CN212538459U - System for utilize LNG apparatus for producing coproduction helium - Google Patents

System for utilize LNG apparatus for producing coproduction helium Download PDF

Info

Publication number
CN212538459U
CN212538459U CN202021219265.8U CN202021219265U CN212538459U CN 212538459 U CN212538459 U CN 212538459U CN 202021219265 U CN202021219265 U CN 202021219265U CN 212538459 U CN212538459 U CN 212538459U
Authority
CN
China
Prior art keywords
gas
helium
heat exchanger
bog
cryogenic
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.)
Active
Application number
CN202021219265.8U
Other languages
Chinese (zh)
Inventor
徐鹏
王广海
熊联友
雷灵龙
汤建成
高金林
龚领会
赵光明
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.)
Beijing Zhongke Fu Hai Low Temperature Technology Co ltd
Technical Institute of Physics and Chemistry of CAS
Original Assignee
Beijing Zhongke Fu Hai Low Temperature Technology Co ltd
Technical Institute of Physics and Chemistry of CAS
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 Beijing Zhongke Fu Hai Low Temperature Technology Co ltd, Technical Institute of Physics and Chemistry of CAS filed Critical Beijing Zhongke Fu Hai Low Temperature Technology Co ltd
Priority to CN202021219265.8U priority Critical patent/CN212538459U/en
Application granted granted Critical
Publication of CN212538459U publication Critical patent/CN212538459U/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
    • F25J3/06—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation
    • F25J3/063—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 separated product stream
    • F25J3/0685—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 separated product stream separation of noble gases
    • F25J3/069—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 separated product stream separation of noble gases of helium
    • 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
    • F25J1/02—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
    • F25J1/0228—Coupling of the liquefaction unit to other units or processes, so-called integrated processes
    • 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
    • F25J3/061—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
    • F25J3/06—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation
    • F25J3/063—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 separated product stream
    • F25J3/0635—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 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
    • F25J3/06—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation
    • F25J3/063—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 separated product stream
    • F25J3/066—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 separated product stream separation of nitrogen
    • 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
    • F25J2205/40—Processes or apparatus using other separation and/or other processing means using hybrid system, i.e. combining cryogenic and non-cryogenic separation techniques
    • 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
    • F25J2205/60—Processes or apparatus using other separation and/or other processing means using adsorption on solid adsorbents, e.g. by temperature-swing adsorption [TSA] at the hot or cold end
    • 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
    • F25J2205/82—Processes or apparatus using other separation and/or other processing means using a reactor with combustion or catalytic reaction
    • 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
    • F25J2210/00—Processes characterised by the type or other details of the feed stream
    • F25J2210/04—Mixing or blending of fluids with 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
    • F25J2210/00—Processes characterised by the type or other details of the feed stream
    • F25J2210/42—Nitrogen
    • 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
    • F25J2210/00—Processes characterised by the type or other details of the feed stream
    • F25J2210/90—Boil-off gas from storage
    • 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
    • F25J2230/30—Compression 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
    • F25J2245/00—Processes or apparatus involving steps for recycling of process streams
    • F25J2245/02—Recycle of a stream in general, e.g. a by-pass 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
    • F25J2245/00—Processes or apparatus involving steps for recycling of process streams
    • F25J2245/90—Processes or apparatus involving steps for recycling of process streams the recycled stream being boil-off gas from storage
    • 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
    • F25J2270/90—External refrigeration, e.g. conventional closed-loop mechanical refrigeration unit using Freon or NH3, unspecified external refrigeration
    • F25J2270/908—External refrigeration, e.g. conventional closed-loop mechanical refrigeration unit using Freon or NH3, unspecified external refrigeration by regenerative chillers, i.e. oscillating or dynamic systems, e.g. Stirling refrigerator, thermoelectric ("Peltier") or magnetic refrigeration
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/90—External refrigeration, e.g. conventional closed-loop mechanical refrigeration unit using Freon or NH3, unspecified external refrigeration
    • F25J2270/908—External refrigeration, e.g. conventional closed-loop mechanical refrigeration unit using Freon or NH3, unspecified external refrigeration by regenerative chillers, i.e. oscillating or dynamic systems, e.g. Stirling refrigerator, thermoelectric ("Peltier") or magnetic refrigeration
    • F25J2270/91—External refrigeration, e.g. conventional closed-loop mechanical refrigeration unit using Freon or NH3, unspecified external refrigeration by regenerative chillers, i.e. oscillating or dynamic systems, e.g. Stirling refrigerator, thermoelectric ("Peltier") or magnetic refrigeration using pulse tube refrigeration
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/90—External refrigeration, e.g. conventional closed-loop mechanical refrigeration unit using Freon or NH3, unspecified external refrigeration
    • F25J2270/912—Liquefaction cycle of a low-boiling (feed) gas in a cryocooler, i.e. in a closed-loop refrigerator
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2290/00—Other details not covered by groups F25J2200/00 - F25J2280/00
    • F25J2290/80—Retrofitting, revamping or debottlenecking of existing plant

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

A system for co-producing helium with an LNG production plant, comprising: raw material gas compressor, dehydrogenation and CO removal2Dehydration drying mechanism, low-temperature separation and cryrogenic adsorption element, helium storage tank and catalytic deoxidation device, feed gas compressor, dehydrogenation and drying mechanism and low-temperature separation and cryrogenic adsorption element set gradually on helium coproduction route, helium storage tank and catalytic deoxidation device are connected to low-temperature separation and cryrogenic adsorption element respectively, feed gas compressor is used for further compressing another part BOG gas after first BOG compressor compression, dehydrogenation and drying element are used for further compressing feed gas compressorThe compressed BOG gas is subjected to dehydrogenation and drying treatment, the low-temperature separation and cryogenic adsorption mechanism is used for cooling, condensing and adsorbing and separating the BOG gas subjected to dehydrogenation treatment to obtain high-purity helium and BOG gas subjected to helium extraction, the helium storage tank is used for storing the high-purity helium, and the catalytic deoxidation device is used for deoxidizing the BOG gas subjected to helium extraction. The present application improves the economics of helium extraction.

Description

System for utilize LNG apparatus for producing coproduction helium
Technical Field
The application relates to the technical field of helium extraction, in particular to a system for co-producing helium by using an LNG production device.
Background
Helium has special properties such as extremely low boiling point, density, strong chemistry, radioactive inertness and the like, is one of indispensable important gases for developing national defense military industry and high technology, and has irreplaceable effects in the fields of national defense, industry and science and technology such as aerospace, nuclear weapons, submarines, saturated diving operation, nuclear magnetic resonance, semiconductors, mobile phones, liquid crystal screens, optical fibers, large scientific devices and the like.
Helium is present in air at only 5ppm, primarily in natural gas, and therefore helium is produced almost entirely from natural gas. The natural gas in the United states is rich in helium resources, the helium content is high (about 0.8 percent on average and is respectively as high as 7.5 percent), and the yield and the consumption amount are the first of the whole world. China is short in helium resources, the content of helium in natural gas is only 0.2% at most, and the value of economically extracting helium is not achieved. Therefore, China has been dependent on importing the required helium from abroad. The helium gas is expensive, so that the method has great influence on the field of using a large amount of helium in China and related scientific research and production units.
At present, in certain natural gas fields in China, the helium content in natural gas is about 0.04-0.2%, and although the helium content is very low, the total storage capacity is huge. For convenience of peak regulation and point supply, pipeline Natural Gas is usually Liquefied for storage and transportation, and the device for liquefying Natural Gas is an LNG (Liquefied Natural Gas) production device. In the LNG production process, a large amount of flash steam is generated in the throttling process of the last-stage throttling valve, the liquefaction temperatures of helium, hydrogen, nitrogen and methane are-269 ℃, 253 ℃, 196 ℃ and-162 ℃ respectively at normal pressure, and the helium, the hydrogen and part of the nitrogen volatilize from the LNG under the pressure of the storage tank. The Gas-liquid mixture at the outlet of the final-stage throttling valve enters an LNG large storage tank through an LNG low-temperature pipeline, and due to heat leakage of the storage tank and generation of Boil-Off Gas (the part of Gas is mainly methane and nitrogen) in a loading station, the two parts of Gas are mixed and are collectively called BOG (Boil-Off Gas).
In the actual operation process, the BOG gas flow is also considerable and can maximally account for about 8 percent of the raw material gas flow, so that the BOG gas can be recovered by a special recovery process in the LNG production process
As the BOG gas is concentrated and enriched with non-condensable gases such as helium, hydrogen and the like, the helium in the BOG gas can be enriched by two orders of magnitude compared with the natural gas feed gas, and the BOG gas which is conventionally burnt as fuel gas completely has the industrial development value of purifying the helium.
SUMMERY OF THE UTILITY MODEL
In view of this, it is necessary to provide a system for co-producing helium by using an LNG production apparatus to purify flash steam generated during LNG production and storage.
In order to solve the technical problem, the application provides a system for utilize LNG apparatus for producing coproduction helium, and LNG apparatus for producing includes natural gas liquefaction mechanism, LNG basin and first BOG compressor, and first BOG compressor is used for compressing the BOG gas that comes from the LNG basin, through first BOAfter the compression of the G compressor, part of BOG gas is converged into a natural gas liquefaction mechanism to be liquefied again; utilize system of LNG apparatus for producing coproduction helium includes: raw material gas compressor, dehydrogenation and CO removal2Dehydration drying mechanism, low-temperature separation and cryogenic adsorption mechanism, helium storage tank and catalytic deoxidation device, raw material gas compressor, dehydrogenation and CO removal2The dehydration drying mechanism and the low-temperature separation and cryogenic adsorption mechanism are sequentially arranged on a helium gas CO-production path, the helium gas storage tank and the catalytic deoxidation device are respectively connected to the low-temperature separation and cryogenic adsorption mechanism, the feed gas compressor is used for further compressing, dehydrogenating and removing CO from the other part of BOG gas compressed by the first BOG compressor2The dehydration and drying mechanism is used for dehydrogenation and CO removal of BOG gas further compressed by the feed gas compressor2And (3) dehydrating and drying, wherein a low-temperature separation and cryogenic adsorption mechanism is used for cooling, condensing and adsorbing the dehydrogenated BOG gas to obtain high-purity helium and the helium-extracted BOG gas, a helium storage tank is used for storing the high-purity helium, and a catalytic deoxidation device is used for deoxidizing the helium-extracted BOG gas.
The low-temperature separation and cryogenic adsorption mechanism comprises a low-temperature condensation separation mechanism and a cryogenic adsorption mechanism, the low-temperature condensation separation mechanism comprises a first heat exchanger, a first gas-liquid separator, a second heat exchanger, a second gas-liquid separator, a third heat exchanger, a third gas-liquid separator and a fourth gas-liquid separator, a crude helium purification pipeline is sequentially connected with a BOG inlet and a BOG outlet of the first heat exchanger, a BOG inlet and a BOG gas outlet of the first gas-liquid separator, a BOG inlet and a BOG outlet of the second heat exchanger, a BOG inlet and a BOG gas outlet of the second gas-liquid separator, a BOG inlet and a BOG outlet of the third heat exchanger, a BOG inlet and a crude helium gas outlet of the third gas-liquid separator, condensate outlets of the first gas-liquid separator, the second gas-liquid separator and the third gas-liquid separator are respectively communicated to the upper part of the fourth gas-liquid separator, and a gas outlet of the fourth gas-, The condensed fluid outlet is communicated to the catalytic deoxidation device; and a crude helium outlet of the third gas-liquid separator is communicated with the cryogenic adsorption mechanism.
The low-temperature condensation separation mechanism further comprises a liquid nitrogen storage tank, and the liquid nitrogen storage tank is communicated with the second heat exchanger and the first heat exchanger sequentially through pipelines.
Wherein, cryocondensation separating mechanism still includes the negative pressure liquid nitrogen container, the liquid level governing valve, negative pressure liquid nitrogen vacuum pump and liquid nitrogen vacuum control valve, the liquid nitrogen storage tank is used for providing liquid nitrogen for it through setting up liquid level governing valve's pipeline and negative pressure liquid nitrogen container intercommunication, the liquid nitrogen export of negative pressure liquid nitrogen container bottom communicates with the liquid nitrogen entry of third heat exchanger, the liquid nitrogen export of third heat exchanger communicates with the liquid nitrogen backward flow mouth on negative pressure liquid nitrogen container upper portion, negative pressure liquid nitrogen vacuum pump communicates through the evacuation mouth that sets up liquid nitrogen vacuum control valve's pipeline and negative pressure liquid nitrogen container top.
The cryogenic adsorption mechanism comprises a first cryogenic adsorption unit, a second cryogenic adsorption unit and a regeneration unit, the first cryogenic adsorption unit comprises a first cryogenic adsorption tower, a first air inlet valve and a first air outlet valve which are respectively arranged on the air inlet side and the air outlet side of the first cryogenic adsorption tower, the second cryogenic adsorption unit comprises a second cryogenic adsorption tower, a second air inlet valve and a second air outlet valve which are respectively arranged on the air inlet side and the air outlet side of the second cryogenic adsorption tower, and the first air inlet valve and the second air inlet valve are both communicated with a crude helium outlet of the third gas-liquid separator; the regeneration unit comprises a first stop valve, a second stop valve and a heating and vacuumizing mechanism, the heating and vacuumizing mechanism is connected to the gas outlet side of the first low-temperature adsorption unit through the first stop valve, and the heating and vacuumizing mechanism is connected to the gas outlet side of the second low-temperature adsorption unit through the second stop valve.
The low-temperature separation and deep-cooling adsorption mechanism further comprises a low-temperature cold box, a first heat exchanger, a second heat exchanger, a third heat exchanger, a first gas-liquid separator, a second gas-liquid separator, a third gas-liquid separator and a fourth gas-liquid separator, and the first adsorption unit and the second adsorption unit are arranged in the low-temperature cold box.
The pipeline where the first gas outlet valve is located and the pipeline where the second gas outlet valve is located are connected in parallel and then are sequentially communicated with the third heat exchanger, the second heat exchanger and the first heat exchanger, and the third heat exchanger, the second heat exchanger and the first heat exchanger are used for sequentially returning the temperature of the high-purity helium gas discharged from the first low-temperature adsorption tower and the second low-temperature adsorption tower.
The crude helium outlet of the third gas-liquid separator is communicated with a third heat exchanger, a second heat exchanger and a first heat exchanger in sequence and then communicated with a cryogenic adsorption mechanism; the low-temperature condensation separation mechanism also comprises a low-temperature cold box, a first heat exchanger, a second heat exchanger, a third heat exchanger, a first gas-liquid separator, a second gas-liquid separator, a third gas-liquid separator and a fourth gas-liquid separator which are arranged in the low-temperature cold box; the cryogenic adsorption mechanism further comprises a liquid nitrogen Dewar, the first cryogenic adsorption unit further comprises a first cryogenic regenerative heat exchanger and a first liquid nitrogen immersed heat exchanger, and the second cryogenic adsorption unit further comprises a second cryogenic regenerative heat exchanger and a second liquid nitrogen immersed heat exchanger; the first cryogenic regenerative heat exchanger, the first liquid nitrogen immersed heat exchanger, the first low-temperature adsorption tower, the second cryogenic regenerative heat exchanger, the second liquid nitrogen immersed heat exchanger and the second low-temperature adsorption tower are arranged in the liquid nitrogen Dewar; a coarse helium outlet of the first heat exchanger is sequentially communicated with a coarse helium inlet and a coarse helium outlet of the first cryogenic regenerative heat exchanger, the first liquid nitrogen immersed heat exchanger, the first low-temperature adsorption tower, a high-purity helium inlet and a high-purity helium outlet of the first cryogenic regenerative heat exchanger and a first gas outlet valve through a first gas inlet valve; and a second air inlet valve is sequentially communicated with a coarse helium inlet and a coarse helium outlet of the second cryogenic regenerative heat exchanger, a second liquid nitrogen immersed heat exchanger, a second low-temperature adsorption tower, a high-purity helium inlet and a high-purity helium outlet of the second cryogenic regenerative heat exchanger, and a second air outlet valve.
Wherein the LNG production plant further comprises a fuel gas line connected to the output of the first BOG compressor, and the output of the catalytic deoxygenator device is connected to the fuel gas line and the natural gas liquefaction plant.
The helium purification device further comprises a helium extraction gas compressor, the helium extraction gas compressor is connected with the low-temperature separation and cryogenic adsorption mechanism and the catalytic deoxidation device, the helium extraction gas compressor is used for pressurizing the helium extraction BOG gas, and the catalytic deoxidation device is used for removing oxygen from the pressurized helium extraction BOG gas.
Wherein, LNG apparatus for producing still includes the second BOG compressor of connecting first BOG compressor and natural gas liquefaction mechanism.
Compared with the prior art, the system for co-producing helium by using the LNG production device is organically combined with the existing LNG production device, helium is extracted from one part of BOG gas, and helium enrichment is continuously performed on the other part of BOG gas, so that the economy of helium extraction is improved.
Drawings
The accompanying drawings, which are included to provide a further understanding of the application and are incorporated in and constitute a part of this application, illustrate embodiment(s) of the application and together with the description serve to explain the application and not to limit the application. In the drawings:
fig. 1 is a schematic diagram of a conventional LNG production plant for recovering BOG gas;
FIG. 2 is a schematic diagram of another prior art LNG production plant for the recovery of BOG gas;
FIG. 3 is a schematic diagram of yet another existing LNG production facility for BOG gas recovery;
FIG. 4 is an overall block diagram of a preferred embodiment of the system for co-producing helium using an LNG production facility;
FIG. 5 is a block diagram of a first embodiment of a cryogenic separation and cryogenic adsorption facility of the system for co-producing helium with an LNG production plant shown in FIG. 4;
FIG. 6 is a block diagram of a second embodiment of a cryogenic separation and cryogenic adsorption facility of the system for co-producing helium with an LNG production plant shown in FIG. 4;
FIG. 7 is a block diagram of a third embodiment of a cryogenic separation and cryogenic adsorption facility of the system for co-producing helium with an LNG production plant shown in FIG. 4;
FIG. 8 is a block diagram of a fourth embodiment of a cryogenic separation and cryogenic adsorption facility of the system for co-producing helium with an LNG production plant shown in FIG. 4;
fig. 9 is a structural view of a fifth embodiment of the cryogenic separation and cryogenic adsorption mechanism of the system for co-producing helium gas using an LNG production plant shown in fig. 4.
Detailed Description
In order to make the objects, technical solutions and advantages of the present application more apparent, the technical solutions of the present application will be described in detail and completely with reference to the following specific embodiments of the present application and the accompanying drawings. It should be apparent that the described embodiments are only some of the embodiments of the present application, and not all of the embodiments.
Fig. 4 is a preferred embodiment of a system for co-producing helium using an LNG production facility according to the present application. The LNG production device includes a raw material gas pretreatment unit 11, a natural gas liquefaction unit 12, a first BOG compressor 15, a second BOG compressor 16, and a regeneration unit 17. The raw material gas pretreatment mechanism 11, the natural gas liquefaction mechanism 12, the LNG storage tank 13 and the LNG loading station 14 are sequentially arranged and are respectively used for pretreating, liquefying, temporarily storing and transferring the raw material gas of the natural gas, and BOG gas generated by the LNG loading station 14 is collected to the LNG storage tank and then is output to the first BOG compressor 15 together with BOG gas in the LNG storage tank through a pipeline. The first BOG compressor 15 is used for compressing BOG gas from the LNG storage tank to medium pressure, after being compressed by the first BOG compressor, part of the BOG gas enters the second BOG compressor 16 as regenerated gas through the regeneration mechanism 17 and is compressed to the same pressure as the raw material gas, and then the compressed gas is converged before the raw material gas pretreatment mechanism 11 or enters the natural gas liquefaction mechanism 12 for reliquefaction according to the condition of the LNG production device, and regulating valves (switching valves) V1 and V2 are respectively arranged between the natural gas liquefaction mechanism 12 and the LNG storage tank 13 and between the second BOG compressor 16 and the regeneration mechanism 17.
The system for CO-producing helium by using the LNG production device specifically comprises a feed gas compressor 21, dehydrogenation and dry CO removal2 A dehydration mechanism 22, a low-temperature separation and cryogenic adsorption mechanism 23, a helium storage tank 24, a catalytic deoxidation device 26 and a helium extraction gas compressor 26. Feed gas compressor 21, dehydrogenation and CO removal2The dehydration drying mechanism 22 and the low-temperature separation and cryogenic adsorption mechanism 23 are sequentially arranged on a helium gas CO-production path, the helium gas storage tank 24 and the catalytic deoxidation device 25 are respectively connected to the low-temperature separation and cryogenic adsorption mechanism 23, and the raw gas compressor 21 is used for further compressing, dehydrogenating and removing CO from the other part of BOG gas compressed by the first BOG compressor 152The dehydration and drying mechanism 22 is used for dehydrogenation and CO removal of BOG gas further compressed by the raw gas compressor 212The dehydration and drying treatment is carried out on the mixture,the low-temperature separation and cryogenic adsorption mechanism 23 is used for cooling, condensing and adsorbing the dehydrogenated BOG gas to obtain high-purity helium and the helium-extracted BOG gas, the helium storage tank 24 is used for storing the high-purity helium, and the catalytic deoxidation device 25 is used for deoxidizing the helium-extracted BOG gas. The helium-extracted gas compressor 26 is connected with the low-temperature separation and cryogenic adsorption mechanism 23 and the catalytic deoxidation device 25, the helium-extracted gas compressor 26 is used for pressurizing the helium-extracted BOG gas, and the catalytic deoxidation device 25 is used for removing oxygen from the pressurized helium-extracted BOG gas.
In this embodiment, the LNG production plant further comprises a fuel gas line connected to the output of the first BOG compressor 15, and the output of the catalytic deoxygenator is connected to the fuel gas line and the natural gas liquefaction plant by regulating valves V5 and V6, respectively. And the combustion of the BOG gas after helium extraction is favorable for not influencing the design flow of the first BOG compressor and the second BOG compressor.
Dehydrogenation and CO removal2The dehydration drying mechanism 22 includes a catalytic dehydrogenation device and a dehydration drying device.
BOG gas is often a mixture of methane, nitrogen, helium, hydrogen, and trace ethane gas, and a large amount of test data indicates that the ratio of hydrogen content (by volume) to helium content (by volume) is often between 1: 9-3: 7, therefore, the hydrogen needs to be removed by catalytic oxidation at the upstream of the helium extracting device so as to prevent the hydrogen from being too high in content after being concentrated at the downstream and difficult to remove.
The catalytic dehydrogenation device makes hydrogen in BOG react with oxygen which is metered in under the action of a specific catalyst at a certain temperature, so that the hydrogen completely reacts and is converted into water, and the reaction formula is as follows:
2H2+O2＝2H2O。
in the process, hydrogen and oxygen completely react, and the content of the hydrogen after the reaction is not higher than 1 ppm. Meanwhile, due to the high methane content in the BOG gas, the following reactions often exist in minute quantities while the catalytic dehydrogenation is carried out:
CH4+2O2＝CO2+2H2O
in metering oxygenIn order to ensure complete removal of hydrogen, an excess of oxygen is often required. The water generated in the reaction is discharged from the device through cooling and condensation, and the rest water vapor and trace CO are discharged2By switched CO removal2The dehydration drying device removes the hydrogen, and the gas obtained at this time is dehydrogenation gas.
The dehydrogenation gas, which consists of methane, nitrogen, helium and trace amounts of ethane, is fed to the cryogenic separation and cryogenic adsorption mechanism 23 for extraction of high purity helium. The low-temperature separation and cryogenic adsorption mechanism 23 comprises a low-temperature condensation separation mechanism 231 and a cryogenic adsorption mechanism 232; the low-temperature condensation separation mechanism 231 is used for cooling, fractional condensation and separation of the BOG gas after dehydrogenation step by step, so that a large amount of methane, nitrogen and trace ethane in the BOG gas after dehydrogenation can be condensed and removed to obtain crude helium; the cryogenic adsorption mechanism 232 removes residual nitrogen, trace methane and the like in the crude helium gas by utilizing the characteristics of large adsorption capacity and deep impurity removal degree of the adsorbent at low temperature, so as to obtain high-purity helium gas meeting the requirements. The high purity helium gas is then fed to helium storage tank 24 for temporary storage.
In view of economy, the BOG gas after helium extraction still needs to be recycled, but the BOG gas after helium extraction contains a certain amount of oxygen (not more than 0.2% -0.5% -V), which is derived from excessive oxygen in catalytic dehydrogenation. If the BOG gas after helium extraction is directly recycled without removing the oxygen, certain potential safety hazard exists. The BOG gas after helium extraction is subjected to deoxidation treatment through the catalytic deoxidation device, specifically, the BOG gas after helium extraction is firstly sent to the gas compressor 26 after helium extraction for pressurization, and is sent to the catalytic deoxidation device 25 for oxygen removal after reaching the pressure of the regenerated gas. Under the action of a specific catalyst, the methane in the BOG after helium extraction reacts with oxygen to generate CO2、H2O and possibly small amounts of H2. After the oxygen is completely removed, a part of the oxygen is sent to a fuel gas pipeline to be used as fuel gas for combustion, and the redundant gas is sent to the inlet of the second BOG compressor 16 and is converged into the existing LNG production device.
The low-temperature separation and cryogenic adsorption mechanism 23 comprises a low-temperature condensation separation mechanism 231 and a cryogenic adsorption mechanism 232, wherein the low-temperature condensation separation mechanism is a low-temperature separation mechanism with at least two stages of cooling, namely, the low-temperature condensation separation mechanism 231 at least comprises two stages of heat exchangers and a gas-liquid separator arranged in one-to-one correspondence with the heat exchangers, the at least two stages of heat exchangers gradually cool BOG gas, methane, nitrogen and trace ethane in the BOG gas after dehydrogenation are condensed and removed in a large quantity, crude helium is obtained, condensate enters the helium extraction gas compressor 26 through a pipeline, is compressed and then is sent to the catalytic deoxidation device 25 to remove oxygen. Because the solidification temperature points of methane and ethane gas are higher, the BOG gas must be cooled to the LNG temperature at the first-stage heat exchanger firstly, most of methane and ethane are condensed, separated and removed, and the BOG gas can be continuously cooled to the normal-pressure liquid nitrogen temperature or the negative-pressure liquid nitrogen temperature by the second-stage heat exchanger according to the difference of the nitrogen content in the BOG. The cryogenic adsorption mechanism 232 may be divided into an internal adsorption mode and an external adsorption mode. Five embodiments of the cryogenic separation and cryogenic adsorption mechanism 23 of the co-production helium system of the present application will be described in detail with reference to fig. 5 to 9, wherein fig. 5 to 7 show an internal adsorption mode, and fig. 8 to 9 show an external adsorption mode.
The first embodiment is as follows:
referring to fig. 5, the cryogenic separation and cryogenic adsorption mechanism 23 includes a cryogenic condensation separation mechanism 231, a cryogenic adsorption mechanism 232, and a cryogenic cooling tank 233.
The low-temperature condensation separation mechanism 231 comprises a first heat exchanger HEX1, a first gas-liquid separator, a second heat exchanger HEX2, a second gas-liquid separator S2, a third heat exchanger HEX3, a third gas-liquid separator S3 and a fourth gas-liquid separator S4, the dehydrogenation-treated crude helium purification pipeline is sequentially connected with a BOG inlet and a BOG outlet of a first heat exchanger HEXT, a BOG inlet and a BOG gas outlet of a first gas-liquid separator, a BOG inlet and a BOG outlet of a second heat exchanger HEX2, a BOG inlet and a BOG gas outlet of a second gas-liquid separator S2, a BOG inlet and a BOG outlet of a third heat exchanger HEX3, a BOG inlet and a crude helium gas outlet of a third gas-liquid separator S3, condensate outlets of the first, second and third gas-liquid separators S1, S2 and S3 are respectively communicated to the upper part of a fourth gas-liquid separator S4, and a gas outlet of the fourth gas-liquid separator S4 is used for discharging helium recovery cycle gas and is communicated to the catalytic deoxidation device 25; the crude helium outlet of the third gas-liquid separator S3 is communicated with the cryogenic adsorption mechanism 232.
The low-temperature condensation separation mechanism 231 further comprises a liquid nitrogen storage tank 2311, and the liquid nitrogen storage tank 2311 is sequentially communicated with the second heat exchanger HEX2 and the first heat exchanger HEX1 through pipelines.
The low-temperature condensation separation mechanism 231 further comprises a negative-pressure liquid nitrogen tank S5, a liquid level regulating valve V26, a negative-pressure liquid nitrogen vacuum pump 2312, a heater 2313 and a liquid nitrogen vacuum regulating valve V27, the liquid nitrogen storage tank 2311 is communicated with the negative-pressure liquid nitrogen tank S5 through a pipeline provided with the liquid level regulating valve V26 and used for providing liquid nitrogen for the negative-pressure liquid nitrogen tank, a liquid nitrogen outlet at the bottom of the negative-pressure liquid nitrogen tank S5 is communicated with a liquid nitrogen inlet of a third heat exchanger HEX3, a liquid nitrogen outlet of the third heat exchanger HEX3 is communicated with a liquid nitrogen return opening at the upper part of the negative-pressure liquid nitrogen tank S5, and the negative-pressure liquid nitrogen vacuum pump 2312 is communicated with a vacuum.
The cryogenic adsorption mechanism 232 includes a first cryogenic adsorption unit, a second cryogenic adsorption unit, and a regeneration unit. The first low-temperature adsorption unit comprises a first low-temperature adsorption tower A1, a first air inlet valve V31 and a first air outlet valve V32 which are respectively arranged on the air inlet side and the air outlet side of the first low-temperature adsorption tower A1, the second low-temperature adsorption unit comprises a second low-temperature adsorption tower A2, a second air inlet valve V33 and a second air outlet valve V34 which are respectively arranged on the air inlet side and the air outlet side of the second low-temperature adsorption tower A2, and the first air inlet valve V31 and the second air inlet valve V33 are communicated with a crude helium outlet of a third gas-liquid separator S3; the regeneration unit comprises a first stop valve V35, a second stop valve V36 and a heating and vacuumizing mechanism. The heating and vacuum-pumping mechanism includes a heater 2321 and a desorption vacuum pump 2322. The heater 2321 is connected to the gas outlet side of the first cryoadsorption unit a1 through a first cut-off valve V35, and the heater 2321 is connected to the gas outlet side of the second cryoadsorption unit a2 through a second cut-off valve V36.
The first, second and third heat exchangers HEX1, HEX2 and HEX3, the first, second, third and fourth gas-liquid separators S1, S2, S3 and S4, and the first and second adsorption units a1 and a2 are all disposed in the low-temperature cold box 233.
The pipeline where the first gas outlet valve V32 is located and the pipeline where the second gas outlet valve V34 is located are connected in parallel and then are sequentially communicated with a third heat exchanger HEX3, a second heat exchanger HEX2 and a first heat exchanger HEX1, and the third heat exchanger HEX3, the second heat exchanger HEX2 and the first heat exchanger HEX1 are used for sequentially returning the temperature of the high-purity helium gas discharged from the first low-temperature adsorption tower A1 and the second low-temperature adsorption tower A2.
The cryogenic adsorption mechanism 23 of the low-temperature separator of the embodiment has the following working process:
after entering the low-temperature cold box 233, the dehydrogenated BOG gas is first cooled to about-175 ℃ to-155 ℃ in a first heat exchanger HEX1, at which time most of the BOG gas becomes liquid, and is subjected to gas-liquid phase separation in a first gas-liquid separator S1. The saturated gas at the top of the first gas-liquid separator S1 is continuously fed into the second heat exchanger HEX2 to be cooled to about-193 ℃, part of the nitrogen/methane gas is liquefied, and gas-liquid phase separation is carried out in the second gas-liquid separator S2.
In this embodiment, the cold source in the second heat exchanger HEX2 comes from liquid nitrogen in the liquid nitrogen storage 2311, the liquid nitrogen is firstly adjusted to about 1.0bar.a through the throttle valve V5, and then the liquid nitrogen is sequentially introduced into the second heat exchanger HEX2 and the first heat exchanger HEX1 for heat exchange, becomes normal temperature nitrogen at the outlet of the first heat exchanger HEX1, and is discharged into the atmosphere. Considering that the existing low-temperature refrigerator can provide cold energy at about-193 ℃, the low-temperature refrigerator can be used for replacing liquid nitrogen, such as a Stirling refrigerator, a G-M refrigerator, a pulse tube refrigerator and the like.
The saturated gas at the top of the second gas-liquid separator S2 was further cooled to about-210 ℃ to-203 ℃ by the third heat exchanger HEX3, at which time most of the nitrogen and all of the methane were liquefied and subjected to gas-liquid separation in the third gas-liquid separator S3. And the saturated gas at the top of the third gas-liquid separator S3 is crude helium, and the saturated gas is sent to an internal adsorption process section for adsorption purification to obtain 5N high-purity helium meeting the requirement. The high-purity helium gas is reheated by sequentially passing through a third heat exchanger HEX3, a second heat exchanger HEX2 and a first heat exchanger HEX1, and the reheated normal-temperature high-purity helium gas is sent to the helium storage tank 24. Since the saturation temperature of the liquid is lower as the saturation pressure of the liquid is lower, the third heat exchanger HEX3 can be provided with cold energy at-210 ℃ to-203 ℃ by obtaining negative pressure liquid nitrogen by vacuumizing normal pressure liquid nitrogen. Specifically, liquid nitrogen is decompressed by a regulating valve V6 and is firstly sent into a negative pressure liquid nitrogen tank S5, a regulating valve V6 plays a role in regulating liquid level, then the liquid phase enters a third heat exchanger HEX3 to provide cold energy, and vaporized gas enters a negative pressure liquid nitrogen vacuum pump 2312 after being reheated by a heater 2313 and is then discharged. The pressure of the negative pressure liquid nitrogen tank S5 is regulated by a regulator valve V7 provided in the vacuum regulation path so as to be stabilized at a set value. Considering that the existing low-temperature refrigerator can provide cold energy at the temperature of-210 ℃ to-203 ℃, the low-temperature refrigerator can be used for replacing negative pressure liquid nitrogen, such as a Stirling refrigerator, a G-M refrigerator, a pulse tube refrigerator and the like.
The condensate at the bottom of the third gas-liquid separator S3 is decompressed to about 1.2Bar.A through a regulating valve V23 and is sent to a fourth gas-liquid separator S4 for gas-liquid separation, wherein the third regulating valve V23 plays a role in regulating the liquid level of the third gas-liquid separator S3; the condensate at the bottom of the second gas-liquid separator S2 is decompressed to about 1.2Bar.A through an adjusting valve V22 and is sent to a fourth gas-liquid separator S4 for gas-liquid separation, wherein the adjusting valve V22 plays a role in adjusting the liquid level of the second gas-liquid separator S2; the condensate at the bottom of the first gas-liquid separator S1 was reduced in pressure to about 1.2Bar.A by means of the control valve V21 and was also fed to the fourth gas-liquid separator S4 for gas-liquid separation, wherein the control valve V21 served to control the liquid level of the first gas-liquid separator S1. The saturated gas at the top of the fourth gas-liquid separator S4 contains a trace amount of helium, so the saturated gas is regenerated by the first regenerator HEX1 and then is recovered as helium recovery cycle gas; the condensate at the bottom of the fourth gas-liquid separator S4 is sent to the first heat regenerator HEX1 through the regulating valve V24 for heat recovery and temperature recovery to be used as the BOG gas after helium extraction, wherein the regulating valve V24 plays a role in regulating the liquid level of the fourth gas-liquid separator S4.
For the internal adsorption process section, one of the first low temperature adsorber a1 and the second low temperature adsorber a2 is operating normally while the other is regenerating. Taking the first low-temperature adsorber a1 working and the second low-temperature adsorber a2 regenerating as an example, at this time, the first air inlet valve V31 and the first air outlet valve V32 are opened, the first stop valve V35 is closed, the crude helium flow is purified by the first low-temperature adsorber a1, and then sent to the three-stage condensation separation process section for heat regeneration. Meanwhile, the second air inlet valve V33 and the second air outlet valve V34 are closed, the second stop valve V36 is opened, the second low-temperature adsorber A2 is heated, vacuumized and regenerated, and the vacuumized desorption gas contains helium and is also merged into the helium recovery circulation gas for recovery.
The second embodiment is as follows:
referring to fig. 6, compared with the embodiment shown in fig. 5, in this embodiment, the third heat exchanger HEX3 does not directly use a negative pressure liquid nitrogen cold source, but uses high purity helium gas after cryogenic adsorption and condensate in the third gas-liquid separator for heat regeneration, and further, a cold source HEX8 is added after the third heat exchanger HEX3 to ensure that the BOG gas can be provided with cold energy at-210 ℃ to-203 ℃.
Further, in the present embodiment, the cryogenic adsorption mechanism 232 is implemented by a single adsorption tower.
The third concrete implementation mode:
referring to fig. 7, compared to the embodiment shown in fig. 5, in the present embodiment, a two-stage heat exchange manner is adopted, the cold source of the first heat exchanger HEX1 is connected in series with the top gas outlet of the negative pressure liquid nitrogen tank providing the cold source for the third heat exchanger HEX3, further, the negative pressure liquid nitrogen vacuum pump 2312 is disposed at the outlet side of the cold source of the first heat exchanger HEX1, and the connection pipeline between the negative pressure liquid nitrogen vacuum pump 2312 and the first heat exchanger HEX1 is disposed with the regulating valve V28 for regulating the vacuum degree of the negative pressure liquid nitrogen vacuum pump.
The fourth concrete implementation mode:
referring to fig. 8, unlike the three embodiments, the present embodiment is an external adsorption process.
The low-temperature condensation separation mechanism 231 comprises a first heat exchanger HEX1, a first gas-liquid separator, a second heat exchanger HEX2, a second gas-liquid separator S2, a third heat exchanger HEX3, a third gas-liquid separator S3 and a fourth gas-liquid separator S4, the dehydrogenation-treated crude helium purification pipeline is sequentially connected with a BOG inlet and a BOG outlet of a first heat exchanger HEXT, a BOG inlet and a BOG gas outlet of a first gas-liquid separator, a BOG inlet and a BOG outlet of a second heat exchanger HEX2, a BOG inlet and a BOG gas outlet of a second gas-liquid separator S2, a BOG inlet and a BOG outlet of a third heat exchanger HEX3, a BOG inlet and a crude helium gas outlet of a third gas-liquid separator S3, condensate outlets of the first, second and third gas-liquid separators S1, S2 and S3 are respectively communicated to the upper part of a fourth gas-liquid separator S4, and a gas outlet of the fourth gas-liquid separator S4 is used for discharging helium recovery cycle gas and is communicated to the catalytic deoxidation device 25; the crude helium outlet of the third gas-liquid separator S3 is communicated with the cryogenic adsorption mechanism 232.
The low-temperature condensation separation mechanism 231 further comprises a liquid nitrogen storage tank 2311, and the liquid nitrogen storage tank 2311 is sequentially communicated with the second heat exchanger HEX2 and the first heat exchanger HEX1 through pipelines.
The low-temperature condensation separation mechanism 231 further comprises a negative-pressure liquid nitrogen tank S5, a liquid level regulating valve V26, a negative-pressure liquid nitrogen vacuum pump 2312, a heater 2313 and a liquid nitrogen vacuum regulating valve V27, the liquid nitrogen storage tank 2311 is communicated with the negative-pressure liquid nitrogen tank S5 through a pipeline provided with the liquid level regulating valve V26 and used for providing liquid nitrogen for the negative-pressure liquid nitrogen tank, a liquid nitrogen outlet at the bottom of the negative-pressure liquid nitrogen tank S5 is communicated with a liquid nitrogen inlet of a third heat exchanger HEX3, a liquid nitrogen outlet of the third heat exchanger HEX3 is communicated with a liquid nitrogen return opening at the upper part of the negative-pressure liquid nitrogen tank S5, and the negative-pressure liquid nitrogen vacuum pump 2312 is communicated with a vacuum.
The cryogenic adsorption mechanism 232 includes a first cryogenic adsorption unit, a second cryogenic adsorption unit, and a regeneration unit. The first low-temperature adsorption unit comprises a first low-temperature adsorption tower A1, a first air inlet valve V31 and a first air outlet valve V32 which are respectively arranged on the air inlet side and the air outlet side of the first low-temperature adsorption tower A1, the second low-temperature adsorption unit comprises a second low-temperature adsorption tower A2, a second air inlet valve V33 and a second air outlet valve V34 which are respectively arranged on the air inlet side and the air outlet side of the second low-temperature adsorption tower A2, and the first air inlet valve V31 and the second air inlet valve V33 are communicated with a crude helium outlet of a third gas-liquid separator S3; the regeneration unit comprises a first stop valve V35, a second stop valve V36 and a heating and vacuumizing mechanism. The heating and vacuum-pumping mechanism includes a heater 2321 and a desorption vacuum pump 2322. The heater 2321 is connected to the gas outlet side of the first cryoadsorption unit a1 through a first cut-off valve V35, and the heater 2321 is connected to the gas outlet side of the second cryoadsorption unit a2 through a second cut-off valve V36.
In the present embodiment, the crude helium outlet of the third gas-liquid separator S3 is connected to the cryogenic adsorption mechanism 232 after being connected to the third heat exchanger HEX3, the second heat exchanger HEX2, and the first heat exchanger HEX1 in this order; the low-temperature condensation separation mechanism 231 further comprises a low-temperature cold box 2314, a first heat exchanger HEX1, a second heat exchanger HEX2, a HEX3 and a first gas-liquid separator S1, a second gas-liquid separator S2, a third gas-liquid separator S3 and a fourth gas-liquid separator S4 are arranged in the low-temperature cold box 2314; the cryogenic adsorption mechanism 232 further comprises a liquid nitrogen dewar 2323, the first cryogenic adsorption unit further comprises a first cryogenic regenerative heat exchanger HEX4 and a first liquid nitrogen immersed heat exchanger HEX5, and the second cryogenic adsorption unit further comprises a second cryogenic regenerative heat exchanger HEX6 and a second liquid nitrogen immersed heat exchanger HEX 7; the first cryogenic regenerative heat exchanger HEX4, the first liquid nitrogen immersed heat exchanger HEX5, the first low-temperature adsorption tower A1, the second cryogenic regenerative heat exchanger HEX6, the second liquid nitrogen immersed heat exchanger HEX7 and the second low-temperature adsorption tower A2 are arranged in a liquid nitrogen Dewar 2323; a coarse helium outlet of the first heat exchanger HEX1 is sequentially communicated with a coarse helium inlet and a coarse helium outlet of the first cryogenic recuperative heat exchanger HEX4, a first liquid nitrogen immersed heat exchanger HEX5, a first low-temperature adsorption tower A1, a high-purity helium inlet and a high-purity helium outlet of the first cryogenic recuperative heat exchanger HEX4 and a first gas outlet valve V32 through a first gas inlet valve V31; and a second air inlet valve V33 is sequentially communicated with a crude helium inlet and a crude helium outlet of a second cryogenic recuperative heat exchanger HEX6, a second liquid nitrogen submerged heat exchanger HEX7, a second low-temperature adsorption tower A2, a high-purity helium inlet and a high-purity helium outlet of the second cryogenic recuperative heat exchanger HEX6 and a second air outlet valve V34.
The process is briefly described as follows: and crude helium at the top of the third gas-liquid separator S3 is reheated sequentially through a third heat regenerator HEX3, a second heat regenerator HEX2 and a first heat regenerator HEX1 and then sent to an external adsorption process section. For the external adsorption process section, one of the first cryogenic adsorption tower a1 and the second cryogenic adsorption tower a2 is normally operated and the other is regenerated. Taking the first cryoadsorption column a1 working and the second cryoadsorption column a2 regenerating as an example, the first air inlet valve V31 and the first air outlet valve V32 are opened, the first stop valve V35 is closed, the crude helium flow is purified by the first cryoadsorber a1, and then sent to the three-stage condensation separation process section for heat regeneration. Meanwhile, the second air inlet valve V33 and the second air outlet valve V34 are closed, the second stop valve V36 is opened, the second low-temperature adsorber A2 is heated, vacuumized and regenerated, and the vacuumized desorption gas contains helium and is also merged into the helium recovery circulation gas for recovery. Typically, a first cryogenic heat regenerator HEX4 and a second cryogenic heat regenerator HEX6 are more adsorbed in the external adsorption system, and pure helium gas after adsorption and purification is regenerated; the first liquid nitrogen immersed heat exchanger HEX5 and the second liquid nitrogen immersed heat exchanger HEX7 are more adsorbed in the external adsorption process than in the internal adsorption process, so that the temperature of crude helium entering the adsorption tower reaches about-196 ℃; all the low-temperature equipment in the outer adsorber is placed in a liquid nitrogen Dewar, and all the low-temperature equipment in the inner adsorber is placed in a low-temperature vacuum cooling box.
Embodiment 5:
referring to fig. 9, compared to the embodiment shown in fig. 5, in the present embodiment, a two-stage heat exchange manner is adopted, the cold source of the first heat exchanger HEX1 is connected in series with the top gas outlet of the negative pressure liquid nitrogen tank providing the cold source for the third heat exchanger HEX3, further, the negative pressure liquid nitrogen vacuum pump 2312 is disposed at the outlet side of the cold source of the first heat exchanger HEX1, and the connection pipeline between the negative pressure liquid nitrogen vacuum pump 2312 and the first heat exchanger HEX1 is disposed with the regulating valve V28 for regulating the vacuum degree of the negative pressure liquid nitrogen vacuum pump.
Compared with the prior art, the system for co-producing helium by using the LNG production device is organically combined with the existing LNG production device, helium is extracted from one part of BOG gas, and helium enrichment is continuously performed on the other part of BOG gas, so that the economy of helium extraction is improved. Furthermore, the BOG gas has a large Joule-Thomson coefficient, rapid cooling can be achieved through isothermal compression refrigeration, the process is simple and efficient, and the adaptability is strong. After extracting helium in the BOG gas, returning the helium-removed BOG gas to the existing device again, wherein the existing device does not need to be changed. The non-condensable gas helium in the BOG gas of the existing LNG production device is extracted, so that the power consumption of the BOG compressor is reduced, and the economy of the existing LNG production device is improved.
The above are merely examples of the present application and are not intended to limit the present application. Various modifications and changes may occur to those skilled in the art. Any modification, equivalent replacement, improvement, etc. made within the spirit and principle of the present application should be included in the scope of the claims of the present application.

Claims (11)

1. A system for co-producing helium by using an LNG production device, wherein the LNG production device comprises a natural gas liquefaction mechanism, an LNG storage tank and a first BOG compressor, the first BOG compressor is used for compressing BOG gas from the LNG storage tank, and part of the BOG gas compressed by the first BOG compressor is converged into the natural gas liquefaction mechanism for re-liquefaction; the system for co-producing helium by using the LNG production device is characterized by comprising: raw material gas compressor, dehydrogenation and drying mechanism, low-temperature separation and cryogenic adsorption mechanism, helium storage tank and catalytic deoxidation device, raw material gas compressor, dehydrogenation and CO removal2Dehydration drying mechanism and low temperature separation and cryrogenic adsorption apparatus construct and set gradually on helium coproduction route, and helium storage tank and catalysis deoxidation device are connected to low temperature separation and cryrogenic adsorption apparatus respectively and are constructed, the feed gas compressor is used for the right warp another part BOG gas further compression after the compression of first BOG compressor, dehydrogenation and take off CO2The dehydration and drying mechanism is used for dehydrogenating and removing CO from BOG gas further compressed by the feed gas compressor2And drying, wherein the low-temperature separation and cryogenic adsorption mechanism is used for cooling, condensing and adsorbing the BOG gas subjected to dehydrogenation treatment to obtain high-purity helium and the BOG gas subjected to helium extraction, the helium storage tank is used for storing the high-purity helium, and the catalytic deoxidation device is used for deoxidizing the BOG gas subjected to helium extraction.
2. The system for co-producing helium gas using an LNG production apparatus according to claim 1, wherein the cryogenic separation and cryogenic adsorption means includes a cryogenic condensation separation means and a cryogenic adsorption means, the cryogenic condensation separation means includes a first heat exchanger, a first gas-liquid separator, a second heat exchanger, a second gas-liquid separator, a third heat exchanger, a third gas-liquid separator, and a fourth gas-liquid separator, the crude helium purification pipeline connects the BOG inlet and the BOG outlet of the first heat exchanger, the BOG inlet and the BOG gas outlet of the first gas-liquid separator, the BOG inlet and the BOG outlet of the second heat exchanger, the BOG inlet and the BOG outlet of the second gas-liquid separator, the BOG inlet and the BOG outlet of the third heat exchanger, the BOG inlet and the crude helium gas outlet of the third gas-liquid separator, and the condensate outlets of the first gas-liquid separator, the second gas-liquid separator, and the third gas-liquid separator are respectively connected to an upper portion of the fourth gas-liquid separator, a gas outlet of the fourth gas-liquid separator is used for discharging helium recovery circulating gas, and a condensate outlet is communicated to the catalytic deoxidation device; and a crude helium outlet of the third gas-liquid separator is communicated with the cryogenic adsorption mechanism.
3. The system for co-producing helium gas using an LNG production plant according to claim 1, wherein the cryogenic condensation separation mechanism further comprises a liquid nitrogen storage tank, and the liquid nitrogen storage tank is sequentially communicated with the second heat exchanger and the first heat exchanger through a pipeline.
4. The system for co-producing helium gas by using an LNG production device according to claim 3, wherein the cryogenic condensation separation mechanism further comprises a negative pressure liquid nitrogen tank, a liquid level regulating valve, a negative pressure liquid nitrogen vacuum pump and a liquid nitrogen vacuum regulating valve, the liquid nitrogen storage tank is communicated with the negative pressure liquid nitrogen tank through a pipeline provided with the liquid level regulating valve and is used for providing liquid nitrogen for the negative pressure liquid nitrogen tank, a liquid nitrogen outlet at the bottom of the negative pressure liquid nitrogen tank is communicated with a liquid nitrogen inlet of the third heat exchanger, a liquid nitrogen outlet of the third heat exchanger is communicated with a liquid nitrogen return port at the upper part of the negative pressure liquid nitrogen tank, and the negative pressure liquid nitrogen vacuum pump is communicated with a vacuum pumping port at the top end.
5. The system for co-producing helium gas using an LNG production plant according to claim 2, wherein the cryogenic adsorption mechanism comprises a first cryogenic adsorption unit, a second cryogenic adsorption unit and a regeneration unit, the first cryogenic adsorption unit comprises a first cryogenic adsorption tower and a first inlet valve and a first outlet valve respectively disposed on an inlet side and an outlet side of the first cryogenic adsorption tower, the second cryogenic adsorption unit comprises a second cryogenic adsorption tower and a second inlet valve and a second outlet valve respectively disposed on an inlet side and an outlet side of the second cryogenic adsorption tower, and the first inlet valve and the second inlet valve are both communicated with the crude helium outlet of the third gas-liquid separator; the regeneration unit comprises a first stop valve, a second stop valve and a heating and vacuumizing mechanism, the heating and vacuumizing mechanism is connected to the gas outlet side of the first low-temperature adsorption unit through the first stop valve, and the heating and vacuumizing mechanism is connected to the gas outlet side of the second low-temperature adsorption unit through the second stop valve.
6. The system for co-producing helium with an LNG production plant according to claim 5, wherein the cryogenic separation and cryogenic adsorption mechanism further comprises a cryogenic cooling box, the first heat exchanger, the second heat exchanger, the third heat exchanger, the first gas-liquid separator, the second gas-liquid separator, the third gas-liquid separator, and the fourth gas-liquid separator, and the first adsorption unit and the second adsorption unit are disposed in the cryogenic cooling box.
7. The system for co-producing helium by using an LNG production device according to claim 6, wherein a pipeline where the first gas outlet valve is located and a pipeline where the second gas outlet valve is located are connected in parallel and then sequentially communicate with the third heat exchanger, the second heat exchanger and the first heat exchanger, and the third heat exchanger, the second heat exchanger and the first heat exchanger are used for sequentially returning the temperature of the high-purity helium discharged from the first cryoadsorption tower and the second cryoadsorption tower.
8. The system for co-producing helium gas using an LNG production plant according to claim 5, wherein the crude helium gas outlet of the third gas-liquid separator is communicated with the cryogenic adsorption mechanism after being communicated with the third heat exchanger, the second heat exchanger and the first heat exchanger in sequence; the low-temperature condensation separation mechanism further comprises a low-temperature cold box, and the first heat exchanger, the second heat exchanger, the third heat exchanger, the first gas-liquid separator, the second gas-liquid separator, the third gas-liquid separator and the fourth gas-liquid separator are arranged in the low-temperature cold box; the cryogenic adsorption mechanism further comprises a liquid nitrogen Dewar, the first cryogenic adsorption unit further comprises a first cryogenic regenerative heat exchanger and a first liquid nitrogen immersed heat exchanger, and the second cryogenic adsorption unit further comprises a second cryogenic regenerative heat exchanger and a second liquid nitrogen immersed heat exchanger; the first cryogenic regenerative heat exchanger, the first liquid nitrogen immersed heat exchanger, the first low-temperature adsorption tower, the second cryogenic regenerative heat exchanger, the second liquid nitrogen immersed heat exchanger and the second low-temperature adsorption tower are arranged in the liquid nitrogen dewar; the coarse helium outlet of the first heat exchanger is sequentially communicated with a coarse helium inlet and a coarse helium outlet of the first cryogenic regenerative heat exchanger, the first liquid nitrogen immersed heat exchanger, the first low-temperature adsorption tower, the high-purity helium inlet and the high-purity helium outlet of the first cryogenic regenerative heat exchanger and the first gas outlet valve through the first gas inlet valve; and the second air inlet valve is sequentially communicated with a coarse helium inlet and a coarse helium outlet of the second cryogenic regenerative heat exchanger, the second liquid nitrogen immersed heat exchanger, the second low-temperature adsorption tower, a high-purity helium inlet and a high-purity helium outlet of the second cryogenic regenerative heat exchanger, and the second air outlet valve.
9. The system for co-producing helium with an LNG production plant according to claim 1, further comprising a fuel gas line connected to an output of the first BOG compressor, an output of the catalytic deoxygenator device being connected to the fuel gas line and a natural gas liquefaction plant.
10. The system for co-producing helium gas using an LNG production plant according to claim 9, wherein the helium gas purification apparatus further comprises a helium-extracted gas compressor, the helium-extracted gas compressor is connected to the cryogenic separation and cryogenic adsorption mechanism and the catalytic deoxygenation apparatus, the helium-extracted gas compressor is configured to pressurize the helium-extracted BOG gas, and the catalytic deoxygenation apparatus is configured to perform oxygen removal on the pressurized helium-extracted BOG gas.
11. The system for co-producing helium with an LNG production plant according to claim 1, further comprising a second BOG compressor connecting the first BOG compressor and a natural gas liquefaction train.
CN202021219265.8U 2020-06-28 2020-06-28 System for utilize LNG apparatus for producing coproduction helium Active CN212538459U (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
CN202021219265.8U CN212538459U (en) 2020-06-28 2020-06-28 System for utilize LNG apparatus for producing coproduction helium

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
CN202021219265.8U CN212538459U (en) 2020-06-28 2020-06-28 System for utilize LNG apparatus for producing coproduction helium

Publications (1)

Publication Number Publication Date
CN212538459U true CN212538459U (en) 2021-02-12

Family

ID=74547008

Family Applications (1)

Application Number Title Priority Date Filing Date
CN202021219265.8U Active CN212538459U (en) 2020-06-28 2020-06-28 System for utilize LNG apparatus for producing coproduction helium

Country Status (1)

Country Link
CN (1) CN212538459U (en)

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN111692837A (en) * 2020-06-28 2020-09-22 北京中科富海低温科技有限公司 System for utilize LNG apparatus for producing coproduction helium
CN113154409A (en) * 2021-03-03 2021-07-23 北京中科富海低温科技有限公司 System and method for extracting helium from BOG gas and utilizing energy
CN113686098A (en) * 2021-09-27 2021-11-23 西南石油大学 Natural gas liquefaction and helium recovery method

Cited By (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN111692837A (en) * 2020-06-28 2020-09-22 北京中科富海低温科技有限公司 System for utilize LNG apparatus for producing coproduction helium
CN113154409A (en) * 2021-03-03 2021-07-23 北京中科富海低温科技有限公司 System and method for extracting helium from BOG gas and utilizing energy
CN113154409B (en) * 2021-03-03 2022-02-22 北京中科富海低温科技有限公司 System and method for extracting helium from BOG gas and utilizing energy
CN113686098A (en) * 2021-09-27 2021-11-23 西南石油大学 Natural gas liquefaction and helium recovery method

Similar Documents

Publication Publication Date Title
CN111692837A (en) System for utilize LNG apparatus for producing coproduction helium
CN212538459U (en) System for utilize LNG apparatus for producing coproduction helium
CN110455038B (en) Helium extraction unit, helium extraction device and system for co-producing helium
CN112361712A (en) Hydrogen liquefaction equipment adopting helium refrigeration cycle system
CN109631494B (en) Helium production system and production method
CN112393527A (en) LNG flash steam recovery method and system
CN111533095A (en) Equipment and process for purifying helium from BOG gas
CN111964354B (en) Method for separating and purifying helium gas by removing methane and nitrogen
CN108469150B (en) Hydrogen liquefying device
US3469410A (en) Process and apparatus for the removal of traces of impurities from carbon dioxide
CN101108724A (en) Manufacture method of extracting pure tritium from raw material of light water (heavy water) containing tritium
CN111086974A (en) System and method for separating and purifying hydrogen and helium from BOG
CN115888386A (en) Process for extracting helium from high-nitrogen BOG gas
CN113144821A (en) Multi-technology integrated separation process for producing high-purity helium gas from helium-rich natural gas liquefaction tail gas
CN114314534B (en) Natural gas helium extraction process
CN109442868B (en) Method for removing oxygen and nitrogen, separating and purifying neon and helium
CN113862051B (en) Double refrigeration cycle methane washing synthetic gas cryogenic separation device and separation method
CN214095167U (en) Hydrogen liquefaction equipment adopting helium refrigeration cycle system
CN114777418B (en) System for extracting helium from natural gas BOG by condensation method
US20210364228A1 (en) Installation and method for producing liquefied methane
CN217148577U (en) System for extracting high-purity helium from low-helium BOG
CN103629894A (en) Air separation method of single-stage distillation device
CN112919437B (en) Refining method and system for crude helium with high hydrogen content
CN109734064B (en) Helium production system and production method
CN212842469U (en) Single-tower cryogenic rectification argon recovery system with argon circulation and hydrogen circulation

Legal Events

Date Code Title Description
GR01 Patent grant
GR01 Patent grant