WO2017121042A1 - Procédé et appareil de liquéfaction de gaz riche en méthane par réfrigération par détente - Google Patents

Procédé et appareil de liquéfaction de gaz riche en méthane par réfrigération par détente Download PDF

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WO2017121042A1
WO2017121042A1 PCT/CN2016/078263 CN2016078263W WO2017121042A1 WO 2017121042 A1 WO2017121042 A1 WO 2017121042A1 CN 2016078263 W CN2016078263 W CN 2016078263W WO 2017121042 A1 WO2017121042 A1 WO 2017121042A1
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gas
methane
heat exchanger
rich
low
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PCT/CN2016/078263
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English (en)
Chinese (zh)
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张惊涛
母斌
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成都赛普瑞兴科技有限公司
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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
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
    • F25J1/0203—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using a single-component refrigerant [SCR] fluid in a closed vapor compression cycle
    • F25J1/0208—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using a single-component refrigerant [SCR] fluid in a closed vapor compression cycle in combination with an internal quasi-closed refrigeration loop, e.g. with deep flash recycle 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
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/06—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation
    • F25J3/0605—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation characterised by 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
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/0002—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the fluid to be liquefied
    • F25J1/0022—Hydrocarbons, e.g. 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
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
    • F25J1/0032—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration"
    • F25J1/0035—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration" by gas expansion with extraction of work
    • F25J1/0037—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration" by gas expansion with extraction of work of a return 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
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
    • F25J1/0032—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration"
    • F25J1/004—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration" by flash gas recovery
    • 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
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
    • F25J1/0047—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using an "external" refrigerant stream in a closed vapor compression cycle
    • F25J1/005—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using an "external" refrigerant stream in a closed vapor compression cycle by expansion of a gaseous refrigerant stream with extraction of work
    • 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
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/006—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the refrigerant fluid used
    • F25J1/008—Hydrocarbons
    • F25J1/0082—Methane
    • 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
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
    • F25J1/0201—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using only internal refrigeration means, i.e. without external refrigeration
    • F25J1/0202—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using only internal refrigeration means, i.e. without external refrigeration in a quasi-closed internal refrigeration 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
    • F25J2220/00—Processes or apparatus involving steps for the removal of impurities
    • F25J2220/60—Separating impurities from natural gas, e.g. mercury, cyclic hydrocarbons
    • F25J2220/64—Separating heavy hydrocarbons, e.g. NGL, LPG, C4+ hydrocarbons or heavy condensates in general

Definitions

  • the invention relates to the field of condensation and separation of methane-rich gas, in particular to a method and a device for liquefying expanded methane-rich gas.
  • the expansion refrigeration cycle mostly adopts an inverse Brayton cycle, in which the working medium is isentropically compressed by a compressor, cooled by an aftercooler, and then isentropically expanded and expanded in a turboexpander to perform external work, thereby obtaining a low-temperature airflow.
  • a turboexpander especially high speed gas bearing turboexpanders
  • the efficiency of the turbine reverse Brayton cycle has been significantly improved, and very low refrigeration temperatures and very low Wide range of cooling capacity with high reliability. Therefore, in recent decades, the reverse Bretton refrigeration cycle has been greatly developed, and the scope of application is becoming wider and wider.
  • the expansion refrigeration cycle mainly adopts three forms of nitrogen expansion refrigeration, nitrogen-methane hybrid expansion refrigeration and natural gas direct expansion refrigeration.
  • nitrogen expansion refrigeration is a variant of direct expansion refrigeration, which has the advantages of strong adaptability, high liquefaction capacity, simple process, flexible operation and convenient operation, but its energy consumption is high.
  • Nitrogen-methane hybrid expansion refrigeration is an improvement of the nitrogen expansion refrigeration cycle. It has the advantages of simple process, easy control, short start-up time, etc., and saves 10% of power consumption compared with pure nitrogen expansion refrigeration.
  • Natural gas direct expansion refrigeration directly uses high-pressure natural gas to adiabatically expand in the expander to liquefy natural gas, make full use of the pressure energy of natural gas itself, consume less energy, and save equipment investment.
  • the gas bearing turboexpander with small size, light weight, high efficiency and long-term reliable operation can effectively improve the system efficiency, and can be used in the peak-shaving device which is frequently operated and requires quick start and stop. It has developed into a multi-stage expansion liquefaction system, and the expansion chiller is also becoming mature, with long life, high reliability, low vibration, light weight, etc., and has good development prospects in natural gas liquefaction. Under the increasing demand of liquefied gas, the cycle has greater advantages: it has the advantages of compact equipment, low investment, flexible adjustment and reliable operation.
  • the object of the present invention is to provide a method for producing liquefied natural gas (GB 2522421A), which is difficult to separate heavy hydrocarbons, has complicated operation, high equipment investment, large methane loss, loss of expansion work, and high energy consumption.
  • the invention has the advantages of simple process, flexible operation, low equipment investment, small methane loss, good nitrogen separation effect and recovery expansion work, low energy consumption, low nitrogen content of liquefied methane-rich gas and strong adaptability of raw materials, and has good performance. Application prospects.
  • a method for liquefying an expanded refrigeration methane-rich gas comprises the following steps:
  • the operation of the step 1 is as follows: after the methane-rich feed gas is mixed with a part of the preheated gas, it is cooled to -10 to -90 ° C by a heat exchanger, and then de-heavy hydrocarbons are introduced into a heavy hydrocarbon separator to obtain a low-temperature dry gas and dried at a low temperature. After the gas is cooled by the heat exchanger, it is throttled and depressurized, and then gas-liquid separation is carried out. After separation, the liquefied methane-rich gas and the low-temperature flash vapor are respectively obtained, and the liquefied methane-rich gas is collected as a product, and the low-temperature flash vapor is exchanged through the heat exchanger. After the heat, pressurize and enter the next cycle;
  • the methane-rich feed gas is mixed with a portion of the preheated gas, directly cooled by a heat exchanger, and then subjected to throttling and depressurization, then gas-liquid separation is performed, and liquefied methane-rich gas is separately obtained after separation. , low temperature flash steam, liquefied methane enriched gas as product collection, low temperature flash vapor after heat exchange through the heat exchanger, pressurization, into the next cycle;
  • step 2 The operation of the step 2 is as follows: after the low temperature flash steam is exchanged by the heat exchanger, the preheating gas is obtained, and the preheating gas is pressurized, and after being pressurized, it is divided into the first material and the second material.
  • the first strand of material is sent to the expander after heat exchange by the heat exchanger, and the expanded material is obtained.
  • the expanded material is mixed with the preheated gas after heat exchange by the heat exchanger, and enters the next cycle, and the second material is the second material. a part of the preheating gas mixed with the methane-rich feed gas in step 1;
  • the operation of the step 2 is as follows: after the low temperature flash vapor is exchanged by the heat exchanger, the preheating gas is obtained, the preheating gas is pressurized, and after being pressurized, the first material and the second material are separated. Two materials, the first material is directly sent into the expander to obtain the expanded material, and the expanded material is mixed with the preheated gas after heat exchange by the heat exchanger, and enters the next cycle, and the second material is the step 1 a portion of the preheated gas mixed with the methane-rich feed gas;
  • the operation of the step 1 is as follows: after the low temperature flash vapor is exchanged by the heat exchanger, the preheating gas is obtained, and the preheating gas is pressurized, and The methane-rich feed gas is mixed with the preheated gas, and the mixed materials are cooled to -10 to -90 ° C by a heat exchanger, and then de-heavy hydrocarbons are introduced into the heavy hydrocarbon separator to obtain low-temperature dry gas, and the low-temperature dry gas is passed through the heat exchanger. After cooling, after throttling and depressurization, gas-liquid separation is carried out.
  • liquefied methane-rich gas, low-temperature flash vapor, liquefied methane-rich gas are collected as products, and low-temperature flash vapor is superheated by heat exchanger.
  • the methane-rich feed gas is free of heavy hydrocarbons, the methane-rich feed gas is mixed with a portion of the preheated gas, directly cooled by a heat exchanger, and then subjected to throttling and depressurization, then gas-liquid separation, after separation Liquefied methane-rich gas, low-temperature flash steam, liquefied methane-rich gas are collected as products, and the low-temperature flash vapor is heated by the heat exchanger, and then pressurized to enter the next cycle;
  • step 2 After the cooling medium is pressurized, it is exchanged by the heat exchanger and enters the expander to obtain the expanded material. After the heat transfer material is exchanged by the heat exchanger, the pressure is returned to the next one. cycle;
  • step 2 the operation of the step 2 is as follows: after the cooling medium is pressurized, it is directly sent into the expander to obtain an expanded material, and the expanded material is then subjected to heat exchange by the heat exchanger, and then returned to the pressurization to enter the next cycle;
  • the methane-rich feed gas has a pressure of 1 MPaG to 20 MPaG and a temperature of -30 to 60 ° C, or the methane-rich feed gas is a self-evaporating gas of the LNG storage tank.
  • the partial preheating gas is mixed with the methane-rich raw material gas to form two materials into the heat exchanger; or the preheating gas is completely mixed with the methane-rich raw material gas, and then divided into two into the heat exchanger.
  • the throttling and depressurization are performed, and the number of stages of the throttling is first-stage throttling, two-stage throttling, three-stage throttling or four-stage throttling.
  • the low-temperature dry gas is cooled by the heat exchanger, then depressurized by the throttling, and then enters the first gas-liquid separator for gas-liquid separation, and the first liquid phase and the first gas phase are respectively obtained after separation.
  • the first liquid phase is a liquefied methane-rich gas
  • the first gas phase is a low-temperature flash vapor.
  • the first liquid phase is depressurized and then depressurized, and then enters the second gas-liquid separator for gas-liquid separation, and after separation, a second liquid phase and a second gas phase are respectively obtained, and the second liquid is obtained.
  • the phase is the liquefied methane-rich gas, and the first gas phase and the second gas phase are low temperature flash vapor.
  • pre-cooling step external cooling is connected to the heat exchanger, and other components in the heat exchanger are pre-cooled by external cooling.
  • a typical refrigerant used for the external cooling is one or more of propylene, propane, ammonia, freon, water, BOG, and lithium bromide.
  • Methane-laden liquefied gases can be extracted from any material in the system.
  • step 2 according to the pressure and temperature of the methane-rich feed gas, it is mixed with the preheated gas at a suitable position in the system.
  • the apparatus for the foregoing method for expanding and refrigerating methane-rich gas liquefaction includes a methane-rich gas liquefaction system and an open-cycle refrigeration system;
  • the methane-rich gas liquefaction system includes a raw material supply device for transporting a methane-rich feed gas, a heat exchanger, and a gas-liquid separator, and the raw material supply device, the heat exchanger, and the gas-liquid separator are sequentially connected through a pipeline;
  • the open-cycle refrigeration system includes a gas-liquid separator, a heat exchanger, a compressor, and an expander, and the gas-liquid separator, the heat exchanger, the compressor, and the expander form an open circulation system through a pipeline;
  • Providing another alternative device including a methane-rich gas liquefaction system, a closed cycle refrigeration system;
  • the methane gas liquefaction system includes a raw material supply device, a heat exchanger, a gas-liquid separator, and a compressor, and the raw material supply device, the heat exchanger, the gas-liquid separator, and the compressor are sequentially connected through a pipeline;
  • the closed cycle refrigeration system includes a compressor, a heat exchanger, and an expander, and the compressor, the heat exchanger, and the expander form a closed circulation system through a pipeline.
  • a methane-containing gas that is not easily liquefied e.g., one or more of nitrogen, hydrogen, argon, oxygen, or helium
  • the methane-containing, non-liquefied gas can be withdrawn from the first preheated gas or the first flash gas or the second preheated gas or the second flash gas.
  • external cooling in conjunction with a heat exchanger, typically one or more of propylene, propane, ammonia, freon, water, BOG, lithium bromide.
  • the invention has the advantages of rich regulation means, simple process, flexible operation, strong adaptability of raw materials, low equipment investment, small methane loss, good nitrogen separation effect and low energy consumption, and has good application prospect.
  • the methane-rich gas is pre-cooled, expanded, and then cooled, and has a better refrigeration effect than the prior art
  • the throttle valve is used for decompression, although the efficiency is slightly lower, but the cooling capacity is equivalent, the operation is simpler, and the equipment investment is smaller;
  • the invention adopts step-by-step throttling, and the pressure drop of each stage is small, so that the invention has the advantages of lower energy consumption, less methane loss and high nitrogen separation coefficient;
  • the present invention enables the expansion work to be transmitted to the compression device through the mutual cooperation between the components, thereby effectively reducing energy consumption, saving cost, and having a good application prospect;
  • the invention has flexible operation, small methane loss, low energy consumption and good application prospect.
  • Embodiment 1 is a schematic diagram of the principle of Embodiment 1.
  • T1 is the pretreatment system
  • P1 is the expander
  • C1 and C2 are the recycle gas compressors
  • E1 and E2 are the coolers
  • E3 is the heat exchanger
  • V2 is the heavy hydrocarbon separator
  • V1 is the gas-liquid separator
  • V3 is an LNG storage tank.
  • Embodiment 2 is a schematic diagram of the principle of Embodiment 2.
  • T1 is the pretreatment system
  • P1 is the expander
  • C1 and C2 are the recycle gas compressors
  • C3 is the methane-rich recycle gas compressor
  • E1, E2, E3 are the coolers
  • E4 is the heat exchanger
  • V1 is The gas-liquid separator
  • V2 is a heavy hydrocarbon separator
  • V3 is an LNG storage tank.
  • the schematic diagram of the flow of this embodiment is shown in Figure 1.
  • the process includes a pretreatment system (T1), an expander (P1), a recycle gas compressor (C1, C2), a cooler (E1, E2), and a heat exchanger ( E3), a heavy hydrocarbon separator (V2), a gas-liquid separator (V1), an LNG storage tank (V3), etc., and a methane-rich gas liquefaction system and an open-cycle refrigeration system are formed by piping between the components.
  • the untreated methane-rich feed gas 1 is treated with a pretreatment system T1 to obtain a methane-rich feed gas 2 .
  • the methane-rich feed gas 2 is mixed with a portion of the preheated gas 16 (mentioned below) to obtain the material 3, which is cooled by the heat exchanger E3 to obtain the material 4.
  • the material 4 exits the heat exchanger E3, enters the heavy hydrocarbon separator V2 to de-heavigate the hydrocarbon, the heavy hydrocarbon is taken out from the material 6, and the low-temperature dry gas material 5 is further cooled into the heat exchanger E3 to obtain the material 7.
  • the material 7 is taken out of the heat exchanger E3 and throttled by the first throttle valve I to obtain the material 8.
  • the material 8 enters the gas-liquid separator V1 for gas-liquid separation, and the liquid phase 10 separated by the gas-liquid separator V1 continues to perform two-stage throttling, and the low-temperature flash vapor 9 separated by the gas-liquid separator V1 enters the heat exchanger E3.
  • the preheating gas 11 is taken out.
  • the preheating gas 11 extracts two materials 12 and 13, the material 12 is taken out as a non-liquefied gas, and the material 13 is mixed with the material 28 (mentioned below) to obtain the material 25.
  • the material 25 is mixed with the material 22 (mentioned below)
  • the material 23 is obtained, and the material 23 is pressurized by the circulating gas compressor C2.
  • the material 24 is cooled by the cooler E2, and the material 14 is divided into the material 15 With material 16, material 16 is mixed with methane-rich feed gas 2 for the next cycle.
  • the liquid phase 10 separated by the gas-liquid separator V1 is throttled by the secondary throttle valve II to obtain the material 17.
  • the material 17 enters the LNG storage tank V3 for gas-liquid separation, and the separated liquid phase product is stored in the tank and transported through the material 18;
  • the low temperature flash steam 19 enters the heat exchanger E3 to reheat, the preheating gas 20 is taken out, and the preheating gas 20 is pressurized into the circulating gas compressor C1 to obtain the material 21.
  • the material 21 is cooled by the cooler E1
  • the material 22 is taken out and the material 22 is mixed with the material 25.
  • the material 15 of the preheated gas 14 is cooled in the heat exchanger E3 to obtain the material 26.
  • Material 26 enters expander P1, and after expansion, material 27 is withdrawn.
  • the material 15 is directly sent to the expander P1 for expansion without heat exchange by the heat exchanger E3, and the material 27 is taken out.
  • Material 27 enters heat exchanger E3 to provide refrigeration and heat exchanger to obtain material 28. After the material 28 is mixed with the preheated gas 13, it proceeds to the next cycle.
  • the temperature of the methane-rich feed gas 2 is 40 ° C and the pressure is 6000 kPaA; the liquefied gas (ie, material 12) is 37 ° C and the pressure is 1080 kPa A; the temperature of the product LNG is -160.5 ° C, and the pressure is 120 kPaA. All are absolutely pressure.
  • the schematic diagram of the flow of this embodiment is shown in FIG. 2, and the process includes a pretreatment system (T1), an expander (P1), a circulating gas compressor (C1, C2), a methane-rich circulating gas compressor (C3), and a cooler. (E1, E2, E3), heat exchanger (E4), gas-liquid separator (V1), heavy hydrocarbon separator (V2), LNG storage tank (V3), and methane-rich gas liquefaction system formed by pipes between the components And closed cycle refrigeration systems.
  • T1 pretreatment system
  • P1 a circulating gas compressor
  • C3 methane-rich circulating gas compressor
  • E4 heat exchanger
  • V1 gas-liquid separator
  • V2 heavy hydrocarbon separator
  • LNG storage tank V3
  • methane-rich gas liquefaction system formed by pipes between the components And closed cycle refrigeration systems.
  • the untreated methane-rich feed gas 1 is treated with a pretreatment system T1 to obtain a methane-rich feed gas 2 .
  • Methane-rich feed gas 2 is mixed with preheated gas 16 (mentioned below) to give material 3.
  • preheated gas 16 (mentioned below) to give material 3.
  • the heat exchanger E4 is discharged from the material 4
  • the heavy hydrocarbon separator V2 is de-heavier
  • the heavy hydrocarbon is taken out by the material 6
  • the low-temperature dry gas material 5 is re-entered into the heat exchanger E4 to be cooled by the material.
  • 7 leads to the heat exchanger E4.
  • the material 8 is obtained.
  • the material 8 enters the gas-liquid separator V1 for gas-liquid separation, and the separated liquid phase 10 continues to perform secondary throttling.
  • the separated low-temperature flash vapor 9 enters the heat exchanger E4 to reheat, and then the preheated gas 11 is taken out, and the preheating is performed.
  • the gas 11 leads to two materials 12 and 13. Wherein the material 12 is taken out as a liquefied gas, and the material 13 is mixed with the material 22 (mentioned below) to obtain the material 14.
  • the material 14 is pressurized by the circulating gas compressor C2, and the material 15 which is taken out after being pressurized is cooled by the cooler E2 to obtain the material 16. Material 16 is mixed with dry gas 2 for the next cycle.
  • the liquid phase 10 separated by the gas-liquid separator V1 is throttled by the secondary throttle valve II to obtain the material 17.
  • the material 17 enters the LNG storage tank V3 for gas-liquid separation, and the separated liquid phase product is stored in the tank and transported through the material 18; the separated low-temperature flash steam 19 enters the heat exchanger E4 to reheat, and the preheating gas 20 is taken out.
  • preheating gas 20 enters the recycle gas compressor C1 is pressurized to obtain material 21. After the material 21 is cooled by the cooler E1, the material 22 is taken out and the material 22 is mixed with the material 13.
  • the material 23 is taken out. After the material 23 is cooled by the cooler E3, the material 24 is obtained. Material 24 enters heat exchanger E4 for further cooling and is withdrawn from material 25. After the material 25 is expanded by the expander P1, the material 26 is obtained. Alternatively, the material 24 is directly sent to the expander P1 for expansion without heat exchange by the heat exchanger E4, and the material 26 is taken out. Material 26 enters heat exchanger E4 to provide refrigeration for the heat exchanger and draws material 27 into rich methane recycle gas compressor C3 to begin the next cycle.
  • the temperature of the methane-rich feed gas 2 is 40 ° C and the pressure is 5000 kPaA; the liquefied gas (ie, material 12) is 37 ° C, the pressure is 1080 kPa A; the temperature of the product LNG is -160.5 ° C, and the pressure is 120 kPaA. All are absolutely pressure.
  • the invention is not limited to the specific embodiments described above.
  • the invention extends to any new feature or any new combination disclosed in this specification, as well as any novel method or process steps or any new combination disclosed.

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  • General Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
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  • General Chemical & Material Sciences (AREA)
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Abstract

L'invention concerne un procédé et un appareil de liquéfaction de gaz riche en méthane par l'intermédiaire d'une réfrigération par détente, le procédé consistant : à introduire un mélange de gaz riche en méthane et de gaz partiellement préchauffé dans des échangeurs de chaleur (E3 et E4) et à refroidir ledit mélange, à retirer les hydrocarbures lourds dans le matériau refroidi, puis à étrangler le matériau à travers une vanne d'étranglement (I) et à le séparer au moyen d'un séparateur gaz-liquide (V1) en un matériau en phase liquide et une vapeur instantanée à basse température. Le matériau en phase liquide est collecté en tant que produit, et la vapeur instantanée à basse température est soumise à un échange de chaleur au moyen des échangeurs de chaleur (E3 et E4) et pressurisée au moyen d'un compresseur (C2), puis divisée en deux parties. Une partie est mélangée avec le gaz riche en méthane et introduite dans les échangeurs de chaleur (E3 et E4), et l'autre partie est introduite successivement dans les échangeurs de chaleur (E3 et E4) et dans un détendeur (P1) afin de subir respectivement un refroidissement et une détente, et le matériau détendu est introduit dans les échangeurs de chaleur (E3 et E4) afin d'assurer une capacité de refroidissement, puis il est retourné afin d'être mis sous pression après l'échange de chaleur et introduit dans un cycle ultérieur.
PCT/CN2016/078263 2016-01-15 2016-04-01 Procédé et appareil de liquéfaction de gaz riche en méthane par réfrigération par détente WO2017121042A1 (fr)

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CN108036583A (zh) * 2018-01-15 2018-05-15 杭州中泰深冷技术股份有限公司 一种混合烷烃反应产物膨胀制冷分离系统及其方法
CN108641750A (zh) * 2018-05-09 2018-10-12 天津市天地创智科技发展有限公司 一种基于氩循环制冷的干气分离系统干气分离系统及分离方法
CN108676579A (zh) * 2018-05-09 2018-10-19 天津市天地创智科技发展有限公司 一种基于氩循环制冷的干气顺序分离系统及分离方法
CN112226259A (zh) * 2020-10-20 2021-01-15 中海石油(中国)有限公司 一种高效紧凑的海上油田伴生气回收利用装置
CN113932564A (zh) * 2021-09-08 2022-01-14 势加透博（上海）能源科技有限公司 采用液化天然气蓄冷的液化空气储能系统及其方法
CN114413573A (zh) * 2022-01-20 2022-04-29 四川空分设备(集团)有限责任公司 基于绕管式换热器的天然气液化系统及工艺
CN114659338A (zh) * 2022-03-24 2022-06-24 浙江大学 一种用于分离天然气bog中重烃和甲烷的制冷系统和方法

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CN107514872B (zh) * 2017-09-27 2022-11-25 中科瑞奥能源科技股份有限公司 从lng储罐闪蒸汽中回收氦气的工艺与系统

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CN108036583A (zh) * 2018-01-15 2018-05-15 杭州中泰深冷技术股份有限公司 一种混合烷烃反应产物膨胀制冷分离系统及其方法
CN108036583B (zh) * 2018-01-15 2023-12-01 杭州中泰深冷技术股份有限公司 一种混合烷烃反应产物膨胀制冷分离系统及其方法
CN108641750A (zh) * 2018-05-09 2018-10-12 天津市天地创智科技发展有限公司 一种基于氩循环制冷的干气分离系统干气分离系统及分离方法
CN108676579A (zh) * 2018-05-09 2018-10-19 天津市天地创智科技发展有限公司 一种基于氩循环制冷的干气顺序分离系统及分离方法
CN108676579B (zh) * 2018-05-09 2023-04-25 天津市天地创智科技发展有限公司 一种基于氩循环制冷的干气顺序分离系统及分离方法
CN108641750B (zh) * 2018-05-09 2023-04-25 天津市天地创智科技发展有限公司 一种基于氩循环制冷的干气分离系统及分离方法
CN112226259A (zh) * 2020-10-20 2021-01-15 中海石油(中国)有限公司 一种高效紧凑的海上油田伴生气回收利用装置
CN113932564A (zh) * 2021-09-08 2022-01-14 势加透博（上海）能源科技有限公司 采用液化天然气蓄冷的液化空气储能系统及其方法
CN114413573A (zh) * 2022-01-20 2022-04-29 四川空分设备(集团)有限责任公司 基于绕管式换热器的天然气液化系统及工艺
CN114413573B (zh) * 2022-01-20 2023-11-17 四川空分设备(集团)有限责任公司 基于绕管式换热器的天然气液化系统及工艺
CN114659338A (zh) * 2022-03-24 2022-06-24 浙江大学 一种用于分离天然气bog中重烃和甲烷的制冷系统和方法

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