy hydrocarbon to the natural gas after taking off the heavy hydrocarbon to the condensation section of liquefaction cold box 2 is sent back to the natural gas after will handling.
The liquefaction cold box 2 is connected with a refrigerant refrigeration unit, the refrigerant refrigeration unit comprises a first cooler 23 and a refrigerant compressor 21, the first cooler 23 is connected with a cooling section in the liquefaction cold box 2, the cooling section is connected with a reheating section in the liquefaction cold box 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 refrigeration circulation loop.
In this embodiment, the condensate recovery unit includes a heavy hydrocarbon recovery cold box 25, a cryogenic separator 27 and a demethanizer 31, one gas phase of the heavy hydrocarbon removal tower reflux tank 7 is connected with a first-stage pre-cooling section inlet end in the heavy hydrocarbon recovery cold box 25 through a pipeline, a first-stage pre-cooling section outlet end in the heavy hydrocarbon recovery cold box 25 is connected with the cryogenic separator 27 through a pipeline, a bottom liquid phase outlet of the cryogenic separator 27 is connected with the demethanizer 31 through a pipeline provided with a third throttle valve 29, a top gas phase outlet of the cryogenic separator 27 is divided into two gas phases, one gas phase is connected with a second-stage pre-cooling section inlet end in the heavy hydrocarbon recovery cold box 25 through a pipeline, a second-stage pre-cooling section outlet end in the heavy hydrocarbon recovery cold box 25 is connected with an upper portion of the demethanizer 31 through a pipeline provided with a fourth throttle valve 37, and the other gas phase is connected with the demethanizer 31 through, the top gaseous phase export of demethanizer 31 passes through the reheat section entrance connection in pipeline and the heavy hydrocarbon recovery cold box 25, reheat section exit end in the heavy hydrocarbon recovery cold box 25 passes through the pipeline and is connected with expander 33 and dry gas compressor 42 in proper order to send back heavy hydrocarbon recovery cold box 25 further cooling after the second cooler 44 cools off, the gaseous phase after the cooling passes through pipeline and the condensation section entrance connection in the liquefaction cold box 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 via a pipe 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 integrating natural gas liquefaction and condensate recovery, which comprises the following steps:
the method comprises the following steps that firstly, 4000 kPa.a-6000 kPa.a from a natural gas inlet pipeline, natural gas at 30-50 ℃ enters a liquefied cooling box for precooling to-25-45 ℃ and then enters the lower part of a heavy hydrocarbon removal tower for separation, liquid hydrocarbon at the bottom of the heavy hydrocarbon removal tower enters the next procedure for treatment, gas phase at the top of the heavy hydrocarbon removal tower enters the liquefied cooling box for precooling to-50-65 ℃ and then enters 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, the gas phase is divided into two paths according to any proportion, thus the flexible switching between natural gas liquefaction and condensate recovery can be realized, and when the condensate recovery is not needed, the gas phase completely enters a liquefaction cold box through a first throttle valve; when condensate recovery is required, the gas phase can be controlled to completely enter or partially enter a heavy hydrocarbon recovery cold box according to requirements, specifically, one path of gas is throttled to 3500 kPa.a-5500 kPa.a by a first throttling valve, enters a liquefaction cold box, is further condensed to-150 to-162 ℃, and then enters the next process for treatment; the other path of the heavy hydrocarbon enters a heavy hydrocarbon recovery cold box and is pre-cooled to-50 to-70 ℃, and then the heavy hydrocarbon is further recovered.
And secondly, entering a heavy hydrocarbon recovery cold box, precooling to-50-70 ℃, and then entering a low-temperature separator for gas-liquid separation, wherein: the liquid phase is throttled to 1000 kPa.a-3500 kPa.a by a third throttling 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-95-125 ℃, enters a fourth throttling valve to be throttled to 1000 kPa.a-3500 kPa.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-3500 kPa.a and then enters the middle upper part of the demethanizer; and the gas phase at the outlet of the top of the demethanizer enters a heavy hydrocarbon recovery cold box to be reheated to 25-40 ℃, enters a dry gas compressor to be pressurized to 4000 kPa.a-6000 kPa.a after being pressurized by an expander, enters a second cooler to be cooled to 40-50 ℃, enters a cooled gas phase into a heavy hydrocarbon recovery cold box to be cooled to-20 to-40 ℃ and then enters a liquefaction cold box to be liquefied.
The liquid phase at the middle part of the demethanizer enters a heavy hydrocarbon recovery cold box to be heated and then returns to the inlet at the middle part of the demethanizer to recover the cold energy in the demethanizer, the liquid phase at the lower part of the demethanizer enters a reboiler of the demethanizer to be heated and then returns to the inlet at the lower part of the demethanizer to control the content of methane in the liquid phase at the bottom of the demethanizer, and the liquid phase at the bottom of the demethanizer enters the next procedure to.
And thirdly, the refrigerant from the first cooler enters a liquefaction cold box to be cooled to-150 to-162 ℃, enters a second throttling valve through a pipeline to be throttled to 300-500 kPa.a, enters the liquefaction cold box to be reheated to 35-45 ℃, enters a refrigerant compressor through a pipeline to be pressurized to 3500 kPa.a-5000 kPa.a, enters the first cooler to be cooled to 40-50 ℃ and then enters the liquefaction cold box to form refrigerant refrigeration cycle to provide the required cold energy for the liquefaction cold box.
Example 2:
as shown in fig. 2, embodiment 2 is substantially the same as embodiment 1, and its main difference is: the gaseous phase at demethanizer 31 top is divided into two the tunnel after the second cooler 44 cools off, sends back heavy hydrocarbon recovery cold box 25 all the way, and another sweetgum fruit is through the cooling section entrance connection in pipeline and 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 main difference of the natural gas liquefaction and condensate recovery integrated method is as follows: in the second step, the gas phase at the outlet of the top of the demethanizer is cooled by a second cooler and then divided into two paths, wherein one path of 80-95% of the material flow enters a heavy hydrocarbon recovery cold box to be cooled to-20 to-40 ℃ and then enters a liquefaction cold box to be liquefied, the other path of 5-20% of the material flow enters the heavy hydrocarbon recovery cold box to be cooled to-95 to-125 ℃, enters a fifth throttling valve to be throttled to 1000 kPa.a-3500 kPa.a and then enters the top of the demethanizer.
The invention is not limited to the foregoing embodiments. The invention extends to any novel feature or any novel combination of features disclosed in this specification and any novel method or process steps or any novel combination of features disclosed.

Claims (10)

1. The utility model provides a natural gas liquefaction and condensate recovery integrated device which characterized in that: including liquefaction cold box (2), take off heavy hydrocarbon tower (4), take off heavy hydrocarbon tower reflux drum (7) and condensate recovery unit, one-level precooling inlet port in liquefaction cold box (2) is connected with natural gas admission line (1), and its exit end passes through the pipeline and is connected with taking off heavy hydrocarbon tower (4), and liquid hydrocarbon after taking off heavy hydrocarbon tower (4) separation passes through bottom pipeline and gets into back process, the top gaseous phase export that takes off heavy hydrocarbon tower (4) passes through pipeline and second grade precooling inlet port connection in liquefaction cold box (2), the exit end of second grade precooling passes through the pipeline and is connected with taking off heavy hydrocarbon tower reflux drum (7), the liquid phase export that takes off heavy hydrocarbon tower reflux drum (7) is connected with taking off heavy hydrocarbon tower (4) upper portion through the pipeline that is provided with and takes off heavy hydrocarbon tower reflux pump (9), the gaseous phase export that takes off heavy hydrocarbon tower reflux drum (7) divide into two tunnel, and one-road is through the pipeline that is provided with first choke valve (12) and the condensing section in liquefaction cold box (2) And the outlet end of the condensation section is connected with a post-process through a pipeline, the other path is connected with a condensate recovery unit through a pipeline, the condensate recovery unit is used for further recovering heavy hydrocarbon from the natural gas after heavy hydrocarbon removal, and the treated natural gas is returned to the condensation section of the liquefied cold box (2).
2. The integrated natural gas liquefaction and condensate recovery apparatus of claim 1, wherein: the liquefaction cold box (2) is connected with a refrigerant refrigeration unit, the refrigerant refrigeration unit comprises a first cooler (23) and a refrigerant compressor (21), the first cooler (23) is connected with a cooling section in the liquefaction cold box (2), the cooling section is connected with a reheating section in the liquefaction cold box (2) through a pipeline provided with a second throttling 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 refrigeration circulation loop.
3. The integrated natural gas liquefaction and condensate recovery apparatus of claim 1 or 2, wherein: the condensate recovery unit comprises a heavy hydrocarbon recovery cold box (25), a low-temperature separator (27) and a demethanizer (31), wherein one path of gas phase of the heavy hydrocarbon removal tower reflux tank (7) is connected with a first-stage pre-cooling section inlet end in the heavy hydrocarbon recovery cold box (25) through a pipeline, a first-stage pre-cooling section outlet end in the heavy hydrocarbon recovery cold box (25) is connected with the low-temperature separator (27) through a pipeline, a 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), a top gas phase outlet of the low-temperature separator (27) is divided into two paths, one path of gas phase outlet is connected with a second-stage pre-cooling section inlet end in the heavy hydrocarbon recovery cold box (25) through a pipeline provided with a fourth throttle valve (37), and the second-stage pre-cooling section outlet end in the heavy hydrocarbon recovery cold box (25) is connected with, another way is connected with demethanizer (31) through the pipeline after expander (33) inflation, the top gaseous phase export of demethanizer (31) passes through the compound hot section entrance connection in pipeline and the heavy hydrocarbon recovery cold box (25), the compound hot section exit end in the heavy hydrocarbon recovery cold box (25) passes through the pipeline and is connected with expander (33) and dry gas compressor (42) in proper order to send back heavy hydrocarbon recovery cold box (25) further cooling after second cooler (44) cooling, the gaseous phase after the cooling passes through pipeline and the interior condensation segment entrance connection of liquefaction cold box (2).
4. The integrated natural gas liquefaction and condensate recovery apparatus of claim 3, wherein: the gaseous phase at demethanizer (31) top is divided into two the tunnel after second cooler (44) cooling, sends back heavy hydrocarbon and retrieves cold box (25) all the way, and another way passes through pipeline and the interior cooling zone entrance connection of heavy hydrocarbon recovery cold box (25), the cooling zone exit end in heavy hydrocarbon recovery cold box (25) is connected with demethanizer (31) upper portion through the pipeline that is provided with fifth choke valve (49).
5. The integrated natural gas liquefaction and condensate recovery apparatus of claim 3, wherein: demethanizer (31) middle part liquid phase export passes through pipeline and heating section entrance point connection in heavy hydrocarbon recovery cold box (25), heating section exit end in heavy hydrocarbon recovery cold box (25) passes through pipeline and demethanizer (31) middle part liquid phase entry and is connected.
6. The integrated natural gas liquefaction and condensate recovery apparatus of claim 3, 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).
7. A method for integrating natural gas liquefaction and condensate recovery is characterized by comprising the following steps: the method comprises the following steps:
the first step, the natural gas that comes from the natural gas admission line gets into the liquefaction cold box precooling and gets into after-25- ~ -45 ℃ and takes off heavy hydrocarbon tower lower part and separate, takes off heavy hydrocarbon tower bottom liquid hydrocarbon and gets into next process and handle, takes off heavy hydrocarbon tower top gas phase and gets into after the liquefaction cold box precooling and-50- ~ -65 ℃ and get into and take off heavy hydrocarbon tower reflux tank and carry out 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, the gas phase is divided into two paths according to any proportion, one path of the gas phase is throttled to 3500 kPa.a-5500 kPa.a by a first throttling valve, enters a liquefaction cooling box and is further condensed to-150 to-162 ℃, and then enters the next step of processing; the other path of heavy hydrocarbon enters a heavy hydrocarbon recovery cold box and is pre-cooled to-50 to-70 ℃, and then heavy hydrocarbon is further recovered;
and secondly, entering a heavy hydrocarbon recovery cold box, precooling to-50-70 ℃, and then entering a low-temperature separator for gas-liquid separation, wherein: the liquid phase is throttled to 1000 kPa.a-3500 kPa.a by a third throttling 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-95-125 ℃, enters a fourth throttling valve to be throttled to 1000 kPa.a-3500 kPa.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-3500 kPa.a and then enters the middle upper part of the demethanizer; the gas phase at the outlet of the top of the demethanizer enters a heavy hydrocarbon recovery cold box to be reheated to 25-40 ℃, enters a dry gas compressor to be pressurized to 4000 kPa.a-6000 kPa.a after being pressurized by an expander, enters a second cooler to be cooled to 40-50 ℃, enters a cooled gas phase into a heavy hydrocarbon recovery cold box to be cooled to-20-40 ℃ and then enters a liquefaction cold box to be liquefied;
and thirdly, the refrigerant from the first cooler enters a liquefaction cold box to be cooled to-150 to-162 ℃, enters a second throttling valve through a pipeline to be throttled to 300-500 kPa.a, enters the liquefaction cold box to be reheated to 35-45 ℃, enters a refrigerant compressor through a pipeline to be pressurized to 3500 kPa.a-5000 kPa.a, enters the first cooler to be cooled to 40-50 ℃ and then enters the liquefaction cold box to form refrigerant refrigeration cycle to provide the required cold energy for the liquefaction cold box.
8. The integrated natural gas liquefaction and condensate recovery process of claim 7, 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 divided into two paths, wherein one path of 80-95% of the material flow enters a heavy hydrocarbon recovery cold box to be cooled to-20 to-40 ℃ and then enters a liquefaction cold box to be liquefied, the other path of 5-20% of the material flow enters the heavy hydrocarbon recovery cold box to be cooled to-95 to-125 ℃, enters a fifth throttling valve to be throttled to 1000 kPa.a-3500 kPa.a and then enters the top of the demethanizer.
9. The integrated natural gas liquefaction and condensate recovery process of claim 7, wherein: 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 inlet in the middle of the demethanizer, and the cold energy in the demethanizer is recovered.
10. The integrated natural gas liquefaction and condensate recovery process of claim 7, wherein: in the second step, the liquid phase at the lower part of the demethanizer enters a demethanizer reboiler for heating and then returns to the inlet at the lower part of the demethanizer for controlling the content of methane in the liquid phase at the bottom of the demethanizer, and the liquid phase at the bottom of the demethanizer enters the next working procedure for treatment.
CN202010841396.8A 2020-08-20 2020-08-20 Natural gas liquefaction and condensate recovery integrated device and method Active CN111964353B (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
CN202010841396.8A CN111964353B (en) 2020-08-20 2020-08-20 Natural gas liquefaction and condensate recovery integrated device and method

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
CN202010841396.8A CN111964353B (en) 2020-08-20 2020-08-20 Natural gas liquefaction and condensate recovery integrated device and method

Publications (2)

Publication Number Publication Date
CN111964353A true CN111964353A (en) 2020-11-20
CN111964353B CN111964353B (en) 2023-10-27

Family

ID=73388577

Family Applications (1)

Application Number Title Priority Date Filing Date
CN202010841396.8A Active CN111964353B (en) 2020-08-20 2020-08-20 Natural gas liquefaction and condensate recovery integrated device and method

Country Status (1)

Country Link
CN (1) CN111964353B (en)

Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN104061758A (en) * 2014-07-01 2014-09-24 天津市振津工程设计咨询有限公司 Device and method for removing heavy hydrocarbon in natural gas through step-by-step condensation
CN105486034A (en) * 2016-01-05 2016-04-13 中国寰球工程公司 Natural gas liquefaction and light dydrocarbon separation integrated process system and technology
KR20160143684A (en) * 2014-03-14 2016-12-14 루머스 테크놀로지 인코포레이티드 Process and apparatus for heavy hydrocarbon removal from lean natural gas before liquefaction
CN212299664U (en) * 2020-08-20 2021-01-05 中国石油集团工程股份有限公司 Natural gas liquefaction and condensate recovery integrated device

Patent Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
KR20160143684A (en) * 2014-03-14 2016-12-14 루머스 테크놀로지 인코포레이티드 Process and apparatus for heavy hydrocarbon removal from lean natural gas before liquefaction
EP3117163A1 (en) * 2014-03-14 2017-01-18 Lummus Technology Inc. Process and apparatus for heavy hydrocarbon removal from lean natural gas before liquefaction
CN104061758A (en) * 2014-07-01 2014-09-24 天津市振津工程设计咨询有限公司 Device and method for removing heavy hydrocarbon in natural gas through step-by-step condensation
CN105486034A (en) * 2016-01-05 2016-04-13 中国寰球工程公司 Natural gas liquefaction and light dydrocarbon separation integrated process system and technology
CN212299664U (en) * 2020-08-20 2021-01-05 中国石油集团工程股份有限公司 Natural gas liquefaction and condensate recovery integrated device

Also Published As

Publication number Publication date
CN111964353B (en) 2023-10-27

Similar Documents

Publication Publication Date Title
US5291736A (en) Method of liquefaction of natural gas
RU2702829C2 (en) Method of natural gas flow liquefaction and nitrogen removal therefrom and device (embodiments) for implementation thereof
CN105074370B (en) Integrated process for NGL (natural gas liquids recovery) and LNG (liquefaction of natural gas)
RU2355960C1 (en) Two-step removal of nitrogen from liquefied natural gas
US3205669A (en) Recovery of natural gas liquids, helium concentrate, and pure nitrogen
US9759481B2 (en) Method for producing a flow which is rich in methane and a cut which is rich in C2+ hydrocarbons from a flow of feed natural gas and an associated installation
NO331440B1 (en) Hybrid cycle for the production of LNG
CN103940199B (en) Method and device for extracting ethane-mixed hydrocarbon from natural gas
US3721099A (en) Fractional condensation of natural gas
KR20100039353A (en) Method and system for producing lng
KR101393384B1 (en) Method and apparatus for liquefying a natural gas stream
CN106831300B (en) Device and method for recycling ethane and co-producing liquefied natural gas
US20110036120A1 (en) Method and apparatus for recovering and fractionating a mixed hydrocarbon feed stream
KR20110122101A (en) Method and system for producing liquified natural gas
EP0161100A2 (en) Distillation process with high thermo-dynamic efficiencies
KR20170063686A (en) Process for increasing ethylene and propylene yield from a propylene plant
CN212299664U (en) Natural gas liquefaction and condensate recovery integrated device
CN103175380B (en) Device for preparing LNG (liquefied natural gas) by low-concentration coal bed gas oxygen-containing cryogenic liquefaction
BR112012009851B1 (en) process and installation of fractionation of a cracked gas stream from a hydrocarbon pyrolysis installation
AU2016324362B2 (en) A method of preparing natural gas to produce liquid natural gas (LNG)
CN212778207U (en) Cold dry gas circulation recovery ethane device
CN111964353B (en) Natural gas liquefaction and condensate recovery integrated device and method
CN212299663U (en) Natural gas single-tower cryogenic helium extraction device
US10598431B2 (en) Method and system for cooling and separating a hydrocarbon stream
CN205448491U (en) Oxygen -containing coal bed gas piece -rate system that liquefies

Legal Events

Date Code Title Description
PB01 Publication
PB01 Publication
SE01 Entry into force of request for substantive examination
SE01 Entry into force of request for substantive examination
TA01 Transfer of patent application right
TA01 Transfer of patent application right

Effective date of registration: 20210301

Address after: No.2 Daqing East Road, Dushanzi District, Karamay City, Xinjiang Uygur Autonomous Region 834000

Applicant after: CNPC Engineering Co.,Ltd.

Applicant after: CHINA PETROLEUM ENGINEERING & CONSTRUCTION Corp.

Applicant after: CHINA NATIONAL PETROLEUM Corp.

Address before: 833699 No.2 Daqing East Road, Dushanzi District, Karamay City, Xinjiang Uygur Autonomous Region

Applicant before: CNPC Engineering Co.,Ltd.

Applicant before: CHINA PETROLEUM ENGINEERING & CONSTRUCTION Corp.

GR01 Patent grant
GR01 Patent grant