WO2017121042A1 - 一种膨胀制冷富甲烷气液化的方法及装置 - Google Patents
一种膨胀制冷富甲烷气液化的方法及装置 Download PDFInfo
- Publication number
- 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
- Authority
- WO
- WIPO (PCT)
- Prior art keywords
- gas
- methane
- heat exchanger
- rich
- low
- Prior art date
Links
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 title claims abstract description 228
- 238000005057 refrigeration Methods 0.000 title claims abstract description 41
- 238000000034 method Methods 0.000 title claims abstract description 32
- 239000000463 material Substances 0.000 claims abstract description 118
- 239000007788 liquid Substances 0.000 claims abstract description 44
- 229930195733 hydrocarbon Natural products 0.000 claims abstract description 24
- 150000002430 hydrocarbons Chemical class 0.000 claims abstract description 24
- 239000007791 liquid phase Substances 0.000 claims abstract description 17
- 238000001816 cooling Methods 0.000 claims abstract description 16
- 238000000926 separation method Methods 0.000 claims description 33
- 239000002994 raw material Substances 0.000 claims description 15
- 239000004215 Carbon black (E152) Substances 0.000 claims description 13
- 239000012071 phase Substances 0.000 claims description 11
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims description 6
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 claims description 6
- AMXOYNBUYSYVKV-UHFFFAOYSA-M lithium bromide Chemical compound [Li+].[Br-] AMXOYNBUYSYVKV-UHFFFAOYSA-M 0.000 claims description 6
- 239000002826 coolant Substances 0.000 claims description 4
- 229910021529 ammonia Inorganic materials 0.000 claims description 3
- 239000001294 propane Substances 0.000 claims description 3
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 claims description 3
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 claims description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 3
- 238000001704 evaporation Methods 0.000 claims description 2
- 239000003507 refrigerant Substances 0.000 claims description 2
- 239000000203 mixture Substances 0.000 abstract 1
- 239000007789 gas Substances 0.000 description 114
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 24
- 239000003949 liquefied natural gas Substances 0.000 description 12
- 229910052757 nitrogen Inorganic materials 0.000 description 12
- 238000005265 energy consumption Methods 0.000 description 8
- 239000003345 natural gas Substances 0.000 description 7
- 230000000694 effects Effects 0.000 description 5
- 238000010586 diagram Methods 0.000 description 4
- XKRFYHLGVUSROY-UHFFFAOYSA-N Argon Chemical compound [Ar] XKRFYHLGVUSROY-UHFFFAOYSA-N 0.000 description 2
- JVFDADFMKQKAHW-UHFFFAOYSA-N C.[N] Chemical compound C.[N] JVFDADFMKQKAHW-UHFFFAOYSA-N 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 238000011084 recovery Methods 0.000 description 2
- 229910052786 argon Inorganic materials 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000006835 compression Effects 0.000 description 1
- 238000007906 compression Methods 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 230000006837 decompression Effects 0.000 description 1
- 239000000284 extract Substances 0.000 description 1
- 239000001307 helium Substances 0.000 description 1
- 229910052734 helium Inorganic materials 0.000 description 1
- SWQJXJOGLNCZEY-UHFFFAOYSA-N helium atom Chemical compound [He] SWQJXJOGLNCZEY-UHFFFAOYSA-N 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- 229910052739 hydrogen Inorganic materials 0.000 description 1
- 125000004435 hydrogen atom Chemical class [H]* 0.000 description 1
- 230000007774 longterm Effects 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 238000003303 reheating Methods 0.000 description 1
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
- 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.
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)
- Separation By Low-Temperature Treatments (AREA)
Abstract
Description
Claims (10)
- 一种膨胀制冷富甲烷气液化的方法,其特征在于,包括如下步骤:(1)富甲烷气液化:所述步骤1的操作如下:富甲烷原料气与部分预热气混合后,经换热器冷却至-10~-90℃,再进入重烃分离器脱重烃,得到低温干气,低温干气再经换热器冷却后,经节流降压,再进行气液分离,分离后分别得到液化富甲烷气、低温闪蒸气,液化富甲烷气作为产品收集,低温闪蒸气经换热器换热后,进行增压,进入下一个循环;若富甲烷原料气无重烃,则富甲烷原料气与部分预热气混合后,直接经换热器冷却,再经节流降压后,进行气液分离,分离后分别得到液化富甲烷气、低温闪蒸气,液化富甲烷气作为产品收集,低温闪蒸气经换热器换热后,进行增压,进入下一个循环;(2)开式循环制冷:所述步骤2的操作如下:低温闪蒸气经换热器换热后,得到预热气,将预热气进行增压,增压后将其分为第一股物料、第二股物料两股物料,第一股物料经换热器换热后送入膨胀机中,或者第一股物料不经换热器换热而直接送入膨胀机中,得到膨胀物料,膨胀物料经换热器换热后与预热气混合,进入下一个循环,第二股物料即为所述步骤1中与富甲烷原料气混合的部分预热气;提供另一种替换方法,包括如下步骤:(1)富甲烷气液化:所述步骤1的操作如下:低温闪蒸气经换热器换热后,得到预热气,将预热气进行增压,并将富甲烷原料气与预热气混合,混合的物料经换热器冷却至-10~-90℃,再进入重烃分离器脱重烃,得到低温干气,低温干气再经换热器冷却后,经节流降压,再进行气液分离,分离后分别得到液化富甲烷气、低温闪蒸气,液化富甲烷气作为产品收集,低温闪蒸气经换热器换热后,进行增压,进入下一个循环;若富甲烷原料气无重烃,则富甲烷原料气与部分预热气混合后,直接经换热器冷却,再经节流降压后,进行气液分离,分离后分别得到液化富甲烷气、低温闪蒸气,液化富甲烷气作为产品收集,低温闪蒸气经换热器换热后,进行增压,进入下一个循环;(2)闭式循环制冷所述步骤2的操作如下:冷却介质经增压后,再经换热器换热,进入膨胀机中,或者冷却介质经增压后不经换热器换热而直接送入膨胀机中,得到膨胀物料,膨胀物料再经换热器换热后,返回增压,进入下一个循环;所述步骤1中,富甲烷原料气的压力为1MPaG~20MPaG、温度为-30~60℃,或所述富甲烷 原料气为LNG储罐的自蒸发气。
- 根据权利要求1所述膨胀制冷富甲烷气液化的方法,其特征在于,所述部分预热气与富甲烷原料气混合,形成两股物料进入换热器;或预热气与富甲烷原料气完全混合,再分为两股进入换热器。
- 根据权利要求1或2所述膨胀制冷富甲烷气液化的方法,其特征在于,所述步骤1中,低温干气经换热器冷却后,再进行节流降压,节流的级数为一级节流、二级节流、三级节流或四级节流。
- 根据权利要求1所述膨胀制冷富甲烷气液化的方法,其特征在于,所述步骤1中,低温干气经换热器冷却后,再经节流降压,然后进入第一气液分离器进行气液分离,分离后分别得到第一液相物、第一气相物,该第一液相物即为液化富甲烷气,该第一气相物即为低温闪蒸气。
- 根据权利要求4所述膨胀制冷富甲烷气液化的方法,其特征在于,所述步骤1中,第一液相物再经节流降压后,进入第二气液分离器进行气液分离,分离后分别得到第二液相物、第二气相物,该第二液相物即为液化富甲烷气,该第一气相物和第二气相物即为低温闪蒸气。
- 根据权利要求1~5任一项所述膨胀制冷富甲烷气液化的方法,其特征在于,还包括预冷步骤:将外部冷却与换热器相连,通过外部冷却对换热器中的其他部件进行预冷。
- 根据权利要求6所述膨胀制冷富甲烷气液化的方法,其特征在于,所述外部冷却采用的典型冷剂为丙烯、丙烷、氨、氟利昂、水、BOG、溴化锂中的一种或多种。
- 根据权利要求1~7任一项所述膨胀制冷富甲烷气液化的方法,其特征在于,含甲烷的不易液化气体能从***的任何物料中引出。
- 根据权利要求1~8任一项所述膨胀制冷富甲烷气液化的方法,其特征在于,步骤2中,根据富甲烷原料气的压力和温度,在***合适的位置与预热气混合。
- 用于前述权利要求1~9任一项所述方法的装置,其特征在于,包括富甲烷气液化***、开式循环制冷***;所述富甲烷气液化***包括用于输送富甲烷原料气的原料供应装置、换热器、气液分离器,所述原料供应装置、换热器、气液分离器通过管道依次相连;所述开式循环制冷***包括气液分离器、换热器、压缩机、膨胀机,所述气液分离器、换热器、压缩机、膨胀机通过管道构成开式循环***;提供另一种替换装置,包括富甲烷气液化***、闭式循环制冷***;所述甲烷气液化***包括原料供应装置、换热器、气液分离器、压缩机,所述原料供应装置、换热器、气液分离器、压缩机通过管道依次相连;所述闭式循环制冷***包括压缩机、换热器、膨胀机,所述压缩机、换热器、膨胀机通过管道构成闭式循环***。
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
CN201610024569.0 | 2016-01-15 | ||
CN201610024569 | 2016-01-15 |
Publications (1)
Publication Number | Publication Date |
---|---|
WO2017121042A1 true WO2017121042A1 (zh) | 2017-07-20 |
Family
ID=56225064
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
PCT/CN2016/078263 WO2017121042A1 (zh) | 2016-01-15 | 2016-04-01 | 一种膨胀制冷富甲烷气液化的方法及装置 |
Country Status (2)
Country | Link |
---|---|
CN (1) | CN105674686B (zh) |
WO (1) | WO2017121042A1 (zh) |
Cited By (7)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
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***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***干气分离***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***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***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***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***和方法 |
Families Citing this family (2)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
WO2017121042A1 (zh) * | 2016-01-15 | 2017-07-20 | 成都赛普瑞兴科技有限公司 | 一种膨胀制冷富甲烷气液化的方法及装置 |
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*** |
Citations (6)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
CN103215093A (zh) * | 2013-03-14 | 2013-07-24 | 上海交通大学 | 小型撬装式氮膨胀天然气液化***及其方法 |
CN103438661A (zh) * | 2013-08-30 | 2013-12-11 | 北京麦科直通石化工程设计有限公司 | 一种低能耗的新型天然气液化工艺 |
WO2014021900A1 (en) * | 2012-08-03 | 2014-02-06 | Air Products And Chemicals, Inc. | Heavy hydrocarbon removal from a natural gas stream |
GB2522421A (en) * | 2014-01-22 | 2015-07-29 | Anthony Dwight Maunder | LNG production process |
CN204718297U (zh) * | 2015-05-22 | 2015-10-21 | 新奥气化采煤有限公司 | 放散天然气利用装置及天然气管网压力能回收利用*** |
CN105674686A (zh) * | 2016-01-15 | 2016-06-15 | 成都赛普瑞兴科技有限公司 | 一种膨胀制冷富甲烷气液化的方法及装置 |
Family Cites Families (6)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
MY122625A (en) * | 1999-12-17 | 2006-04-29 | Exxonmobil Upstream Res Co | Process for making pressurized liquefied natural gas from pressured natural gas using expansion cooling |
RU2272973C1 (ru) * | 2004-09-24 | 2006-03-27 | Салават Зайнетдинович Имаев | Способ низкотемпературной сепарации газа (варианты) |
EP1939564A1 (en) * | 2006-12-26 | 2008-07-02 | Repsol Ypf S.A. | Process to obtain liquefied natural gas |
GB2486036B (en) * | 2011-06-15 | 2012-11-07 | Anthony Dwight Maunder | Process for liquefaction of natural gas |
CN103075868B (zh) * | 2011-10-25 | 2015-09-23 | 中国石油天然气股份有限公司 | 一种天然气的液化***和液化方法 |
CN102492505B (zh) * | 2011-12-01 | 2014-04-09 | 中国石油大学(北京) | 一种两段式单循环混合制冷剂天然气液化工艺及设备 |
-
2016
- 2016-04-01 WO PCT/CN2016/078263 patent/WO2017121042A1/zh active Application Filing
- 2016-04-01 CN CN201610203041.XA patent/CN105674686B/zh active Active
Patent Citations (6)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
WO2014021900A1 (en) * | 2012-08-03 | 2014-02-06 | Air Products And Chemicals, Inc. | Heavy hydrocarbon removal from a natural gas stream |
CN103215093A (zh) * | 2013-03-14 | 2013-07-24 | 上海交通大学 | 小型撬装式氮膨胀天然气液化***及其方法 |
CN103438661A (zh) * | 2013-08-30 | 2013-12-11 | 北京麦科直通石化工程设计有限公司 | 一种低能耗的新型天然气液化工艺 |
GB2522421A (en) * | 2014-01-22 | 2015-07-29 | Anthony Dwight Maunder | LNG production process |
CN204718297U (zh) * | 2015-05-22 | 2015-10-21 | 新奥气化采煤有限公司 | 放散天然气利用装置及天然气管网压力能回收利用*** |
CN105674686A (zh) * | 2016-01-15 | 2016-06-15 | 成都赛普瑞兴科技有限公司 | 一种膨胀制冷富甲烷气液化的方法及装置 |
Cited By (11)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
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***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***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***干气分离***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***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***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***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***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***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***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***和方法 |
Also Published As
Publication number | Publication date |
---|---|
CN105674686A (zh) | 2016-06-15 |
CN105674686B (zh) | 2018-09-14 |
Similar Documents
Publication | Publication Date | Title |
---|---|---|
WO2017121042A1 (zh) | 一种膨胀制冷富甲烷气液化的方法及装置 | |
US6412302B1 (en) | LNG production using dual independent expander refrigeration cycles | |
US6751985B2 (en) | Process for producing a pressurized liquefied gas product by cooling and expansion of a gas stream in the supercritical state | |
US6378330B1 (en) | Process for making pressurized liquefied natural gas from pressured natural gas using expansion cooling | |
JP5984192B2 (ja) | 天然ガスの液化プロセス | |
US7469556B2 (en) | Natural gas liquefaction system | |
AU674813B2 (en) | Process and apparatus for producing liquefied natural gas | |
US20060225461A1 (en) | Process for sub-cooling an LNG stream obtained by cooling by means of a first refrigeration cycle, and associated installation | |
EA006724B1 (ru) | Способ получения сжиженного природного газа (варианты) | |
RU2011124891A (ru) | Способ и система сжижения | |
JP6415329B2 (ja) | ガス液化装置及びガス液化方法 | |
CN105823304A (zh) | 一种双级膨胀制冷富甲烷气液化的方法及装置 | |
JP2016128738A5 (zh) | ||
US20100154469A1 (en) | Process and system for liquefaction of hydrocarbon-rich gas stream utilizing three refrigeration cycles | |
CN216620451U (zh) | 一种lng重整制氢和lng冷能液化氢气一体化*** | |
US20230332833A1 (en) | Process for Producing Liquefied Hydrogen | |
CN105737516A (zh) | 混合制冷剂预冷氮气膨胀的天然气液化***及方法 | |
CN205448491U (zh) | 含氧煤层气液化分离*** | |
KR20180130029A (ko) | 천연가스 액화장치 및 액화방법 | |
CN109734064B (zh) | 一种氦气生产***和生产方法 | |
CN114659338B (zh) | 一种用于分离天然气bog中重烃和甲烷的制冷***和方法 | |
CN218764248U (zh) | 一种丙烷预冷双氮膨胀制冷天然气提粗氦联产lng的装置 | |
CN219149269U (zh) | 一种低压原料气高压干气的乙烷回收装置 | |
MX2023014287A (es) | Sistema y metodo de licuefaccion de hidrogeno. | |
US10330381B2 (en) | Plant for the liquefaction of nitrogen using the recovery of cold energy deriving from the evaporation of liquefied natural gas |
Legal Events
Date | Code | Title | Description |
---|---|---|---|
121 | Ep: the epo has been informed by wipo that ep was designated in this application |
Ref document number: 16884602 Country of ref document: EP Kind code of ref document: A1 |
|
NENP | Non-entry into the national phase |
Ref country code: DE |
|
32PN | Ep: public notification in the ep bulletin as address of the adressee cannot be established |
Free format text: NOTING OF LOSS OF RIGHTS PURSUANT TO RULE 112(1) EPC (EPO FORM 1205A DATED 05/12/2018) |
|
32PN | Ep: public notification in the ep bulletin as address of the adressee cannot be established |
Free format text: NOTING OF LOSS OF RIGHTS PURSUANT TO RULE 112(1) EPC (EPO FORM 1205A DATED 05/12/2018) |
|
122 | Ep: pct application non-entry in european phase |
Ref document number: 16884602 Country of ref document: EP Kind code of ref document: A1 |