CN106369935A - Air separation system and method utilizing pressure energy of high-pressure natural gas pipeline network - Google Patents

Air separation system and method utilizing pressure energy of high-pressure natural gas pipeline network Download PDF

Info

Publication number
CN106369935A
CN106369935A CN201610957129.0A CN201610957129A CN106369935A CN 106369935 A CN106369935 A CN 106369935A CN 201610957129 A CN201610957129 A CN 201610957129A CN 106369935 A CN106369935 A CN 106369935A
Authority
CN
China
Prior art keywords
pressure
natural gas
air
temperature
energy
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Granted
Application number
CN201610957129.0A
Other languages
Chinese (zh)
Other versions
CN106369935B (en
Inventor
马国光
张晨
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.)
Southwest Petroleum University
Original Assignee
Southwest Petroleum University
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 Southwest Petroleum University filed Critical Southwest Petroleum University
Priority to CN201610957129.0A priority Critical patent/CN106369935B/en
Publication of CN106369935A publication Critical patent/CN106369935A/en
Application granted granted Critical
Publication of CN106369935B publication Critical patent/CN106369935B/en
Expired - Fee Related legal-status Critical Current
Anticipated expiration legal-status Critical

Links

Classifications

    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04151—Purification and (pre-)cooling of the feed air; recuperative heat-exchange with product streams
    • F25J3/04187—Cooling of the purified feed air by recuperative heat-exchange; Heat-exchange with product streams
    • F25J3/04218—Parallel arrangement of the main heat exchange line in cores having different functions, e.g. in low pressure and high pressure cores
    • F25J3/04224—Cores associated with a liquefaction or refrigeration cycle
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04012—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of warm gaseous streams; details of intake or interstage cooling
    • F25J3/04018—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of warm gaseous streams; details of intake or interstage cooling of main feed air
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04012—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of warm gaseous streams; details of intake or interstage cooling
    • F25J3/04024—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of warm gaseous streams; details of intake or interstage cooling of purified feed air, so-called boosted air
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04109—Arrangements of compressors and /or their drivers
    • F25J3/04115—Arrangements of compressors and /or their drivers characterised by the type of prime driver, e.g. hot gas expander
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04151—Purification and (pre-)cooling of the feed air; recuperative heat-exchange with product streams
    • F25J3/04163—Hot end purification of the feed air
    • F25J3/04169—Hot end purification of the feed air by adsorption of the impurities
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04254—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using the cold stored in external cryogenic fluids
    • F25J3/0426—The cryogenic component does not participate in the fractionation
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04278—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using external refrigeration units, e.g. closed mechanical or regenerative refrigeration units
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04284—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams
    • F25J3/0429—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams of feed air, e.g. used as waste or product air or expanded into an auxiliary column
    • F25J3/04296—Claude expansion, i.e. expanded into the main or high pressure column
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04406—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system
    • F25J3/04412—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system in a classical double column flowsheet, i.e. with thermal coupling by a main reboiler-condenser in the bottom of low pressure respectively top of high pressure column
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2210/00—Processes characterised by the type or other details of the feed stream
    • F25J2210/60—Natural gas or synthetic natural gas [SNG]
    • 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
    • F25J2260/10—Integration in a gas transmission system at a pressure reduction, e.g. "let down" station
    • 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
    • F25J2270/14—External refrigeration with work-producing gas expansion loop
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/14—External refrigeration with work-producing gas expansion loop
    • F25J2270/16—External refrigeration with work-producing gas expansion loop with mutliple gas expansion loops of the same refrigerant
    • 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
    • F25J2270/42—Quasi-closed internal or closed external nitrogen refrigeration cycle

Landscapes

  • Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Mechanical Engineering (AREA)
  • Thermal Sciences (AREA)
  • General Engineering & Computer Science (AREA)
  • Separation By Low-Temperature Treatments (AREA)

Abstract

The invention discloses an air separation system and a method utilizing pressure energy of a high-pressure natural gas pipeline network. The air separation system comprises a natural gas pressure energy recovery system, an air separation system and a refrigerant circulation loop, wherein the natural gas pressure energy recovery system comprises a natural gas purification device, a high-pressure natural gas expansion machine, a high-pressure refrigerant compressor, a heat exchanger A, a refrigerant expansion machine, a medium-pressure refrigerant compressor, a medium-pressure natural gas expansion machine and a heat exchanger B, and the air separation system comprises a blower, an air filter, an air compressor, an air compressor aftercooler, an air precooler, a molecular sieve adsorption device, an electric heater, a main heat exchanger, an air expansion machine, a rectifying tower, an oxygen storage device and a nitrogen storage device. According to the air separation system, high pressure energy of high-pressure natural gas is converted into cold energy for air separation, the expansion machines and the heat exchangers are used as intermediate equipment for energy conversion, the pressure is reduced, and additionally, the pressure energy is fully refrigerated and used, so that the problems of high energy consumption and low pressure energy utilization of an air separation technique are solved.

Description

A kind of air-seperation system of utilization high-pressure natural gas pipe network pressure energy and method
Technical field
The present invention relates to the applied technical field of high-pressure natural gas pressure reduction refrigeration, more particularly, to one kind utilizes high-pressure natural gas The Cryognic air separation system of pipe network pressure energy refrigeration and method.
Background technology
The most conveying carrying out distance with the high pressure of more than 10mpa of gas distributing system, and pipeline network of fuel gas in city design pressure Power, in 0.2～0.4mpa, need to be delivered to downstream pipe network after carrying out pressure regulation, in pressure regulation, typically have one-level pressure regulation and second voltage regulation Two ways.The middle pressure standard that supertension or high-pressure natural gas are directly depressurized to 0.2mpa～0.4mpa (gauge pressure) is adjusted for one-level Pressure；First hyperpressure or high-pressure natural gas are depressurized to 1.6mpa～2.0mpa (gauge pressure), are then depressurized to 0.2mpa again The middle pressure standard of～0.4mpa (gauge pressure) is second voltage regulation.Pressure regulation process contains immense pressure energy.At present in urban gate station and When point defeated station adopts choke valve pressure regulation, not only produce huge noise, adjoint cooling is likely to result in downstream line low temperature frozen block, The huge pressure drop that above all this pressure regulation process produces is not recycled, and causes energy waste.
An important use reclaiming high-pressure natural gas ductwork pressure is to can be used for freezing, and can be efficiently applied to air and separate Technical field, it is possible to reduce produced for maintaining low temperature environment and producing liquid by the mechanical refrigeration of driven by power in space division system A large amount of cold energy needed for product.Reduce the refrigeration cost in air-separating technology, to reducing electrical energy demands amount, promote air to separate Industry development is significant.Oxygen and nitrogen are common air separation products, and they are not only the important life of chemical industry Produce raw material, also have a very wide range of applications in fields such as medical treatment, electronics, metallurgy, aviation, environmental protection simultaneously.With World Science Technology and rapid development of economy, all trades and professions increase sharply to the demand of oxygen and nitrogen, and consumption also gets more and more, and promote The development of air separation technology.Existing air separation technology is mainly used for producing the process gas products such as liquid oxygen, liquid nitrogen, though So most common voltage contraction cold air isolation technics can obtain various industry, pharmaceutical sectors and the oxygen required for aircraft industry, Nitrogen etc., but due to needing the low temperature creating and maintaining 150 DEG C～191 DEG C, huge to electrical energy demands amount, equipment energy consumption is about Duty is divided into this 70～80%.Thus exploitation energy-conservation, efficient air separation technology have become Air separation industry developing direction.
At present, the pressure energy of natural gas of recovery has been used for generating, freezer, cooling water air conditioner, ice making, ice rink, air divide The field such as separate with purification, dry ice production, rubber deep cooling crush and natural gas lighter hydrocarbons from, Component seperation.More ripe high pressure The recovery of natural gas pipe network pressure energy is mainly used for freezing and generates electricity, but it is low all to there is efficiency, and equipment investment is big, and overbottom pressure cannot The shortcoming being utilized effectively.The technical scheme using high-pressure natural gas pressure energy refrigeration having been disclosed in prior art has A lot, the Chinese patent of Application No. 200810026979.4 proposes one kind using high-pressure natural gas directly by unpowered system The technological process of cold decompressional expansion refrigeration, can obtain the low temperature between 40 DEG C～100 DEG C.But due in this patent not Reclaim the mechanical energy in expansion process, merely with expanding the cold energy producing, lead to pressure energy utilization rate relatively low, less than 50%, and Less than 100 DEG C of low temperature cannot be obtained, be not suitable for air and separate.The Chinese patent of Application No. 201210128345.6 and The Chinese patent of Application No. 200510037532.3 proposes using high-pressure natural gas pressure energy swell refrigeration liquefied natural gas Technological process.100 DEG C of cryogenic natural gas can be obtained using pre-cooling and swell refrigeration, but do not consider that big temperature drop is easily made Become gas pipeline frozen block, for ensureing the normal investment producing and need to increasing natural gas processing, operation cost is higher.In addition, publication number Patent for cn101245956a, cn101852529b, cn102563958b, cn2791144y, us5137558 also discloses that phase The technical scheme of ductwork pressure should be recycled.But only disclose in technique scheme using recovery natural gas pipe network pressure energy Generate electricity or freeze, the development people that current natural gas pipe network pressure energy is used for the detached technology of air is in starting stage, publication number A kind of air-seperation system of utilization natural gas pressure difference generating cold energy of patent for cn103968640a, is related to natural gas pressure difference Generating cold energy applied technical field, this patent is that high-pressure natural gas pressure regulation generating is combined with air-separating plant, fully profit The cold energy being produced with natural gas pressure regulating power generation process, but pressure energy is relatively low by turbine pipe organic efficiency, and air separates and is only Its attached technique, and be lost in refrigerant circulation and increase year by year, thus this technology exist air separate yield poorly, equipment investment is big, It is only applicable to the shortcoming that the high natural valve station of the big pressure of flow is the scope of application relatively limitation.
Therefore, find one kind to recycle pressure energy of natural gas and not cause frozen block to pipe network, and hardware can be saved and throw The processing system being applied to middle-size and small-size separating station of money, makes great sense for realizing green production.
Content of the invention
For the problems referred to above, the purpose of the present invention is for overcoming the deficiencies in the prior art, providing a kind of natural using high pressure The air-seperation system of gas pipe network pressure energy.This system combines pressure energy of natural gas recovery and separates two kinds of technology with air, by height The higher pressure energy of pressure natural gas is converted into the detached cold energy of air, by the use of decompressor and heat exchanger as in energy conversion Between equipment, not only meet the requirement of pressure drop, and natural gas pipe network pressure energy fully can be freezed and make full use of, and solve The low problem of capacity usage ratio in existing air separation technology high energy consumption and natural gas pipe network pressure energy recycling.
For reaching this purpose, the present invention is achieved through the following technical solutions:
A kind of air-seperation system of utilization high-pressure natural gas pipe network pressure energy, including pressure energy of natural gas recovery system, Air-seperation system, connection pressure energy of natural gas recovery system are with the refrigerant circulation circuit of air-seperation system, this refrigerant circulation Loop is used for the air-separating plant that the huge cold energy of gas distributing system pressure reduction generation is changed to invention, provides air to divide Cold energy needed for from system, and the energy discharging when being cooled down by absorption air ensures that the low pressure natural gas temperature of output will not mistake Low；
Described pressure energy of natural gas recovery system includes purifying device for natural gas, high-pressure natural gas decompressor, high pressure refrigerant Compressor, heat exchanger a, coolant decompressor, middle pressure cold medium compressor, middle pressure Natural gas expander, heat exchanger b；Air segregative line System includes aerator, air filter, air compressor machine, cooler behind air compressor, air precooler, molecular sieve adsorption device, electricity add Hot device, main heat exchanger, air expander, rectifying column, oxygen-storing device, nitrogen storage device；
Purifying device for natural gas connects high-pressure natural gas decompressor, is then connected into heat exchanger a, heat exchanger a connects cold respectively Matchmaker's decompressor and middle pressure Natural gas expander, middle pressure Natural gas expander connects heat exchanger b, and heat exchanger b outlet connects downstream sky So gas pipe network, is simultaneously provided with branch road and connects high pressure refrigerant compressor, high pressure refrigerant compressor accesses heat exchanger a；Coolant decompressor Connect main heat exchanger, heat exchanger has three outlet lines, pressure cold medium compressor, electric heater, air expander in connecting respectively, Middle pressure cold medium compressor connects heat exchanger b, and electric heater is sequentially connected molecular sieve adsorption device and air precooler, air expansion Machine is connected to rectifying column bottom；Aerator is sequentially connected air filter, air compressor machine, cooler behind air compressor, is then connected into sky Gas precooler；Rectifying column upper end outlet connects main heat exchanger, and lower end outlet connects oxygen-storing device and nitrogen storage dress respectively Put.
A kind of air-seperation system of utilization high-pressure natural gas pipe network pressure energy, including following operating procedure: first, in height During pressure natural gas pressure regulating, the pressure energy of high-pressure natural gas is converted to by mechanical work and cold energy by decompressor, recycles cold Matchmaker as medium, reclaims the mechanical energy producing and cold energy, on the one hand utilizes high-pressure natural gas to expand the mechanical work producing by coolant Compression, so as to become high-pressure refrigeration working medium, on the other hand, by the optimization design of heat-exchange network, is expanded using high-pressure natural gas The cold energy producing, to cool down the high pressure refrigerant after compression, improves the intake air temperature that high-pressure natural gas enter decompressor simultaneously, increases High-pressure natural gas expand the mechanical work producing, and then using hot insulated line, the high pressure refrigerant after cooling down are delivered to air separation dress Put region, recycle the cryogenic cold energy that high pressure refrigerant expander produces；Meanwhile, high pressure refrigerant expands the mechanical work producing and uses Tentatively it is pressurized after main heat exchanger heat exchange in coolant；Then the coolant after preliminary supercharging is delivered to by heat exchanger by hot insulated line Reclaim high-pressure natural gas and expand the cold energy producing, form refrigerant circulation.
A kind of air-seperation system of utilization high-pressure natural gas pipe network pressure energy, comprises the following steps.
A. high-pressure natural gas pressure energy reclaims:
High-pressure natural gas pipe network is delivered to the high-pressure natural gas of voltage regulating station, point defeated station, pressure 1.5mpa (absolute pressure, Pressure appears below is absolute pressure) more than.After high-pressure natural gas flow through purifying device for natural gas preliminary treatment, enter high Pressure Natural gas expander expands and is depressurized to 1～7mpa, and the mechanical work of high-pressure natural gas decompressor output is used for middle pressure coolant compression The driving of machine, obtains the middle pressure natural gas that temperature reduces simultaneously, and by adjusting the outlet pressure of high-pressure natural gas decompressor, protects Demonstrate,prove the water dew point that its temperature is higher than natural gas.Middle pressure natural gas after high-pressure natural gas expander passes through heat exchanger a With the high pressure refrigerant heat exchange after high pressure refrigerant compressor compresses, after obtaining heat, temperature is increased to 15 DEG C～100 DEG C；Temperature By middle pressure Natural gas expander, after expansion, reduced pressure, to 0.4～3mpa, obtains temperature fall to middle pressure natural gas after degree rising Low low pressure natural gas, the mechanical work of acquisition is used for driving high pressure refrigerant compressor, and ensures that its temperature is higher than its water dew point.Low Warm low pressure natural gas are by heat exchanger b with the middle pressure coolant heat exchange after middle pressure cold medium compressor compression, the low pressure after heat exchange Natural gas temperature is increased to more than 0 DEG C and is delivered to gas distributing system.
B. it is used for connecting the refrigerant circulation with air-seperation system for the natural gas pressure difference refrigeration system:
Low temperature refrigerant flows through what the main heat exchanger of air-seperation system distributed with the pressure-air after pre-cooling and rectifying column Low temperature waste gas heat exchange, after heat exchange, refrigerant temperature is increased to 0～20 DEG C.During low pressure refrigerant after temperature rising flows into, pressure coolant compresses Machine, is pressurized to 2～3mpa, and temperature is increased to 90～130 DEG C, becomes middle pressure coolant, and its pressure and temperature are subject to high-pressure natural gas swollen The output work size impact of swollen machine.Middle pressure coolant presses Natural gas expander in being delivered to heat exchanger b and passed through by hot insulated line Low-pressure low-temperature heat exchange gas after expansion, middle pressure refrigerant temperature is reduced to 0 DEG C～30 DEG C, is then passed through high pressure refrigerant compressor It is pressurized to 4～6mpa, becomes high pressure refrigerant, its pressure and temperature are affected by the output work size of middle pressure Natural gas expander.High By heat exchanger a with the middle pressure heat exchange gas after high-pressure natural gas expander, temperature is down to 30～0 to pressure coolant DEG C, then coolant decompressor is delivered to by hot insulated line, the refrigerant temperature after expansion is down to 120～140 DEG C.Enter to become owner of Heat exchanger provides cold energy for air-separating plant, and middle pressure natural gas expands the mechanical work obtaining and is used for driving air-separating plant Air compressor, forms refrigerant circulation.
C. air separates:
Air passes through air line air inlet filter, enters air compressor unit, be compressed to 1 after removing solid impurity ～2.5mpa.Temperature is increased to 110～200 DEG C, and the air after compression enters cooler behind air compressor and is cooled to 90～180 DEG C. The High Temperature High Pressure air air inlet precooler obtaining, changes with the Cryogenic air after main heat exchanger heat exchange in air precooler Heat, temperature is down to 10～20 DEG C, and the air after pre-cooling enters molecular sieve adsorption device, enters main heat exchange after removing water and impurity Device, carries out heat exchange with the low temperature waste gas that low temperature refrigerant and rectifying tower top distribute, and temperature is down to 120～140 DEG C, warm Pipelined to air expander, pressure 0.3～1mpa after expansion, temperature is down to the saturation temperature under this pressure, from rectifying column Bottom enters, and low-temp low-pressure air repeatedly condenses in rectifying column and evaporates, and the more oxygen-enriched liquid air of composition containing liquid oxygen is collected in Rectifying column Shang Ta and lower tower bottom, nitrogen is then collected in Shang Ta and lower top of tower.(oxygen-containing 99.80%) is from rectifying column for high-purity liquid oxygen Upper tower bottom outlet flows out warm pipeline to oxygen-storing device；(nitrogenous 99.99%) is cold in lower top of tower for High Purity Nitrogen Be condensed into liquid nitrogen in solidifying vaporizer, after extraction, be divided into two strands, one as backflow from upper top of tower dirty for upper tower rise Steam provides cold, to obtain the higher liquid form product of purity；Another strand imports liquid nitrogen storage device and is stored；From rectifying column Tower top shunts one low temperature waste gas, is delivered to main heat exchanger, after the air after pre- cold cleaning and coolant heat exchange, is divided into two strand one Part, through pressure regulator valve pressure regulation to normal pressure, air inlet precooler, provides cold, outer row for air, another strand of low temperature waste gas are through pipe Road is delivered to electric heater, and regenerating for molecular sieve adsorption device provides source of the gas, drains into air outward afterwards；The richness that rectifier bottoms are assembled (about 180 DEG C of oxygen-containing about 38%), after throttling, about 190 DEG C enter rectifiers backflow to oxygen liquid air, on the one hand increase liquid air Evaporation cold flow number of times in rectifying column, on the other hand provides cold for the steam that upper tower rises, so that it is higher to obtain purity Liquid form product.
Enter high-pressure natural gas recovery system gas pressure between 1.6～10mpa, using the side of double expansion heat exchange Formula, including high-pressure natural gas decompressor and middle pressure Natural gas expander, through two-stage blood pressure lowering, pressure is down to downstream sky to high-pressure natural gas So gas pipe network discharge pressure.And followed by adjusting high-pressure natural gas decompressor and middle pressure Natural gas expander outlet pressure and coolant The flow-control gas outlet temperature of ring is it is ensured that it is higher than gas water dew point.
High-pressure natural gas decompressor, middle pressure Natural gas expander, air expander and coolant decompressor are turbine expansion.
Pressure cold medium compressor, high pressure refrigerant compressor two-stage supercharging in coolant warp in refrigerant circulation.Middle pressure cold medium compressor Driven by the mechanical energy that high-pressure natural gas decompressor produces, the machinery that high pressure refrigerant compressor is produced by middle pressure Natural gas expander Can drive.
Coolant all is used for heating expanded machine swollen through the heat energy that compressor compression supercharging produces by heat exchanger a, heat exchanger b Natural gas after swollen.And high-pressure natural gas expand the coolant that the cold energy producing all heats up after heat exchanger is used for cooling compression.
The cold energy temperature that refrigerant circulation provides in air-seperation system, on the one hand can be another by adjusting refrigerant circulation Aspect can change the amount of rectifying tower top low temperature waste gas shunting, reduce refrigerant circulation, increase rectifying tower top shunting low temperature waste gas Amount, increase coolant two-stage compression compression ratio all can reduce cryogenic temperature.Contrary then cryogenic temperature can be improved.
High-pressure natural gas pressure regulation and pressure energy retracting device are connected it is ensured that two with air-separating plant by kind of refrigeration cycle The personal distance in region.
The present invention has the advantage that with respect to prior art
(1) a kind of air-seperation system of utilization high-pressure natural gas pipe network pressure energy proposed by the present invention, is based on energy Pressure energy is converted to cold energy and mechanical work using decompressor by transfer principle, by refrigerant circulation, reclaims high-pressure natural gas simultaneously Expand the cold energy producing and mechanical energy, and the cryogenic cold energy that can produce less than 120 DEG C is used for air separation, is that air divides From providing cheap low-temperature receiver, reduce the energy consumption of space division product；
(2) present invention passes through Optimization of Heat Exchanger Networks, realizes high-pressure natural gas are expanded with the cold energy producing and coolant compression is produced The cascade utilization of raw heat energy, on the one hand, the heat energy reclaiming coolant compression generation is used for carrying entering of high pressure Natural gas expander Mouth temperature and the temperature entering downstream gas distributing system, increase the mechanical work of natural gas expansion process generation it is ensured that entering downstream The natural gas temperature of gas distributing system is higher than its water dew point；On the other hand high-pressure natural gas are utilized to expand the cold energy cooling producing cold Matchmaker, can save the investment of cooling device and operating cost after coolant compression during refrigerant circulation.Reduce the fortune of refrigerant circulation Row cost；
(3) present invention by coolant as energy transmission tie, by natural gas pressure regulating process and pressure energy removal process Equipment with air separation equipment separately, and ensures safe distance, it is to avoid two links are in the same area, and security against fire causing etc. The hidden danger of aspect, is conducive to safe operation；
(4) present invention passes through to reclaim high-pressure natural gas pipe network pressure energy refrigeration for less than 120 DEG C of air separation offer Cold energy, is not required to consume outside energy, energy consumption for cooling is very low.And it is by systematically optimization design, swollen using high-pressure natural gas Swollen refrigerating part has relatively strong operation flexibility, in the fluctuation of gas flow amount and the fluctuation of air separation produce load, all can protect Hold normal operating.This process is not required to extraneous offer cold and heat source, and ensures that the outer defeated temperature of natural gas is higher than water dew point, it is to avoid ice Stifled；
(5) employ nitrogen as the working medium for refrigerant circulation, nitrogen is the product of this system, can reduce the same of production cost When, heat transfer process air can be avoided to contact with natural gas and security incident occurs.
Brief description
Accompanying drawing 1 is the structural representation of the present invention.
In figure 1, air filter, 2, air compressor machine, 3, air precooler, 4, molecular sieve adsorption device, 5, electric heater, 6, Main heat exchanger, 7, rectifying column, 8, air expander, 9, middle pressure cold medium compressor, 10, heat exchanger b, 11, high pressure refrigerant compressor, 12nd, heat exchanger a, 13, coolant decompressor, 14, oxygen-storing device, 15, nitrogen storage device, 16, purifying device for natural gas, 17th, high-pressure natural gas decompressor, 18, middle pressure Natural gas expander, 19, choke valve a, 20, choke valve b, 21, choke valve c, 22, Cooler behind air compressor, 23, aerator.
Specific embodiment
Below in conjunction with the accompanying drawings, technical scheme is described specifically further:
A kind of air-seperation system of utilization high-pressure natural gas pipe network pressure energy that the present invention provides, mainly by air filtration Device 1, air compressor machine 2, air precooler 3, molecular sieve adsorption device 4, electric heater 5, main heat exchanger 6, rectifying column 7, air expansion Machine 8, middle pressure cold medium compressor 9, heat exchanger b10, high pressure refrigerant compressor 11, heat exchanger a12, coolant decompressor 13, oxygen storage Cryopreservation device 14, nitrogen storage device 15, purifying device for natural gas 16, high-pressure natural gas decompressor 17, middle pressure Natural gas expander 18th, choke valve a19, choke valve b20, choke valve c21, cooler behind air compressor 22, aerator 23 are constituted.
A kind of air-seperation system of utilization high-pressure natural gas pipe network pressure energy, is embodied as comprising the following steps:
(1) high-pressure natural gas pressure energy reclaims
Pressure is that the high-pressure natural gas of 1.5～10mpa are delivered to purifying device for natural gas 16 through natural gas line, at purification Enter high-pressure natural gas decompressor 17 expansion after reason and be depressurized to 1～7mpa, the mechanical work of high-pressure natural gas decompressor output is used for The driving of middle pressure cold medium compressor 9, the middle pressure natural gas of output enters heat exchanger a12 and exports with through high pressure refrigerant compressor 8 High pressure refrigerant heat exchange, be warming up to 15 DEG C～100 DEG C；In entrance, pressure Natural gas expander 18 expands and is depressurized to 0.4～3mpa, The mechanical work obtaining is used for the driving of high pressure refrigerant compressor 8；The low-temp low-pressure natural gas of output is delivered to through natural gas line Heat exchanger b10 with through in pressure cold medium compressor 9 output middle pressure coolant heat exchange, the natural gas after heat exchange through gas pipeline convey To downstream gas distributing system.
(2) it is used for connecting the refrigerant circulation with air-seperation system for the natural gas pressure difference refrigeration system
Low temperature refrigerant enters the air that main heat exchanger 6 exports with molecular sieve adsorption device 4 and the low temperature that rectifying column 7 distributes Waste gas heat exchange, is delivered to middle pressure cold medium compressor 9 through refrigerant pipe after temperature rises to 0～20 DEG C after heat exchange and is pressurized to 2～3mpa, It is low with the low temperature of middle pressure Natural gas expander 18 output that the middle pressure coolant of output is delivered to heat exchanger b10 by coolant utilidor Pressure heat exchange gas, the middle pressure refrigerant temperature of output is reduced to 0 DEG C～30 DEG C, enter high pressure refrigerant compressor 8 be pressurized to 4～ 6mpa, the high pressure refrigerant of output enters heat exchanger a12 with the middle pressure heat exchange gas exporting through high-pressure natural gas decompressor 17, defeated The refrigerant temperature going out is down to 30～0 DEG C, is then passed through refrigerant pipe and is delivered to coolant decompressor 13, the refrigerant temperature fall of output As little as 120～140 DEG C, enter main heat exchanger 6 and form refrigerant circulation circuit.
(3) air separates
Air is conveyed into air filter 1 through aerator 23, and the air of the abjection solid impurity of output is delivered to air compressor machine Group 2,1～2.5mpa air of output is delivered to cooler behind air compressor 22 through air line and is cooled to 90～180 DEG C, is delivered to The Cryogenic air heat exchange that air precooler 3 exports with main heat exchanger 6, the air themperature of output is down to 10～20 DEG C, is delivered to point Son sieve adsorbent equipment 4 enters low temperature refrigerant and the rectifying column 7 that main heat exchanger 6 exports with coolant decompressor 13 after removing water and impurity Push up the low temperature waste gas distributing and carry out heat exchange, the air themperature of output is reduced to 120～140 DEG C, warm pipelined To air expander 8,0.3～1mpa air of output enters from rectifying column 7 bottom, and low-temp low-pressure air is anti-in rectifying column 7 Multiple condensation and evaporation, (the tower bottom outlet from rectifying column 7 of oxygen-containing 99.80%) flows out warm pipeline to oxygen to high-purity liquid oxygen Gas storage device；High Purity Nitrogen (nitrogenous 99.99%) is condensed in lower top of tower condenser/evaporator after liquid nitrogen is drawn and is divided into two strands, Being delivered to rectifying column 7 top after one stock-traders' know-how pressure regulator valve a19 pressure regulation provides cold as backflow for the steam that upper tower rises, another Stock imports liquid nitrogen storage device and is stored；Shunt one low temperature waste gas from rectifying column 7 tower top, be delivered to the same molecule of main heat exchanger 6 After the coolant heat exchange of the air of sieve adsorbent equipment 4 output and coolant decompressor 13 output, it is divided into a two streams part through pressure regulation Valve c21 pressure regulation is outer after being delivered to the air heat-exchange that air precooler 3 is exported with cooler behind air compressor 22 to normal pressure to be drained into greatly Gas；Another stock is delivered to molecular sieve adsorption device 4 and drains into as outer after regeneration gas after being then delivered to electric heater 5 heating by the road Air.The oxygen-enriched liquid air of rectifying column 7 congregate is (about 180 DEG C of oxygen-containing about 38%) from bottom of towe output, about 190 DEG C after pressure regulation From the input of rectifying column 7 top.
With reference to state parameter and the accompanying drawing of Sichuan Natural Gas Station natural gas, technical scheme is made It is discussed further, but embodiments of the present invention not limited to this, for not marked technological parameter, can refer to routine techniquess and enter OK.
Embodiment
A kind of air-seperation system of utilization high-pressure natural gas pipe network pressure energy, its technological process is as shown in figure 1, adopt two Level expands the mode of blood pressure lowering, and refrigerant circulation is chosen as nitrogen.
Certain Natural Gas Station, total score throughput rate is 100 × 104nm3/ d, is delivered to point defeated station from natural gas main pipeline network High-pressure natural gas pressure is 7.0mpa, and temperature is 20.0 DEG C, and the volume composition of natural gas is shown in Table 1, and ambient temperature is 25.0 DEG C, should Water dew point under 7.0mpa for the pipeline gas is 15.0 DEG C, and in point defeated station, the high-pressure natural gas of 7.0mpa need to be reduced to Gas distributing system is pressed to divide in entering after 2.0mpa defeated.The pressure energy now all carrying out controlled atmosphere pressure release with point defeated station is used for freezing, and is Air-separating plant outside Natural Gas Station provides low-temperature receiver.Refrigerant circulation flow is 7000nm3/ h, coolant is chosen as nitrogen. The isentropic efficiency of the equipment such as decompressor, compressor takes 0.8.
Certain Natural Gas Station of table 1 carrys out the gas composition of gas
Composition ch4 c2h6 c3h8 i-c4h10 n-c4h10 i-c5h12 n-c5h12 co2
Mol% 97.56 1.44 0.20 0.02 0.07 0.01 0.02 0.64
The specifically comprising the following steps that of a kind of air-seperation system using high-pressure natural gas pipe network pressure energy
(1) high-pressure natural gas pressure energy reclaims
The tolerance that this point defeated station high-pressure natural gas carrys out gas is 100 × 104nm3/ d, is introduced into purifying device for natural gas 16, removes After removing water and solid impurity, enter high-pressure natural gas decompressor 17 and expand, high-pressure natural gas are depressurized to 3.0mpa by 7.0mpa, high Pressure Natural gas expander 17 output work is 578.2kw, presses cold medium compressor 9, the natural temperature of middle pressure after expansion in driving Degree is down to 29.8 DEG C, enters in 174.9 DEG C flowing out with high pressure refrigerant compressor 11 through heat exchanger a12,5mpa high pressure nitrogen Row heat exchange, after absorbing its heat, temperature is increased to 8.9 DEG C, middle pressure pressure drop 0.5mpa, Ran Houjin in heat exchanger a for the natural gas Enter and in pressure Natural gas expander 18, be expanded to 2mpa, the output work of middle pressure Natural gas expander 18 is 280.7kw, for driving High pressure refrigerant compressor 11, therefrom in pressure Natural gas expander 18, the low pressure natural gas temperature of output is 30.4 DEG C, Ran Houjin Enter 233.2 DEG C, the 1.6mpa medium pressure nitrogen gas heat exchange that heat exchanger b10 flows out with middle pressure cold medium compressor 9, absorb temperature liter after heat Up to 3.4 DEG C, enter downstream gas distributing system.
(2) it is used for connecting the refrigerant circulation with air-seperation system for the natural gas pressure difference refrigeration system
7000nm3/ h, 131.2 DEG C, the cold cycle nitrogen entrance main heat exchanger 6 of 300kpa, divide with rectifying column 7 tower top The air of 191 DEG C of outflow, the low temperature waste gas of 0.13mpa and 10 DEG C after molecular sieve adsorption device 4 filtration, 2mpa is carried out Heat exchange, is warming up to 8 DEG C after absorbing heat, is compressed to 1.6mpa subsequently into middle pressure cold medium compressor 9, middle pressure cold medium compressor 9 Power consumption is about 550.6kw, and circulating nitrogen gas temperature is increased to 233.2 DEG C, subsequently into heat exchanger b10 with middle pressure Natural gas expander 18 30.4 DEG C exporting, the low pressure natural gas of 2mpa carry out heat exchange, and after release heat, temperature is reduced to 18 DEG C, subsequently into height Pressure cold medium compressor 11 is compressed to 4mpa, and high pressure refrigerant compressor 11 power consumption is about 279.2kw, same subsequently into heat exchanger a12 29.8 DEG C, the middle pressure heat exchange gas of 3mpa that high-pressure natural gas decompressor 17 flows out, discharge heat, and temperature is reduced to 27 DEG C, after expanding subsequently into coolant decompressor 13, pressure is down to 0.3mpa, and the output work of coolant decompressor 13 is 215.4kw, follows Ring nitrogen temperature is down to 131.2 DEG C, and circulating nitrogen gas are respectively in the pressure drop of main heat exchanger 6, heat exchanger a12, heat exchanger b10 0.5mpa、0.3mpa、0.3mpa.
(3) air separates
Temperature is that 15 DEG C of raw air inputs self-cleaning air filter 1 except fine particles such as dusts through aerator 23 After solid impurity, air inlet compressor bank 2, the low pressure air compressor in air compressor unit 2 is pressurized to 0.8mpa, low Pressure air compressor power consumption is about 408.5kw, and the middle pressure air compressor unit that temperature is increased in air compressor unit 2 is pressed Contracting, to 2mpa, middle pressure air compressor power consumption is about 416.3kw, and temperature is increased to 182.9 DEG C for pressure rise, enters air compressor machine Aftercooler 22 temperature is down to 164 DEG C.The High Temperature High Pressure air air inlet precooler 3 obtaining, same warp in air precooler 3 8.9 DEG C after main heat exchanger 6 heat exchange, 0.13mpa low temperature waste gas heat exchange, temperature is down to 10 DEG C, and the air after pre-cooling enters and divides Son sieve adsorbent equipment 4, removing water and impurity after enter main heat exchanger 6, disregard pressure drop in molecular sieve adsorption device 4 for the air and Temperature drop.Flow out with coolant decompressor 13 131.2 DEG C, 300kpa low temperature refrigerant and rectifying column 7 top distribute 191 DEG C, 0.13mpa low temperature waste gas carry out heat exchange, and temperature is down to 137 DEG C, and warm pipelined, to air expander 8, is pressed after expansion Power 0.35mpa, the mechanical work of air expander 8 output is 93.2kw, and after expansion, the temperature of air is delivered to essence for 179.3 DEG C Evaporate tower 7 bottom.Low-temp low-pressure air repeatedly condenses in rectifying column 7 and evaporates, upper tower bottom obtain 180.2 DEG C, (oxygen-containing 99.80%) is imported into liquid oxygen storage device storage 14 to 0.135mpa high-purity liquid oxygen.(nitrogenous 99.99%) exists High Purity Nitrogen It is condensed into liquid nitrogen (183.4 DEG C, 0.35mpa) in lower top of tower condenser/evaporator, be divided into two strands after extraction, a stock-traders' know-how pressure regulator valve 19 Pressure regulation provides cold as backflow from the dirty steam for the rising of upper tower of upper top of tower to 0.13mpa, to obtain purity more High liquid form product；Another strand imports liquid nitrogen storage device 15 and is stored；At liquid air charging aperture, lower tower oxygen-enriched liquid air is (oxygen-containing About 38%) about 180 DEG C, after pressure regulator valve 20 pressure regulation, about 190 DEG C enter upper tower upper return.Rectifying column 7 top distributes 5 × 104nm3/ d, 191.5 DEG C, 0.132mpa low temperature waste gas, enter main heat exchanger 6 and adsorb with through molecular sieve adsorption device 4 131.2 DEG C, 300kpa circulating nitrogen gas heat exchange that afterwards 10 DEG C, the air of 2mpa and coolant decompressor 8 flow out, low temperature after heat exchange The temperature of waste gas is increased to 8.9 DEG C, be divided into two strands one 4 × 104nm3The low temperature waste gas air inlet precooler 3 of/d is compression 182.9 DEG C of machine output, 2mpa High Temperature High Pressure air offer cold energy, absorb and drain into air outside the waste gas after heat.Another stock is then Enter molecular sieve adsorption device 4 through choke valve 21, be delivered to electric heater 5, regenerating for molecular sieve adsorption device 4 provides source of the gas, Air is drained into outside afterwards.
Using the air-seperation system of utilization high-pressure natural gas pipe network pressure energy of the present invention, 100 × 104nm3/ d's High-pressure natural gas are about 5650kw by 7mpa pressure regulation to the callable pressure energy of 2mpa, reclaim high-pressure natural gas in this example swollen The mechanical work about 829.6kw that swollen process produces, provides cryogenic cold energy for air separation process simultaneously, can be by 3.09 × 104nm3/h Air be down to 179.6 DEG C of the saturation temperature of 350mpa, relatively going out traditional electric refrigeration low-temperature air separating method can save Electric energy about 726.72 × 104Kwh, energy-conservation is worth about 581.36 × 104Unit.
The above, be only presently preferred embodiments of the present invention, not the present invention is made with any pro forma restriction, though So the present invention is disclosed above with preferred embodiment, but is not limited to the present invention, any is familiar with this professional technology people Member, in the range of without departing from technical solution of the present invention, when the technology contents of available the disclosure above make a little change or modification For the Equivalent embodiments of equivalent variations, as long as being the content without departing from technical solution of the present invention, the technical spirit of the foundation present invention Any simple modification, equivalent variations and the modification that above example is made, all still falls within the range of technical solution of the present invention.

Claims (8)

1. a kind of air-seperation system of utilization high-pressure natural gas pipe network pressure energy is it is characterised in that include pressure energy of natural gas The refrigerant circulation of recovery system, air-seperation system and connection pressure energy of natural gas recovery system and air-seperation system returns Road, the huge cold energy that this refrigerant circulation circuit is used for the generation of gas distributing system pressure reduction changes the air separation dress to invention Put, the cold energy needed for air-seperation system is provided, and the energy discharging when being cooled down by absorption air ensures the low pressure sky of output So temperature degree will not be too low；
Pressure energy of natural gas retracting device is connected it is ensured that between the safety in two regions with air-separating plant by kind of refrigeration cycle Every.
Described pressure energy of natural gas recovery system includes purifying device for natural gas, high-pressure natural gas decompressor, high pressure refrigerant compression Machine, heat exchanger a, coolant decompressor, middle pressure cold medium compressor, middle pressure Natural gas expander, heat exchanger b；Air-seperation system bag Include aerator, air filter, air compressor machine, cooler behind air compressor, air precooler, molecular sieve adsorption device, electric heater, Main heat exchanger, air expander, rectifying column, oxygen-storing device, nitrogen storage device；
Purifying device for natural gas connects high-pressure natural gas decompressor, is then connected into heat exchanger a, it is swollen that heat exchanger a connects coolant respectively Swollen machine and middle pressure Natural gas expander, middle pressure Natural gas expander connects heat exchanger b, and heat exchanger b outlet connects downstream natural gas Pipe network, is simultaneously provided with branch road and connects high pressure refrigerant compressor, high pressure refrigerant compressor accesses heat exchanger a；Coolant decompressor connects Main heat exchanger, heat exchanger has three outlet lines, pressure cold medium compressor, electric heater, air expander, middle pressure in connecting respectively Cold medium compressor connects heat exchanger b, and electric heater is sequentially connected molecular sieve adsorption device and air precooler, and air expander is even It is connected to rectifying column bottom；Aerator is sequentially connected air filter, air compressor machine, cooler behind air compressor, is then connected into air pre- Cooler；Rectifying column upper end outlet connects main heat exchanger, and lower end outlet connects oxygen-storing device and nitrogen storage device respectively.
2. a kind of air separating method of utilization high-pressure natural gas pipe network pressure energy is it is characterised in that include following operating procedure: First, during high-pressure natural gas pressure regulation, the pressure energy of high-pressure natural gas is converted to by mechanical work and cold energy by decompressor, Recycle coolant as medium, reclaim the mechanical energy producing and cold energy, on the one hand utilize high-pressure natural gas to expand the machinery producing Work(compresses coolant so as to become high-pressure refrigeration working medium, on the other hand, by the optimization design of heat-exchange network, using high pressure sky So gas expands the cold energy producing to cool down the high pressure refrigerant after compression, and that improves high-pressure natural gas entrance decompressor enters temperature simultaneously Degree, increases high-pressure natural gas and expands the mechanical work producing, and then using hot insulated line, the high pressure refrigerant after cooling down is delivered to sky Air separation region, recycles the cryogenic cold energy that high pressure refrigerant expander produces；Meanwhile, high pressure refrigerant expands generation Mechanical work is tentatively pressurized after main heat exchanger heat exchange for coolant；Then by hot insulated line, the coolant after preliminary supercharging is conveyed Reclaim high-pressure natural gas to heat exchanger and expand the cold energy producing, form refrigerant circulation.
3. the air separating method of a kind of utilization high-pressure natural gas pipe network pressure energy according to claim 2, its feature exists In comprising the following steps:
A, high-pressure natural gas pressure energy reclaim:
High-pressure natural gas pipe network is delivered to the high-pressure natural gas of voltage regulating station, point defeated station, and pressure is in more than 1.5mpa；High-pressure natural gas After flowing through purifying device for natural gas preliminary treatment, enter high-pressure natural gas expander and be depressurized to 1～7mpa, high-pressure natural gas The mechanical work of decompressor output is used for the driving of middle pressure cold medium compressor, obtains the middle pressure natural gas that temperature reduces simultaneously, and leads to Overregulate the outlet pressure of high-pressure natural gas decompressor it is ensured that its temperature is higher than the water dew point of natural gas；By high-pressure natural gas The high pressure refrigerant heat exchange by heat exchanger a and after high pressure refrigerant compressor compresses for the middle pressure natural gas after expander, After obtaining heat, temperature is increased to 15 DEG C～100 DEG C；Temperature raise after middle pressure natural gas by middle pressure Natural gas expander, After expansion, reduced pressure, to 0.4～3mpa, obtains the low pressure natural gas of temperature reduction, and the mechanical work of acquisition is used for driving high pressure cold Matchmaker's compressor, and ensure that its temperature is higher than its water dew point；Low-temp low-pressure natural gas passes through heat exchanger b with pressure coolant compression in passing through Middle pressure coolant heat exchange after machine compression, the low pressure natural gas temperature after heat exchange is increased to more than 0 DEG C and is delivered to gas distributing system；
B, for connecting the refrigerant circulation with air-seperation system for the natural gas pressure difference refrigeration system:
Low temperature refrigerant flows through the low temperature that the main heat exchanger of air-seperation system distributes with the pressure-air after pre-cooling and rectifying column Waste gas heat exchange, after heat exchange, refrigerant temperature is increased to 0～20 DEG C；Low pressure refrigerant after temperature rising presses cold medium compressor in flowing into, It is pressurized to 2～3mpa, temperature is increased to 90～130 DEG C, becomes middle pressure coolant, its pressure and temperature are subject to high-pressure natural gas decompressor Output work size impact；During middle pressure coolant is delivered to heat exchanger b and is passed through by hot insulated line, pressure Natural gas expander expands Low-pressure low-temperature heat exchange gas afterwards, middle pressure refrigerant temperature is reduced to 0 DEG C～30 DEG C, is then passed through high pressure refrigerant compressor boost To 4～6mpa, become high pressure refrigerant, its pressure and temperature are affected by the output work size of middle pressure Natural gas expander；High pressure is cold By heat exchanger a with the middle pressure heat exchange gas after high-pressure natural gas expander, temperature is down to 30～0 DEG C, so to matchmaker Afterwards coolant decompressor is delivered to by hot insulated line, the refrigerant temperature after expansion is down to 120～140 DEG C；Enter main heat exchange Device provides cold energy for air-separating plant, and middle pressure natural gas expands the mechanical work obtaining and is used for driving the air of air-separating plant Compressor, forms refrigerant circulation；
C, air separate:
Air passes through air line air inlet filter, enters air compressor unit after removing solid impurity, it is compressed to 1～ 2.5mpa；Temperature is increased to 110～200 DEG C, and the air after compression enters cooler behind air compressor and is cooled to 90～180 DEG C；Obtain The High Temperature High Pressure air air inlet precooler obtaining, changes with the Cryogenic air after main heat exchanger heat exchange in air precooler Heat, temperature is down to 10～20 DEG C, and the air after pre-cooling enters molecular sieve adsorption device, enters main heat exchange after removing water and impurity Device, carries out heat exchange with the low temperature waste gas that low temperature refrigerant and rectifying tower top distribute, and temperature is down to 120～140 DEG C, warm Pipelined to air expander, pressure 0.3～1mpa after expansion, temperature is down to the saturation temperature under this pressure, from rectifying column Bottom enters, and low-temp low-pressure air repeatedly condenses in rectifying column and evaporates, and the more oxygen-enriched liquid air of composition containing liquid oxygen is collected in Rectifying column Shang Ta and lower tower bottom, nitrogen is then collected in Shang Ta and lower top of tower；Liquid oxygen tower bottom outlet from rectifying column is flowed out Warm pipeline is to oxygen-storing device；Nitrogen is condensed into liquid nitrogen in lower top of tower condenser/evaporator, is divided into after extraction Two strands, one provides cold as backflow from the dirty steam for the rising of upper tower of upper top of tower, so that it is higher to obtain purity Liquid form product；Another strand imports liquid nitrogen storage device and is stored；Shunt one low temperature waste gas from rectifying column tower top, be delivered to master and change Hot device, after the air after pre- cold cleaning and coolant heat exchange, is divided into two bursts of parts through pressure regulator valve pressure regulation to normal pressure, air inlet Precooler, provides cold, outer row for air, another strand of low temperature waste gas are delivered to electric heater by the road, is molecular sieve adsorption dress Putting regeneration provides source of the gas, drains into air outward afterwards；Oxygen-enriched liquid air (about 180 DEG C of oxygen-containing about 38%), section that rectifier bottoms are assembled After stream, about 190 DEG C enter rectifier backflow, on the one hand increase evaporation cold flow number of times in rectifying column for the liquid air, the opposing party The steam that face rises for upper tower provides cold, the liquid form product higher to obtain purity.
4. the air separating method of a kind of utilization high-pressure natural gas pipe network pressure energy according to claim 3, its feature exists In, in described step a, enter high-pressure natural gas recovery system gas pressure between 1.6～10mpa, using double expansion The mode of heat exchange, including high-pressure natural gas decompressor and middle pressure Natural gas expander, high-pressure natural gas are through two-stage blood pressure lowering, pressure drop To downstream gas distributing system discharge pressure；And by adjusting high-pressure natural gas decompressor and middle pressure Natural gas expander outlet pressure And the flow-control gas outlet temperature of refrigerant circulation is it is ensured that it is higher than gas water dew point.
5. the air separating method of a kind of utilization high-pressure natural gas pipe network pressure energy according to claim 3, its feature exists In pressure cold medium compressor, high pressure refrigerant compressor two-stage supercharging in coolant warp in refrigerant circulation；Middle pressure cold medium compressor is by high pressure The mechanical energy that Natural gas expander produces drives, and high pressure refrigerant compressor is driven by the mechanical energy that middle pressure Natural gas expander produces Dynamic.
6. the air separating method of a kind of utilization high-pressure natural gas pipe network pressure energy according to claim 3, its feature exists In the heat energy that coolant produces through compressor compression supercharging all is used for heating after expanded machine expansion by heat exchanger a, heat exchanger b Natural gas；And high-pressure natural gas expand the coolant that the cold energy producing all heats up after heat exchanger is used for cooling compression.
7. the air separating method of a kind of utilization high-pressure natural gas pipe network pressure energy according to claim 3, its feature exists In, the cold energy temperature that refrigerant circulation provides in air-seperation system, on the one hand can on the other hand may be used by adjusting refrigerant circulation To change the amount of rectifying tower top low temperature waste gas shunting, reduce refrigerant circulation, increase rectifying tower top shunting low temperature waste gas amount, increase Coolant two-stage compression compression ratio all can reduce cryogenic temperature；Contrary then cryogenic temperature can be improved.
8. the air separation side of a kind of utilization high-pressure natural gas pipe network pressure energy according to any one of claim 2～7 Method it is characterised in that separate after liquid oxygen purity be 99.80%, purity liquid nitrogen be 99.99%.
CN201610957129.0A 2016-10-27 2016-10-27 Air separation system and method utilizing pressure energy of high-pressure natural gas pipe network Expired - Fee Related CN106369935B (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
CN201610957129.0A CN106369935B (en) 2016-10-27 2016-10-27 Air separation system and method utilizing pressure energy of high-pressure natural gas pipe network

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
CN201610957129.0A CN106369935B (en) 2016-10-27 2016-10-27 Air separation system and method utilizing pressure energy of high-pressure natural gas pipe network

Publications (2)

Publication Number Publication Date
CN106369935A true CN106369935A (en) 2017-02-01
CN106369935B CN106369935B (en) 2022-04-12

Family

ID=57893848

Family Applications (1)

Application Number Title Priority Date Filing Date
CN201610957129.0A Expired - Fee Related CN106369935B (en) 2016-10-27 2016-10-27 Air separation system and method utilizing pressure energy of high-pressure natural gas pipe network

Country Status (1)

Country Link
CN (1) CN106369935B (en)

Cited By (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN109028759A (en) * 2018-07-12 2018-12-18 北京拓首能源科技股份有限公司 A kind of coolant circulating system using cold energy of liquefied natural gas
CN109140903A (en) * 2018-08-24 2019-01-04 邢仁钊 A kind of space division system and air separating method using cold energy of liquefied natural gas
CN109297043A (en) * 2018-11-09 2019-02-01 湖北和远气体股份有限公司 The method and system of gas supply are stablized in a kind of low energy consumption
CN113149393A (en) * 2021-03-16 2021-07-23 东南大学 Sludge dewatering and drying system driven by natural gas pressure energy
CN114134266A (en) * 2021-11-30 2022-03-04 北京科技大学 Nitrogen gas pipe network system

Citations (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN101532768A (en) * 2009-04-27 2009-09-16 四川空分设备(集团)有限责任公司 Space-division system for highly effectively using cold energy of liquefied natural gas
CN101852529A (en) * 2010-05-28 2010-10-06 华南理工大学 Method and device for efficient utilization of pressure energy of natural gas pipeline network
CN102563958A (en) * 2011-12-13 2012-07-11 华南理工大学 Method for generating power and making ice by aid of pressure energy of natural gas of pipe network and device
CN102660341A (en) * 2012-04-27 2012-09-12 新地能源工程技术有限公司 Process and device utilizing pressure of natural gas to partially liquefy natural gas
CN103629840A (en) * 2013-10-25 2014-03-12 暨南大学 High-pressure natural gas pressure energy refrigeration method for junked tire cryogenic pulverization
CN103968640A (en) * 2014-05-15 2014-08-06 碧海舟（北京）石油化工设备有限公司 Air separation system utilizing natural gas differential pressure power generation cold energy
CN206160625U (en) * 2016-10-27 2017-05-10 西南石油大学 Utilize air separation system of high -pressure natural gas pipe network pressure ability

Patent Citations (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN101532768A (en) * 2009-04-27 2009-09-16 四川空分设备(集团)有限责任公司 Space-division system for highly effectively using cold energy of liquefied natural gas
CN101852529A (en) * 2010-05-28 2010-10-06 华南理工大学 Method and device for efficient utilization of pressure energy of natural gas pipeline network
CN102563958A (en) * 2011-12-13 2012-07-11 华南理工大学 Method for generating power and making ice by aid of pressure energy of natural gas of pipe network and device
CN102660341A (en) * 2012-04-27 2012-09-12 新地能源工程技术有限公司 Process and device utilizing pressure of natural gas to partially liquefy natural gas
CN103629840A (en) * 2013-10-25 2014-03-12 暨南大学 High-pressure natural gas pressure energy refrigeration method for junked tire cryogenic pulverization
CN103968640A (en) * 2014-05-15 2014-08-06 碧海舟（北京）石油化工设备有限公司 Air separation system utilizing natural gas differential pressure power generation cold energy
CN206160625U (en) * 2016-10-27 2017-05-10 西南石油大学 Utilize air separation system of high -pressure natural gas pipe network pressure ability

Cited By (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN109028759A (en) * 2018-07-12 2018-12-18 北京拓首能源科技股份有限公司 A kind of coolant circulating system using cold energy of liquefied natural gas
CN109140903A (en) * 2018-08-24 2019-01-04 邢仁钊 A kind of space division system and air separating method using cold energy of liquefied natural gas
CN109140903B (en) * 2018-08-24 2024-01-09 邢仁钊 Air separation system and air separation method utilizing cold energy of liquefied natural gas
CN109297043A (en) * 2018-11-09 2019-02-01 湖北和远气体股份有限公司 The method and system of gas supply are stablized in a kind of low energy consumption
CN113149393A (en) * 2021-03-16 2021-07-23 东南大学 Sludge dewatering and drying system driven by natural gas pressure energy
CN113149393B (en) * 2021-03-16 2024-04-12 东南大学 Natural gas pressure energy driven sludge dewatering and drying system
CN114134266A (en) * 2021-11-30 2022-03-04 北京科技大学 Nitrogen gas pipe network system

Also Published As

Publication number Publication date
CN106369935B (en) 2022-04-12

Similar Documents

Publication Publication Date Title
CN106369935A (en) Air separation system and method utilizing pressure energy of high-pressure natural gas pipeline network
CN104061757B (en) A kind of liquid oxygen and liquid nitrogen device for making and method
WO2021043182A1 (en) Air separation apparatus and method using lng cold energy
CN104807289B (en) LNG cold energy sky point is utilized to produce the method for liquid oxygen liquid nitrogen
CN202675796U (en) Device utilizing liquefied Natural Gas (LNG) cold energy to produce liquid air separation products
CN108731379A (en) A kind of amount of liquid is adjustable and produces the air separation plant and production method of more specification oxygen products simultaneously
CN102538398A (en) Process and system for purifying, separating and liquefying nitrogen-and-oxygen-containing coal mine methane (CMM)
CN204115392U (en) With the full air separation units producing liquids of air supply compressor
CN104515361B (en) Method for producing liquid carbon dioxide
CN101846436A (en) Full-liquid air separation device using cold energy of liquefied natural gas (LNG)
CN106091574B (en) Gas liquefaction device with compression heat recovery function and liquefaction method thereof
CN109140903A (en) A kind of space division system and air separating method using cold energy of liquefied natural gas
CN107345737A (en) The double condensation stream backed expansion nitrogen making machines of double tower and its method for preparing nitrogen
CN104807290A (en) Device and method for preparing low-pressure nitrogen gas by using single-tower double-backflow expansion
CN208751137U (en) A kind of space division system using cold energy of liquefied natural gas
CN206160625U (en) Utilize air separation system of high -pressure natural gas pipe network pressure ability
CN108759311A (en) The air separation unit and method that big amount of liquid is produced
CN101943512A (en) Air separation method utilizing cold energy of liquefied natural gas
CN102809262B (en) A kind of method and device utilizing IGCC gas turbine compressed air production oxygen
CN201852409U (en) Air separation system utilizing liquefied natural gas (LNG) cold energy
CN104251600A (en) Liquid nitrogen washing device
CN106123487B (en) A kind of devices and methods therefor that pure neon is produced by ne-He mixture
CN110017628A (en) A kind of LNG cold energy use system and method based on argon circulation
CN208688103U (en) A kind of skid movable carbon dioxide displacement of reservoir oil output gas recovery system
CN203240840U (en) Energy saving system integrated by conversion section waste heat recovery and rectisol process refrigeration station

Legal Events

Date Code Title Description
C06 Publication
PB01 Publication
SE01 Entry into force of request for substantive examination
SE01 Entry into force of request for substantive examination
GR01 Patent grant
GR01 Patent grant
CF01 Termination of patent right due to non-payment of annual fee
CF01 Termination of patent right due to non-payment of annual fee

Granted publication date: 20220412