CN110776965A - Low-temperature removal of water and CO in natural gas 2Process flow of - Google Patents
Low-temperature removal of water and CO in natural gas 2Process flow of Download PDFInfo
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- CN110776965A CN110776965A CN201810852914.9A CN201810852914A CN110776965A CN 110776965 A CN110776965 A CN 110776965A CN 201810852914 A CN201810852914 A CN 201810852914A CN 110776965 A CN110776965 A CN 110776965A
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- heat exchanger
- natural gas
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- valve
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- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 title claims abstract description 258
- 239000003345 natural gas Substances 0.000 title claims abstract description 128
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 title claims abstract description 59
- 239000003507 refrigerant Substances 0.000 claims abstract description 103
- 230000018044 dehydration Effects 0.000 claims abstract description 87
- 238000006297 dehydration reaction Methods 0.000 claims abstract description 87
- 239000007789 gas Substances 0.000 claims abstract description 72
- 238000010438 heat treatment Methods 0.000 claims abstract description 69
- 238000001816 cooling Methods 0.000 claims abstract description 66
- 238000005057 refrigeration Methods 0.000 claims abstract description 56
- 239000003949 liquefied natural gas Substances 0.000 claims abstract description 37
- PZZOEXPDTYIBPI-UHFFFAOYSA-N 2-[[2-(4-hydroxyphenyl)ethylamino]methyl]-3,4-dihydro-2H-naphthalen-1-one Chemical compound C1=CC(O)=CC=C1CCNCC1C(=O)C2=CC=CC=C2CC1 PZZOEXPDTYIBPI-UHFFFAOYSA-N 0.000 claims abstract description 25
- 238000007710 freezing Methods 0.000 claims abstract description 13
- 238000003303 reheating Methods 0.000 claims abstract description 13
- 230000008014 freezing Effects 0.000 claims abstract description 12
- 238000000034 method Methods 0.000 claims description 64
- 230000008569 process Effects 0.000 claims description 41
- 239000007788 liquid Substances 0.000 claims description 29
- 239000000047 product Substances 0.000 claims description 13
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 10
- 239000006227 byproduct Substances 0.000 claims description 5
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- 229910052757 nitrogen Inorganic materials 0.000 claims description 5
- 239000002994 raw material Substances 0.000 claims description 5
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- 239000004215 Carbon black (E152) Substances 0.000 claims description 2
- 229930195733 hydrocarbon Natural products 0.000 claims description 2
- 150000002430 hydrocarbons Chemical class 0.000 claims description 2
- 239000013526 supercooled liquid Substances 0.000 claims description 2
- 235000018936 Vitellaria paradoxa Nutrition 0.000 description 13
- 238000001179 sorption measurement Methods 0.000 description 12
- 239000003463 adsorbent Substances 0.000 description 5
- 238000009833 condensation Methods 0.000 description 4
- 230000005494 condensation Effects 0.000 description 4
- 238000004458 analytical method Methods 0.000 description 3
- 238000001035 drying Methods 0.000 description 3
- 238000004519 manufacturing process Methods 0.000 description 3
- 238000000746 purification Methods 0.000 description 3
- 230000008929 regeneration Effects 0.000 description 3
- 238000011069 regeneration method Methods 0.000 description 3
- 238000000926 separation method Methods 0.000 description 3
- 239000007787 solid Substances 0.000 description 3
- 230000007547 defect Effects 0.000 description 2
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/0002—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
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
- C10L3/06—Natural gas; Synthetic natural gas obtained by processes not covered by C10G, C10K3/02 or C10K3/04
- C10L3/10—Working-up natural gas or synthetic natural gas
- C10L3/101—Removal of contaminants
- C10L3/102—Removal of contaminants of acid contaminants
- C10L3/104—Carbon dioxide
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
- C10L3/06—Natural gas; Synthetic natural gas obtained by processes not covered by C10G, C10K3/02 or C10K3/04
- C10L3/10—Working-up natural gas or synthetic natural gas
- C10L3/101—Removal of contaminants
- C10L3/106—Removal of contaminants of water
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
- F25J1/0047—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using an "external" refrigerant stream in a closed vapor compression cycle
- F25J1/005—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using an "external" refrigerant stream in a closed vapor compression cycle by expansion of a gaseous refrigerant stream with extraction of work
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
- F25J1/0047—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using an "external" refrigerant stream in a closed vapor compression cycle
- F25J1/0052—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using an "external" refrigerant stream in a closed vapor compression cycle by vaporising a liquid refrigerant stream
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/006—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the refrigerant fluid used
- F25J1/007—Primary atmospheric gases, mixtures thereof
- F25J1/0072—Nitrogen
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/006—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the refrigerant fluid used
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- F25J1/0092—Mixtures of hydrocarbons comprising possibly also minor amounts of nitrogen
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- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
- F25J1/0203—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using a single-component refrigerant [SCR] fluid in a closed vapor compression cycle
- F25J1/0204—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using a single-component refrigerant [SCR] fluid in a closed vapor compression cycle as a single flow SCR cycle
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
- F25J1/0211—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using a multi-component refrigerant [MCR] fluid in a closed vapor compression cycle
- F25J1/0212—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using a multi-component refrigerant [MCR] fluid in a closed vapor compression cycle as a single flow MCR cycle
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
- F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
- F25J1/0257—Construction and layout of liquefaction equipments, e.g. valves, machines
- F25J1/0262—Details of the cold heat exchange system
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
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- F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
- F25J1/0257—Construction and layout of liquefaction equipments, e.g. valves, machines
- F25J1/0262—Details of the cold heat exchange system
- F25J1/0263—Details of the cold heat exchange system using different types of heat exchangers
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
- F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
- F25J1/0257—Construction and layout of liquefaction equipments, e.g. valves, machines
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- 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
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- F25J2205/20—Processes or apparatus using other separation and/or other processing means using solidification of components
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2205/00—Processes or apparatus using other separation and/or other processing means
- F25J2205/24—Processes or apparatus using other separation and/or other processing means using regenerators, cold accumulators or reversible heat exchangers
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
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- F25J2220/00—Processes or apparatus involving steps for the removal of impurities
- F25J2220/60—Separating impurities from natural gas, e.g. mercury, cyclic hydrocarbons
- F25J2220/64—Separating heavy hydrocarbons, e.g. NGL, LPG, C4+ hydrocarbons or heavy condensates in general
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
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- F25J2220/00—Processes or apparatus involving steps for the removal of impurities
- F25J2220/60—Separating impurities from natural gas, e.g. mercury, cyclic hydrocarbons
- F25J2220/66—Separating acid gases, e.g. CO2, SO2, H2S or RSH
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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- F25J2220/00—Processes or apparatus involving steps for the removal of impurities
- F25J2220/60—Separating impurities from natural gas, e.g. mercury, cyclic hydrocarbons
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- Engineering & Computer Science (AREA)
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- Oil, Petroleum & Natural Gas (AREA)
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- General Chemical & Material Sciences (AREA)
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Abstract
Low-temperature removal of water and CO in natural gas
2The device mainly comprises a refrigerant circulating system and two switching heat exchanger groups, wherein each switching heat exchanger group comprises a precooling dehydration heat exchanger and a copious cooling refrigeration CO removal
2A heat exchanger. The refrigerant circulation system is used for liquefying natural gas and removing water and CO in the natural gas
2The required cold quantity, the switching heat exchanger group is switched to work regularly according to the total resistance value of the natural gas side in each heat exchanger. Removing water from natural gas by precooling dehydration heat exchanger, removing CO by deep cooling and freezing
2CO removal by heat exchanger
2And obtaining a liquefied natural gas product; when the heat exchanger group is switched for reheating, the heating gas is sequentially subjected to deep cooling and freezing to remove CO
2Heat exchanger and precooling dehydration heat exchanger, heating and gasifying water and CO existing in the heat exchanger
2。
Description
Technical Field
The invention belongs to the technical field of natural gas liquefaction, particularly relates to a natural gas purification and liquefaction process flow, and more particularly relates to a method for removing water and CO in natural gas by using low temperature
2The process flow of (1).
Background
The natural gas production place usually has a certain spatial distance from the terminal use, the temperature of the normal pressure liquefied natural gas is usually-161 ℃, the density is about 1/600 under the standard state, the volume energy density can reach more than 70% of the gasoline, thereby being very beneficial to transportation, storage and utilization, and the main purpose of the domestic natural gas liquefaction at present can be basically summarized as follows: firstly, the problem of long-distance transportation is solved; and secondly, the problem of natural gas storage is solved.
The produced natural gas contains water and CO
2And the like, which are easily frozen in a low temperature environment, and are frozen in pipelines and heat exchangers of a natural gas liquefaction plant during liquefaction to causePlugging, which results in the inability of the natural gas liquefaction plant to continue production, necessitates natural gas pretreatment to remove the aforementioned impurities.
In response to the above problems, the conventional approach to natural gas liquefaction plants is to separate the purification and liquefaction of natural gas into two separate systems. For CO
2The removal method commonly used in China comprises a physical adsorption method, a chemical adsorption method, a combined adsorption method, a membrane separation method and the like, but the methods all have certain requirements on application occasions, for example, the physical adsorption method in the dry method is only used for CO
2The chemical adsorption method in the wet method is obvious in economy for treating large natural gas, and the membrane separation method is also directed at high CO content
2The content of natural gas and the removal precision can not meet the quality index requirement of natural gas liquefaction, and CO is treated conventionally
2The technical route has the defects of large one-time investment, complex operation and the like.
Patent document (CN 102636002A) proposes the use of low temperature for CO removal
2But due to CO in the patent
2The temperature range of low-temperature removal of the liquefied natural gas does not reach the temperature of the common liquefied natural gas product (minus 161 ℃), so the method can not ensure that CO in the liquefied natural gas product is removed
2The content of (A) reaches the content index of liquefied natural gas (50ppm), thereby causing CO to be generated in the natural gas treated by the method during liquefaction
2Freezing and blocking cannot guarantee long-time continuous operation of the liquefaction device. On the other hand, the presence of the separator tank 7 in the solution of the above patent reduces the liquefaction rate of the liquefied natural gas. At the same time, the patent is only directed to low temperature CO removal
2The treatment is carried out, and the water contained in the natural gas cannot be removed and purified in the cold box at the same time, so that the dehydration drying tower described in the patent must be additionally added, which increases the one-time investment and the operation cost of the system.
In the current market, no matter the scale of a natural gas liquefaction device, more than 95 percent of devices adopt a wet method to treat CO in natural gas
2The removal is carried out so that the economy becomes higher when the device is directed to a small natural gas liquefaction plantAnd (4) poor.
The conventional removal method for water in the raw material gas by heating adopts a physical adsorption mode to remove water, the conventional physical adsorption mode is mainly divided into a pressure swing adsorption drying mode and an isobaric adsorption drying mode, and the physical adsorption method is adopted to remove water in the current market. The problems of large investment and poor economy of a small-sized natural gas liquefaction device exist, and the adsorbent needs to be replaced regularly, so that the operation cost and the consumption of material loss are increased, the operation cost is integrally increased, and the economy of the small-sized liquefied natural gas is reduced.
Based on the defects of the prior natural gas purification technology, the invention provides the method for simultaneously removing H contained in natural gas by adopting low temperature
2O、CO
2Component (c) to remove H from natural gas
2O、CO
2The composition is completed in the cold box simultaneously with the process of producing liquefied natural gas.
Disclosure of Invention
The invention aims to provide a method for removing water and CO in natural gas by using a low-temperature method
2The process flow of (1).
The specific technical scheme is as follows:
method for removing water and CO in natural gas by using low-temperature method
2The process flow mainly comprises the following steps:
a) containing water and CO
2The normal temperature raw material natural gas enters the shell pass of the first precooling dehydration heat exchanger/the second precooling dehydration heat exchanger through the first air inlet valve/the second air inlet valve, flows from bottom to top to absorb cold energy provided by a refrigerant flowing from top to bottom in the tube pass to cool down, so that moisture contained in the natural gas is gradually condensed and separated from the natural gas, and the condensed H is condensed
2Part of O automatically flows to the bottoms of the first precooling dehydration heat exchanger/the second precooling dehydration heat exchanger to be collected by means of self gravity, part of O is frozen and attached to and fixed on the outer surface of the heat exchanger, and natural gas which passes through the shell pass outlet of the first precooling dehydration heat exchanger/the second precooling dehydration heat exchanger and is discharged through the first exhaust valve/the second exhaust valve is removed H
2Low temperature natural gas of O;
b) through the first preliminaryRemoving H by cold dehydration heat exchanger/second pre-cooling dehydration heat exchanger
2The low-temperature natural gas after O continuously enters the first deep cooling refrigeration CO removal
2Heat exchanger/second cryogenic refrigeration CO removal
2The heat exchanger is further cooled and cooled by the refrigerant outside the tube from bottom to top along the tube pass of the heat exchanger, and the CO is removed along the deep cooling refrigeration
2The natural gas is gradually changed into gas-liquid two phases from a gaseous state until the natural gas is completely changed into liquid natural gas and CO in the natural gas by the flow direction of the heat exchanger and the cooling capacity provided by the refrigerant circulating system
2Gradually cooled to separate out CO, wherein a part of CO is dissolved in the liquefied natural gas and exceeds the saturated solubility
2Then the natural gas is separated out, frozen and attached to and fixed on the inner surface of the heat exchange tube, and finally the natural gas is cooled to become supercooled liquid natural gas, and then CO is removed from the first deep cooling refrigeration
2Heat exchanger/second cryogenic refrigeration CO removal
2Discharging the liquid from a tube pass outlet at the top of the heat exchanger and allowing the liquid to enter a liquid outlet through a first liquid outlet valve/a second liquid outlet valve so as to produce a Liquid Natural Gas (LNG) product;
c) in a refrigerant circulating system for providing cooling capacity for natural gas liquefaction, normal-temperature low-pressure refrigerant from a refrigerant backflow outlet of a main heat exchanger enters a compressor refrigerant inlet of the refrigerant circulating system for pressurization, is cooled by a condenser and then enters a refrigerant inlet of the main heat exchanger, the refrigerant is cooled by the backflow low-pressure refrigerant and then enters a first switching heat exchanger group/a second switching heat exchanger group through a first refrigerant throttle valve/a second refrigerant throttle valve, and the refrigerant entering the first switching heat exchanger group/the second switching heat exchanger group is subjected to first cryogenic freezing for CO removal
2Heat exchanger/second cryogenic refrigeration CO removal
2After the shell pass of the heat exchanger and the tube pass of the first precooling dehydration heat exchanger/the second precooling dehydration heat exchanger, the refrigerant flows through the first check valve/the second check valve from the refrigerant backflow inlet of the main heat exchanger to the main heat exchanger, and then flows through the refrigerant backflow outlet of the main heat exchanger to return to the refrigerant inlet of the refrigerant compressor, so that a closed refrigerant circulation process is formed;
d) when the first switching heat exchanger group/the second switching heat exchanger group is reheated, high-temperature heating gas enters from the first heating gas inlet valve/the second heating gas inlet valve, and then the first heating gas exhaust valve/the second heating gas exhaust valve are opened to switch the heat exchangersReheating to heat and gasify CO present in the heat exchanger bank
2And H
2O。
Furthermore, the refrigerant flowing out of the main heat exchanger can also flow back to the main heat exchanger through a third throttling valve for heat exchange.
Further, the switching of the first switching heat exchanger group and the second switching heat exchanger group is switched periodically according to the total resistance reduction value of the natural gas side in each heat exchanger.
Furthermore, a first temperature sensor and a second temperature sensor are respectively arranged at the shell pass outlets of the first precooling dehydration heat exchanger and the second precooling dehydration heat exchanger, and the water-containing hydrocarbon-mixed by-product can be collected at the bottom of the precooling dehydration heat exchanger while water is removed by adjusting the temperature of the natural gas discharged from the outlet of the precooling dehydration heat exchanger aiming at different natural gas components.
Further, the CO is removed by first cryogenic refrigeration
2Heat exchanger and secondary cryogenic refrigeration CO removal
2And a third temperature sensor and a fourth temperature sensor are respectively arranged at the tube pass outlet of the heat exchanger and used for monitoring the temperature of the discharged liquefied natural gas product. When the first switching heat exchanger group is switched to the second switching heat exchanger group to work, the second throttle valve is opened, the second air inlet valve is opened, the first throttle valve is closed, the first air inlet valve is closed, the temperature value of the second temperature sensor is monitored, and when the temperature value of the second temperature sensor is higher than a set value, the second connecting valve is closed and the second exhaust valve is opened; when the temperature of the second temperature sensor is lower than a set value, the second connecting valve is opened, the second exhaust valve is closed, the temperature value of the fourth temperature sensor is monitored, the second liquid discharge valve is closed when the temperature value of the fourth temperature sensor is higher than the set temperature value, and the second liquid discharge valve is opened when the temperature value of the second temperature sensor is smaller than or equal to the set temperature value.
Furthermore, a fifth temperature sensor and a sixth temperature sensor are respectively arranged at tube pass outlets of the first precooling dehydration heat exchanger and the second precooling dehydration heat exchanger, and in a precooling flow before switching of the first switching heat exchanger group and the second switching heat exchanger group, resistance of a natural gas side of the normally-operated switching heat exchanger group is reducedAfter the value reaches the resistance drop value of the precooling process, precooling is carried out on the switching heat exchanger group after the reheating replacement is finished, the first heating air inlet valve/the second heating air inlet valve are closed, the first heater exhaust valve/the second heating air exhaust valve are closed, and then the CO is removed according to the first deep cooling freezing
2Heat exchanger/second cryogenic refrigeration CO removal
2And gradually starting the first throttle valve/the second throttle valve and opening the first connecting valve/the second connecting valve according to the temperature value of the third temperature sensor/the fourth temperature sensor at the tube pass outlet of the heat exchanger, respectively cooling and precooling the first switching heat exchanger group and the second switching heat exchanger group until the fifth temperature sensor/the sixth temperature sensor meets the precooling temperature value requirement, and ending the precooling process of the first switching heat exchanger group and the second switching heat exchanger group.
Furthermore, the heat exchange tubes in the first precooling dehydration heat exchanger and the second precooling dehydration heat exchanger can adopt finned tubes, so that the condensation of moisture in natural gas on the surfaces of the finned tubes is facilitated while the heat exchange area of the natural gas side is increased, and the analysis of water in the natural gas is accelerated.
Further, when the switching heat exchanger set is reheated, high-temperature heating gas can enter from the middle of the switching heat exchanger set, at the moment, the first exhaust valve/the second exhaust valve is opened, and the first heating gas exhaust valve/the second heating gas exhaust valve and the first heating gas inlet valve/the second heating gas inlet valve are opened simultaneously.
Further, when the switching heat exchanger set is reheated, high-temperature heating gas can also enter from the bottom of the switching heat exchanger set, at the moment, the first heating gas exhaust valve/the second heating gas exhaust valve is opened, and meanwhile, the first heating gas inlet valve/the second heating gas inlet valve is opened.
Further, the refrigerant cycle system is a refrigerant cycle using a plurality of media, for example, an expansion refrigeration cycle or a mixed refrigerant refrigeration cycle.
Further, when the refrigerant cycle is expanded by nitrogen or by nitrogen methane, a turbo expander is provided at the outlet of the main heat exchanger for removing water and CO
2And producing liquefied natural gas to provide cold.
Of the natural gas liquefaction plant of the present inventionThe cold energy comes from the refrigerant circulating system, wherein the cold energy of the refrigerant circulating system is mainly divided into three parts: wherein part of cold energy is continuously supplied to the main heat exchanger, part of cold energy is supplied to the precooling dehydration refrigeration heat exchanger, and part of cold energy is supplied to the copious cooling refrigeration CO removal
2The heat exchanger and the rest part are used for precooling before the switching heat exchanger group after freezing and reheating is put into use. H in natural gas
2O and CO
2Respectively in a precooling dehydration heat exchanger and a deep cooling refrigeration CO removal
2Condensing and freezing in the heat exchanger and attaching the condensed and frozen natural gas to the heat exchange surface of the heat exchanger, wherein the natural gas heat exchanger in the precooling dehydration freezing heat exchanger flows from bottom to top on the shell side, and the refrigerant flows from top to bottom in the tube side to exchange heat with the natural gas on the shell side; low temperature CO removal
2Cryogenic freezing and CO removal of refrigerant
2The shell pass of the heat exchanger flows from top to bottom, and the natural gas flows from bottom to top in the tube pass of the heat exchanger. The flow rate of the natural gas outside the precooling dehydration heat exchanger tube is controlled so as to facilitate the condensation of H in the natural gas by the refrigerant
2And part of O can flow back along the surface of the heat exchanger under the action of gravity and is collected and discharged at the bottom of the heat exchanger, while part of O is frozen on the outer surface of the heat exchanger, and the water content in the feed gas after low-temperature removal can be controlled to be 5 ppm-20 ppm as required. Allowing the natural gas to enter the deep cooling refrigeration CO removal only when the outlet temperature or the water content of the precooling dehydration heat exchanger reaches a design value
2Heat exchanger, CO in feed gas
2After being precooled by a precooling dehydration heat exchanger, the mixture enters deep cooling refrigeration for removing CO
2After the heat exchanger continues to cool down, part of the CO freezes and adheres to the inner surface of the heat exchanger, and part of the CO freezes and adheres to the inner surface of the heat exchanger
2And the liquefied natural gas is dissolved in the LNG liquid, so that the quality of the liquefied natural gas product is ensured. When the resistance in the switching heat exchanger group exceeds the design value, the natural gas is switched into the switching heat exchanger group for heating and reheating, and the switched heat exchanger heats the H frozen on the surface of the heat exchanger by utilizing a reheating gas source
2O and CO
2Heating to change solid state into liquid state water and CO respectively
2Gas, wherein liquid water is discharged from the bottom of the precooling freeze dehydration heat exchanger and solid CO is discharged
2Sublimation to CO by absorbing heat of the regeneration gas
2The gas is discharged together with the regeneration gas.
The invention has the advantages that:
1. improve the economy of a small natural gas liquefaction device and remove CO compared with the traditional amine method
2Physical adsorption to remove H
2Compared with the investment of disposable equipment, the O is reduced by at least 15-20%;
2. removing H
2The O separation process does not involve any adsorbent, so the system does not produce waste gas solid adsorbent;
3. removing H from the solution
2O and CO removal
2In contrast, the system does not need additional heating for regeneration and H removal
2O adsorbent and CO removal
2Regenerating a heat source by the high temperature and the medium temperature of the adsorbent;
4. compared with the conventional adsorption, the valve removes H
2O、CO
2Is not subject to H
2O、CO
2Influence of content and partial pressure;
5. the natural gas liquefaction device has simple and efficient flow and can realize H removal of the device
2O, CO removal
2The unmanned operation is realized by program control, so that the labor cost for operation is greatly reduced;
6. removes the pretreatment CO removal in the conventional natural gas liquefaction device
2And H
2The equipment is rotated in the O flow, so that the failure rate of the device is reduced;
7. LNG products can be continuously produced, and the natural gas with impurities removed can be completely changed into Liquid Natural Gas (LNG) products, so that the liquefaction rate of the natural gas is high;
8. the heating gas can adopt raw materials of natural gas, nitrogen and air, and the sources are simple to obtain;
9. the switching heat exchanger adopts a wound tube type heat exchanger, so that the internal reheating temperature difference is increased when the switching heat exchanger is reheated, and the reheating time of the switching heat exchanger group is reduced;
10. the heat source for heating the gas can adopt high-temperature gas at the outlet of a refrigerant compressor as the heat source;
11. the outlet temperature of the precooling dehydration heat exchanger in the switching heat exchanger group is reasonably adjusted according to the feed gas components, and the hydrocarbon mixture byproduct can be collected at the bottom of the precooling dehydration heat exchanger.
Drawings
FIG. 1: according to the inventionExample 1 removal of water and CO from natural gas using a cryogenic process
2The device and the process flow thereof.
FIG. 2: removal of water and CO from Natural gas Using cryogenic Process according to example 2 of the invention
2The device and the process flow thereof, wherein the refrigerant cycle adopts nitrogen expansion or nitrogen methane expansion.
FIG. 3: example 3 according to the invention removal of water and CO from natural gas using a cryogenic process
2And process flow thereof
Reference numerals:
SHEA/SHEB: a first/second switching heat exchanger group; HE1A/HE 1B: a first/second precooling dehydration heat exchanger; HE2A/HE 2B: first/second cryogenic freezing CO removal
2A heat exchanger; MHE: a primary heat exchanger; V1A/V1B: first/second intake valves; V2A/V2B: a first/second exhaust valve; V3A/V3B: a first/second connecting valve; V4A/V4B: a first/second drain valve; V5A/V5B: a first/second refrigerant throttle valve; V6A/V6B: a first/second heating air exhaust valve; V7A/V7B: first/second heated air inlet valves; v8: a third throttle valve; v9: a first check valve; v10: a second check valve; m1: a primary heat exchanger refrigerant inlet; m2: a primary heat exchanger refrigerant outlet; m3: a refrigerant return port of the main heat exchanger; m4: a refrigerant outflow port; m5: a refrigerant return port; T1A/T1B: a first/second temperature sensor; T2A/T2B: a third/fourth temperature sensor; T3A/T3B: fifth/sixth temperature sensors.
Detailed Description
The process flow of the present invention is described in detail below with reference to FIGS. 1-3 and the corresponding reference numerals.
Example 1:
FIG. 1 illustrates the removal of water and CO from natural gas using a cryogenic process according to the present invention
2The device mainly comprises: the refrigerant circulating system is used for providing cold energy for natural gas liquefaction and mainly comprises a refrigerant compressor, a main heat exchanger MHE, a first refrigerant throttle valve V5A and a second refrigerant throttle valve V5B; a first switching heat exchanger group SHEA comprising a first pre-cooling dehydration heat exchanger HE1A and a first cryogenic refrigeration CO removal
2 Heat exchanger HE 2A; and a second switching heat exchanger groupSHEB comprising a second pre-cooling dehydration heat exchanger HE1B and a second cryogenic refrigeration CO removal
2Heat exchanger HE 2B; the first switching heat exchanger group SHEA and the second switching heat exchanger group SHEB are mutually standby switching heat exchanger groups. A natural gas inlet is respectively connected with shell-side inlets below the first pre-cooling dehydration heat exchanger HE1A and the second pre-cooling dehydration heat exchanger HE1B through a first air inlet valve V1A and a second air inlet valve V2A, a shell-side outlet above the first pre-cooling dehydration heat exchanger HE1A is connected with a discharge port for discharging dehydrated natural gas through a first air outlet valve V2A, and the shell-side outlet is connected with the first cryogenic refrigeration CO-removal through a first connecting valve V3A
2The lower tube pass inlet of the heat exchanger HE2A is connected, the shell pass outlet above the second precooling dehydration heat exchanger is connected with a discharge port for discharging dehydrated natural gas through a second exhaust valve V2B, and the shell pass outlet is connected with the second deep cooling refrigeration CO removal through a second connecting valve V3B
2The lower process inlet of the heat exchanger HE2B is connected; first cryogenic freezing CO removal
2Heat exchanger HE2A and second cryogenic refrigeration CO removal
2Tube pass outlets are arranged above the heat exchanger HE2B and are respectively used for discharging and removing CO after cooling through a first liquid discharge valve V4A and a second liquid discharge valve V4B
2The liquefied natural gas liquid outlet is connected; the outlet of the refrigerant compressor is connected with a condenser, the outlet of the condenser is connected with a refrigerant inlet M1 of a main heat exchanger MHE, and a refrigerant outlet M2 of the main heat exchanger is respectively connected with a first deep cooling refrigeration CO removal through a first expansion valve V5A and a second expansion valve V5B
2Heat exchanger HE2A and second cryogenic refrigeration CO removal
2The refrigerant inlet above the heat exchanger HE2B is connected, and the first deep cooling refrigeration removes CO
2Heat exchanger HE2A and second cryogenic refrigeration CO removal
2A refrigerant outlet below the heat exchanger HE2B is respectively connected with tube pass inlets above the first pre-cooling dehydration heat exchanger and the second pre-cooling dehydration heat exchanger, tube pass outlets below the first pre-cooling dehydration heat exchanger and the second pre-cooling dehydration heat exchanger are respectively connected with a refrigerant backflow inlet M5 of the main heat exchanger through a first check valve V9 and a second check valve V10, and the refrigerant backflow outlet M4 of the main heat exchanger is connected with a refrigerant inlet of the compressor; first cryogenic freezing CO removal
2Heat exchanger HE2A and second cryogenic refrigeration CO removal
2The tube side outlets of the heat exchanger HE2B are respectively subjected to first additionThe hot gas inlet valve V7A and the second heating gas inlet valve V7B are connected with a gas inlet pipeline for the inflow of heating gas for reheating switching heat exchanger groups, and the heating gas is subjected to CO removal along the first deep cooling refrigeration
2Heat exchanger HE 2A/second cryogenic refrigeration CO removal
2The tube pass of heat exchanger HE2B and the shell pass flow of first pre-cooling dehydration heat exchanger HE 1A/second pre-cooling dehydration heat exchanger HE1B are reheated and finally discharged from the heating gas outlet below first pre-cooling dehydration heat exchanger HE 1A/second pre-cooling dehydration heat exchanger HE1B through first heating gas exhaust valve V6A/second heating gas exhaust valve V6B.
Further, a third throttle valve V8 is connected to the refrigerant outlet of the main heat exchanger, and the refrigerant throttled by this throttle valve is returned to the main heat exchanger MHE.
Further, the refrigerant cycle system is a refrigerant cycle using a plurality of media, for example, an expansion refrigeration cycle, a mixed refrigerant refrigeration cycle.
Further, a first temperature sensor T1A and a second temperature sensor T1B are respectively arranged at the shell side outlets of the first pre-cooling dehydration heat exchanger HE1A and the second pre-cooling dehydration heat exchanger HE1B, and for different natural gas components, the water can be removed and simultaneously water-containing hydrocarbon-mixed byproducts can be collected at the bottom of the pre-cooling dehydration heat exchanger by adjusting the temperature of the natural gas discharged from the outlet of the pre-cooling dehydration heat exchanger.
Further, the CO is removed by first cryogenic refrigeration
2Heat exchanger HE2A and second cryogenic refrigeration CO removal
2The tube side outlet of the heat exchanger HE2B is provided with a third temperature sensor T2A and a fourth temperature sensor T2B, respectively, for monitoring the temperature of the discharged liquefied natural gas product. In the precooling process after the switching heat exchanger group is heated and reheated, after the resistance drop value of the natural gas side of the normally operated switching heat exchanger group reaches the designed precooling value, precooling is started on the switching heat exchanger group after reheating replacement is completed, for example, the first switching heat exchanger group SHEA is in production, the second throttle valve is gradually opened at the moment, the opening degree of the first liquid discharge valve V4A is adjusted according to the temperature of the liquefied natural gas product monitored by the third temperature sensor T2A, and continuous production and stable yield of the device are maintained.
Further, a fifth temperature sensor T3A and a sixth temperature sensor T3B are respectively arranged at tube side outlets of the first pre-cooling dehydration heat exchanger and the second pre-cooling dehydration heat exchanger.
Furthermore, the heat exchange tubes in the first and second pre-cooling dehydration heat exchangers HE1A and HE1B can adopt finned tubes, so that the heat exchange area of the natural gas side is increased, and the condensation of moisture in the natural gas on the surfaces of the finned tubes is facilitated, thereby accelerating the analysis of water in the natural gas.
The removal of water and CO from natural gas using a cryogenic process according to the invention as shown in FIG. 1
2The process flow of the device mainly comprises the following steps:
a) containing water and CO
2The normal-temperature raw material natural gas enters the shell passes of the first precooling dehydration heat exchanger HE 1A/the second precooling dehydration heat exchanger HE1B through the first air inlet valve V1A/the second air inlet valve V1B, flows from bottom to top to absorb cold energy provided by refrigerant flowing from top to bottom in the tube pass for cooling, so that moisture contained in the natural gas is gradually condensed and separated from the natural gas, and the condensed H is separated from the natural gas
2Part of O automatically flows to the bottoms of the first pre-cooling dehydration heat exchanger HE1A and the second pre-cooling dehydration heat exchanger HE1B by means of self gravity to be collected, part of O is frozen and attached to the outer surface of the heat exchanger, and natural gas is discharged through the shell pass outlet of the first pre-cooling dehydration heat exchanger HE1A and the second pre-cooling dehydration heat exchanger HE1B and the first exhaust valve V2A and the second exhaust valve V2B, namely H is removed
2Low temperature natural gas of O;
b) h is removed by the first pre-cooling dehydration heat exchanger HE 1A/the second pre-cooling dehydration heat exchanger HE1B
2The low-temperature natural gas after O continuously enters the first deep cooling refrigeration CO removal
2 Heat exchanger HE 2A/second cryogenic refrigeration CO removal
2The heat exchanger HE2B is further cooled by the refrigerant outside the tubes from bottom to top along the tube pass of the heat exchanger, the natural gas is gradually changed into a gas-liquid two-phase state from a gaseous state by the cooling capacity provided by the refrigerant circulating system and finally is completely changed into liquid natural gas, and CO in the natural gas
2Gradually cooled to separate out CO, wherein a part of CO is dissolved in the liquefied natural gas and exceeds the saturated solubility
2Then the natural gas is separated out, frozen and attached and fixed on the inner surface of the heat exchange tube, and finally the natural gasRemoving CO from the first cryogenic refrigeration after being cooled to become subcooled liquid natural gas
2 Heat exchanger HE 2A/second cryogenic refrigeration CO removal
2The liquid is discharged from a tube side outlet at the top of the heat exchanger HE2B and enters a liquid outlet through a first liquid outlet valve V4A/a second liquid outlet valve V4B to produce a Liquid Natural Gas (LNG) product;
c) in a refrigerant circulating system for providing cold for natural gas liquefaction, normal-temperature low-pressure refrigerant from a refrigerant reflux outlet M4 of a main heat exchanger enters a refrigerant inlet M1 of a main heat exchanger MH3 after entering a compressor of the refrigerant circulating system for pressurization and being cooled by a condenser, then enters a first switching heat exchanger group SHEA/a second switching heat exchanger group SHEB through a first refrigerant throttle valve V5A/a second refrigerant throttle valve V5B, and the refrigerant entering the first switching heat exchanger group SHEA/the second switching heat exchanger group SHEB sequentially passes through first deep cooling refrigeration and CO removal
2Heat exchanger HE 2A/second cryogenic refrigeration CO removal
2The heat exchanger HE2B and the first pre-cooling dehydration heat exchanger HE 1A/the second pre-cooling dehydration heat exchanger HE1B enter the main heat exchanger MHE from a refrigerant backflow inlet M5 of the main heat exchanger MHE through a first check valve V9/a second check valve V10, and then heat exchange returns to a refrigerant inlet of the refrigerant compressor through a refrigerant outlet M4 of the main heat exchanger, so that a closed refrigerant circulation process is formed;
d) when the first switching heat exchanger group SHEA/the second switching heat exchanger group SHEB is reheated, firstly, the exhaust valve V6A/the exhaust valve V6B of the first heater is opened to remove liquid at the bottom of the precooling dehydration heat exchanger, then external high-temperature heating gas enters from the first heating gas inlet valve V7A/the second heating gas inlet valve V7B, the first/second exhaust valve V2A/V2B of the first precooling dehydration heat exchanger HE 1A/the second precooling dehydration heat exchanger HE1B is closed, and then the first heating gas exhaust valve V6A/the second heating gas exhaust valve V6B are opened to carry out switching heat exchanger reheating to heat and gasify CO existing in the heat exchanger group
2And H
2O。
Further, the refrigerant flowing out of the main heat exchanger can also flow back to the main heat exchanger MHE for heat exchange through a third throttling valve V8.
Further, the refrigerant cycle system is a refrigerant cycle using a plurality of media, for example, an expansion refrigeration cycle, a mixed refrigerant refrigeration cycle.
Further, a first temperature sensor T1A and a second temperature sensor T1B are respectively arranged at the shell side outlets of the first pre-cooling dehydration heat exchanger HE1A and the second pre-cooling dehydration heat exchanger HE1B, and for different natural gas components and water contents, the water can be removed and simultaneously the water-containing hydrocarbon-mixed by-product can be collected at the bottom of the pre-cooling dehydration heat exchanger by adjusting the temperature of the natural gas discharged from the outlet of the pre-cooling dehydration heat exchanger. During normal operation, only when the temperature values of the first temperature sensor T1A and the second temperature sensor T1B reach set values, the first/second connecting valve V3A/V3B can be opened and the first/second exhaust valve V2A/V2B is closed, so that natural gas with moisture removed by the first precooling dehydration heat exchanger HE1A and the second precooling dehydration heat exchanger HE1B enters the first copious cooling refrigeration CO removal
2Heat exchanger HE2A and second cryogenic refrigeration CO removal
2The tube side inlet below heat exchanger HE 2B.
Further, the CO is removed by first cryogenic refrigeration
2Heat exchanger HE2A and second cryogenic refrigeration CO removal
2A third temperature sensor T2A and a fourth temperature sensor T2B are respectively arranged at a shell pass outlet of the heat exchanger HE2B, and are used for monitoring the temperature of the discharged liquefied natural gas product and controlling the cooling rate of the first switching heat exchanger group SHEA and the second switching heat exchanger group SHEB in the pre-cooling flow before switching.
Further, a fifth temperature sensor T3A and a sixth temperature sensor T3B are respectively arranged at tube side outlets of the first pre-cooling dehydration heat exchanger and the second pre-cooling dehydration heat exchanger. In a precooling process before switching of the first switching heat exchanger group SHEA and the second switching heat exchanger group SHEB, after a resistance drop value on a natural gas side of a normally operated switching heat exchanger group reaches a resistance drop value of a precooling process, precooling is started to be performed on the switching heat exchanger group after reheating replacement is completed, a first heating gas inlet valve V7A/a second heating gas inlet valve V7B are closed, a first heater exhaust valve V6A/a second heating gas exhaust valve V6B are closed, then a first throttle valve V5A/a second throttle valve V5B and a first connecting valve V3A/a second connecting valve V3B are gradually opened according to temperature values of a third temperature sensor T2A/a fourth temperature sensor T2B at an outlet of a tube pass of a first cryogenic refrigeration CO-removing heat exchanger HE 2B/a second cryogenic refrigeration CO-removing heat exchanger HE2A, and the first switching heat exchanger group SHEA and the second heat exchanger group SHEB are respectively cooled until a fifth temperature sensor T3 reaches a sixth temperature sensor T8536/T3 And when the value is required, the precooling process of the first switching heat exchanger group SHEA and the second switching heat exchanger group SHEB is finished.
Furthermore, the heat exchange tubes in the first/second pre-cooling dehydration heat exchanger HE1A/HE1B can adopt finned tubes, so that the heat exchange area of the natural gas side is increased, and the condensation of moisture in the natural gas on the surfaces of the finned tubes is facilitated, so that the analysis of water in the natural gas is accelerated.
Further, the switching of the first switching heat exchanger group SHEA and the second switching heat exchanger group SHEB is switched periodically according to the total resistance reduction value of the natural gas side in each heat exchanger. When the first switching heat exchanger group SHEA is switched to the second switching heat exchanger group SHEB to work, the second throttle valve V5B is opened, the second air inlet valve V1B is opened, the first throttle valve V5A is closed, the first air inlet valve V1A is closed, the temperature value of the second temperature sensor T1B is monitored, and when the temperature value T1B is higher than a set value, the second connecting valve V3B is closed, and the second exhaust valve V2B is opened; when the temperature of the second temperature sensor T1B is lower than the set value, the second connecting valve V3B is opened, the second exhaust valve V2B is closed, the temperature value of the fourth temperature sensor T2B is monitored, the second drain valve V4B is closed when the temperature value of the fourth temperature sensor T2B is higher than the set temperature value, and the second drain valve V4B is opened when the temperature value of the second temperature sensor T1B is lower than or equal to the set temperature value.
Further, when the switching heat exchanger set is reheated, high-temperature heating gas can enter from the middle of the switching heat exchanger set, at this time, the first exhaust valve V2A/the second exhaust valve V2B are opened, and the first heating gas exhaust valve V6A/the second heating gas exhaust valve V6B and the first heating gas inlet valve V7A/the second heating gas inlet valve V7B are opened at the same time.
Further, when the switching heat exchanger set is reheated, high-temperature heating gas can also enter from the bottom of the switching heat exchanger set, at this time, the first heating gas exhaust valve V6A/the second heating gas exhaust valve V6B are opened, and at the same time, the first heating gas inlet valve V7A/the second heating gas inlet valve V7B are opened.
Example 2:
FIG. 2 is a diagram of the removal of water and CO from natural gas using a cryogenic process according to example 2 of the present invention
2The apparatus and process are substantially the same as in example 1 except that the refrigerant cycle is expanded with nitrogen or with methyl-nitrogen, at which time the water is condensed and frozen to remove CO and the water is frozen to remove CO
2The cold energy and the cold energy for producing the liquefied natural gas product mainly come from a turbine expander Tu, namely, the turbine expander Tu is arranged at a refrigerant outlet of the main heat exchanger MHE, and the refrigerant is expanded and cooled by the turbine expander Tu after flowing out of the main heat exchanger to generate a cold energy supply system.
Example 3:
FIG. 3 is a diagram of the removal of water and CO from natural gas using a cryogenic process according to example 3 of the present invention
2The apparatus and process of the present invention are substantially the same as those of embodiment 1, except that the first check valve V9 and the second check valve V10 are replaced with switching valves V9 and V10, and the number of valve timing controls during switching is increased after the check valves are replaced with the switching valves, without substantially departing from the scope of the present invention.
Although embodiments of the present invention have been shown and described above, it is understood that the above embodiments are exemplary only, and are not to be construed as limiting the present invention, and those skilled in the art can make changes, modifications or substitutions to the above embodiments within the scope of the present invention without departing from the scope of the present invention as claimed.
Claims (10)
1. Method for removing water and CO in natural gas by using low-temperature method
2The process flow mainly comprises the following steps:
a) containing water and CO
2The normal temperature raw material natural gas enters the shell pass of the first precooling dehydration heat exchanger/the second precooling dehydration heat exchanger through the first air inlet valve/the second air inlet valve, flows from bottom to top and absorbs the cold energy provided by the refrigerant flowing from top to bottom in the tube pass to cool, so that the natural gas is cooledThe water content is gradually condensed and separated from the natural gas, part of the condensed water automatically flows to the bottoms of the first precooling dehydration heat exchanger/the second precooling dehydration heat exchanger to be collected by means of self gravity, and the other part of the condensed water is frozen and attached to the outer surface of the heat exchanger;
b) the low-temperature natural gas after water removal by the first precooling dehydration heat exchanger/the second precooling dehydration heat exchanger continues to enter the first deep cooling refrigeration CO removal
2Heat exchanger/second cryogenic refrigeration CO removal
2The heat exchanger is further cooled by the refrigerant outside the pipe from bottom to top along the pipe pass of the heat exchanger, the natural gas is gradually changed into gas-liquid two phases from gaseous state until the natural gas is completely changed into liquid natural gas by the cold energy provided by the refrigerant circulating system, and CO in the natural gas
2Gradually cooled to separate out CO, wherein a part of CO is dissolved in the liquefied natural gas and exceeds the saturated solubility
2Then the natural gas is separated out, frozen and attached to and fixed on the inner surface of the heat exchange tube, and finally the natural gas is cooled to become supercooled liquid natural gas, and then CO is removed from the first deep cooling refrigeration
2Heat exchanger/second cryogenic refrigeration CO removal
2Discharging the liquid from a tube pass outlet at the top of the heat exchanger and allowing the liquid to enter a liquid outlet through a first liquid outlet valve/a second liquid outlet valve so as to produce a Liquid Natural Gas (LNG) product;
c) in a refrigerant circulating system for providing cooling capacity for natural gas liquefaction, normal-temperature low-pressure refrigerant from a refrigerant backflow outlet of a main heat exchanger enters a compressor refrigerant inlet of the refrigerant circulating system for pressurization, is cooled by a condenser and then enters a refrigerant inlet of the main heat exchanger, the refrigerant is cooled by the backflow low-pressure refrigerant and then enters a first switching heat exchanger group/a second switching heat exchanger group through a first refrigerant throttle valve/a second refrigerant throttle valve, and the refrigerant entering the first switching heat exchanger group/the second switching heat exchanger group is subjected to first cryogenic freezing for CO removal
2Heat exchanger/second cryogenic refrigeration CO removal
2After the shell pass of the heat exchanger and the tube pass of the first precooling dehydration heat exchanger/the second precooling dehydration heat exchanger, the refrigerant reflowing inflow port of the main heat exchanger enters the main heat exchange port through the first check valve/the second check valveThe refrigerant flows back to the refrigerant inlet of the refrigerant compressor through the refrigerant backflow outlet of the main heat exchanger, so that a closed refrigerant circulation process is formed;
d) when the first switching heat exchanger set/the second switching heat exchanger set is reheated, high-temperature heating gas enters from the first heating gas inlet valve/the second heating gas inlet valve, and then the first heating gas exhaust valve/the second heating gas exhaust valve are opened to conduct switching heat exchanger set reheating so as to heat and gasify CO existing in the heat exchanger set
2And water.
2. The cryogenic process for removing water and CO from natural gas according to claim 10
2In the process flow, the refrigerant flowing out of the main heat exchanger can also flow back to the main heat exchanger through the third throttling valve for heat exchange.
3. The cryogenic process for removing water and CO from natural gas according to claim 10 or 11
2The switching of the first switching heat exchanger group and the second switching heat exchanger group is switched periodically according to the total resistance reduction value of the natural gas side in each heat exchanger.
4. The cryogenic process for removing water and CO from natural gas according to claim 10 or 11
2According to the process flow, a first temperature sensor and a second temperature sensor are respectively arranged at the shell pass outlets of a first precooling dehydration heat exchanger and a second precooling dehydration heat exchanger, and according to different natural gas components, the temperature of the natural gas discharged from the outlet of the precooling dehydration heat exchanger can be adjusted, so that water can be removed, and meanwhile, a water-containing hydrocarbon mixture byproduct can be collected at the bottom of the precooling dehydration heat exchanger.
5. The cryogenic process for removing water and CO from natural gas according to claim 13
2In the first cryogenic refrigeration CO removal
2Heat exchanger and secondary cryogenic refrigeration CO removal
2A third temperature sensor and a fourth temperature sensor are respectively arranged at the tube pass outlet of the heat exchanger and used for monitoring the temperature of the discharged liquefied natural gas productAnd (4) degree.
6. The cryogenic process for removing water and CO from natural gas according to claim 14
2When the first switching heat exchanger group is switched to the second switching heat exchanger group to work, the second throttle valve is opened, the second air inlet valve is opened, the first throttle valve is closed, the first air inlet valve is closed, the temperature value of the second temperature sensor is monitored, and when the temperature value of the second temperature sensor is higher than a set value, the second connecting valve is closed and the second exhaust valve is opened; when the temperature of the second temperature sensor is lower than a set value, the second connecting valve is opened, the second exhaust valve is closed, the temperature value of the fourth temperature sensor is monitored, the second liquid discharge valve is closed when the temperature value of the fourth temperature sensor is higher than the set temperature value, and the opening degree of the second liquid discharge valve is gradually opened and adjusted when the temperature value of the fourth temperature sensor is smaller than or equal to the set temperature value.
7. The cryogenic process for removing water and CO from natural gas according to claim 15
2In the process flow before the switching of the first switching heat exchanger group and the second switching heat exchanger group, after the resistance reduction value of the natural gas side of the switching heat exchanger group in normal operation reaches the resistance reduction value of the precooling flow, precooling is carried out on the switching heat exchanger group after the reheating replacement is finished, the first heating gas inlet valve/the second heating gas inlet valve are closed, the first heater exhaust valve/the second heating gas exhaust valve are closed, and then CO is removed according to the first cryogenic refrigeration
2Heat exchanger/second cryogenic refrigeration CO removal
2The temperature value of a third temperature sensor/a fourth temperature sensor at the tube pass outlet of the heat exchanger gradually opens a first throttle valve/a second throttle valve, opens a first connecting valve/a second connecting valve, respectively carries out cooling and precooling on a first switching heat exchanger group and a second switching heat exchanger group until a fifth temperature sensor/a sixth temperature sensor meets the precooling temperature value requirement, and precooling flows of the first switching heat exchanger group and the second switching heat exchanger groupThe routine ends.
8. The cryogenic process for removing water and CO from natural gas according to claim 10 or 11
2When the switching heat exchanger group is reheated, high-temperature heating gas can enter from the middle of the switching heat exchanger group, at the moment, the first exhaust valve/the second exhaust valve is opened, and the first heating gas exhaust valve/the second heating gas exhaust valve and the first heating gas inlet valve/the second heating gas inlet valve are opened at the same time.
9. The cryogenic process for removing water and CO from natural gas according to claim 10 or 11
2When the switching heat exchanger group is reheated, high-temperature heating gas can also enter from the bottom of the switching heat exchanger group, at the moment, the first heating gas exhaust valve/the second heating gas exhaust valve is opened, and meanwhile, the first heating gas inlet valve/the second heating gas inlet valve is opened.
10. The cryogenic removal of water and CO from natural gas according to any one of claims 10, 11, 14-16
2When the refrigerant circulation adopts nitrogen expansion or nitrogen methane expansion, a turboexpander is arranged at the outlet of the main heat exchanger, and the refrigerant flowing out of the main heat exchanger is expanded in the turboexpander for removing water and CO
2And producing liquefied natural gas to provide cold.
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| CN113683136A (en) * | 2021-09-02 | 2021-11-23 | 上海泓济环保科技股份有限公司 | Heat exchange solidification separation switchable regeneration organic wastewater separation device and use method thereof |
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