CN109654807A - A kind of Method and system for coalbed methane liquefaction - Google Patents

A kind of Method and system for coalbed methane liquefaction Download PDF

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Publication number
CN109654807A
CN109654807A CN201811444660.3A CN201811444660A CN109654807A CN 109654807 A CN109654807 A CN 109654807A CN 201811444660 A CN201811444660 A CN 201811444660A CN 109654807 A CN109654807 A CN 109654807A
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Prior art keywords
gas
coal bed
coal
nitrogen
bed gas
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Inventor
冯会方
张新旺
贺栋
曹明哲
王建斌
吉先锋
毛志军
杨卓鹏
毋亚峰
李爱军
曲飙
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ECO SHANXI COALBED METHANE Co Ltd
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ECO SHANXI COALBED METHANE Co Ltd
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Priority to CN201811444660.3A priority Critical patent/CN109654807A/en
Publication of CN109654807A publication Critical patent/CN109654807A/en
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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
    • F25J1/0228—Coupling of the liquefaction unit to other units or processes, so-called integrated processes
    • F25J1/0234—Integration with a cryogenic air separation unit
    • 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
    • F25J3/0204—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 characterised by the feed stream
    • F25J3/0209—Natural gas or substitute natural gas
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—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
    • F25J3/0228—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 characterised by the separated product stream
    • F25J3/0233—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 characterised by the separated product stream separation of CnHm with 1 carbon atom or more
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—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
    • F25J3/0228—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 characterised by the separated product stream
    • F25J3/0257—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 characterised by the separated product stream separation of nitrogen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/08—Separating gaseous impurities from gases or gaseous mixtures or from liquefied gases or liquefied gaseous mixtures
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2205/00—Processes or apparatus using other separation and/or other processing means
    • F25J2205/40—Processes or apparatus using other separation and/or other processing means using hybrid system, i.e. combining cryogenic and non-cryogenic separation techniques
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2210/00—Processes characterised by the type or other details of the feed stream
    • F25J2210/40—Air or oxygen enriched air, i.e. generally less than 30mol% of O2
    • 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
    • F25J2215/00—Processes characterised by the type or other details of the product stream
    • F25J2215/04—Recovery of liquid products
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2220/00—Processes or apparatus involving steps for the removal of impurities
    • F25J2220/60—Separating impurities from natural gas, e.g. mercury, cyclic hydrocarbons
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2220/00—Processes or apparatus involving steps for the removal of impurities
    • F25J2220/60—Separating impurities from natural gas, e.g. mercury, cyclic hydrocarbons
    • F25J2220/62—Separating low boiling components, e.g. He, H2, N2, 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
    • 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
    • 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
    • F25J2270/42—Quasi-closed internal or closed external nitrogen refrigeration cycle

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  • Mechanical Engineering (AREA)
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  • General Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
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Abstract

The present invention relates to the technical fields of gas utilization to reduce line clogging possibility more particularly to a kind of Method and system for coalbed methane liquefaction, improves the rate of utilization of work hour, improves raw material recycling rate of waterused, improves LNG purity；The following steps are included: (1) removes the sour gas such as carbon dioxide and hydrogen sulfide in unstripped gas: unstripped gas enters ethanol amine absorption tower, ethanol amine absorption tower is drenched using the aqueous ethanolamine of 10%-20% from ethanol amine absorbing tower top spray, and coal bed gas enters the ethanol amine mist of water tourie removal coal bed gas entrainment after purification；(2) most of water is removed, makes coal bed gas by mole sieve drier, the moisture removal that mole sieve drier carries coal bed gas secretly, the coal bed gas after drying enters filter, the molecular sieve dust carried secretly in filter removal coal bed gas；(3) depth removes water；(4) nitrogen processed；(5) coal gas gasification；(6) LNG is purified.

Description

A kind of Method and system for coalbed methane liquefaction
Technical field
The present invention relates to the technical fields of gas utilization, more particularly to a kind of coal gas gasification method and coal seam gas-liquid Change system.
Background technique
It is well known that LNG is a kind of colourless, tasteless, nontoxic and non-corrosive liquid, main component is methane, The weight that volume is about 1/625, LNG of same amount gaseous natural gas volume is only 45% or so of androgynous ponding, has larger heat Value, and generated after completely burned without toxic and harmful gas, it is widely used in a variety of applications in the field of the energy.
Coal bed gas refer to be stored in coal seam using methane as main component, to be adsorbed on based on matrix of coal particle surface, portion Divide the hydrocarbon gas for being free in coal hole or being dissolved in coal seam water, be the associated minerals resource of coal, belongs to Unconventional gas, It is cleaning, high-grade energy and the industrial chemicals to emerge in the world in nearly ten or twenty year, coal bed gas is commonly called as " gas ", and calorific value is general 2-5 times of coal, the calorific value of 1 cubic metre of pure coal bed gas are equivalent to 1.13kg gasoline, 1.21kg standard coal, calorific value and natural gas phase When, can be mixed with natural gas it is defeated mixed, and burn after it is very clean, be nearly free from any exhaust gas, be first-class industry, change Work, power generation and resident living fuel, when coal bed gas air concentration reaches 5%-16%, meeting open fire will explode, this is coal mine gas The root of explosion accident, coal bed gas are directly discharged in atmosphere, and greenhouse effects are about 21 times of carbon dioxide, to ecological environment It is destructive extremely strong.If first exploiting coal bed methane before coal mining, coal mine gas from explosion rate will reduce by 70% to 85%, and coal bed gas is opened Hair, which utilizes, to be had effects that achieve many things at one stroke.
The common separation method of coal bed gas has absorption process, absorption method, film osmosis process and cryogenic rectification method, existing to adopt more With cryogenic rectification method, for existing method generally using first filtering in cooling method, this mode be easy to cause pipeline blockage, working hour Utilization rate is low, and raw material recycling rate of waterused is lower, and the LNG purity of output is lower.
Gas chromatography is the method for being commonly used to detection natural gas purity, and the LNG ingredient produced using the prior art is such as Under: methane 99.0%, hydrogen sulfide 0.1%, carbon dioxide 0.2%, nitrogen 0.4%, remaining ingredient are other organic gas.
Summary of the invention
In order to solve the above technical problems, the present invention provides a kind of reduction line clogging possibility, the rate of utilization of work hour is improved, is mentioned High raw material recycling rate of waterused improves the Method and system for coalbed methane liquefaction of LNG purity.
A kind of coal gas gasification method of the invention, comprising the following steps:
(1) remove the sour gas such as carbon dioxide and the hydrogen sulfide in unstripped gas: unstripped gas enters ethanol amine absorption tower, ethanol amine Absorption tower is drenched using the aqueous ethanolamine of 10%-20% from ethanol amine absorbing tower top spray, and coal bed gas enters water absorption after purification Tank removes the ethanol amine mist of coal bed gas entrainment；
(2) it removes most of water: coal bed gas after purification being carried out to be forced into 0.1-0.4Mpa, is then cooled down, then by gas-liquid point From most of water in coal bed gas after device removal purification；
(3) depth removes water: make coal bed gas by mole sieve drier, the moisture removal that mole sieve drier carries coal bed gas secretly, Coal bed gas after drying enters filter, the molecular sieve dust carried secretly in filter removal coal bed gas；
(4) nitrogen processed: outside air enters nitrogen making machine, and nitrogen making machine produces high-purity nitrogen, stores spare to nitrogen storage tank；
(5) coal gas gasification；Expanding machine is by high-purity nitrogen greenhouse cooling to natural gas boiling point low temperature nitrogen formed below, low temperature Nitrogen temperature is -140 degrees Celsius to -170 degrees Celsius, carries out heat exchange, coal bed gas transformation subsequently into heat exchanger and coal bed gas For gas-liquid mixed state coal bed gas；
(6) LNG is purified: gas-liquid mixed state coal bed gas enters separator, and gaseous state mixed state coal bed gas gas-liquid two-phase is separated, liquid State LNG enters LNG storage tank and stores.
A kind of coal gas gasification method of the invention, it is preferred that coal bed gas is forced into 0.3Mpa in the step (2).
A kind of coal gas gasification method of the invention, it is preferred that aqueous ethanolamine concentration is 15% in the step (1).
A kind of coal gas gasification method of the invention, it is preferred that the low temperature nitrogen temperature mentioned in the step (5) be- 140 degrees Celsius to -160 degrees Celsius.
A kind of coal gas gasification system of the invention, including with lower unit:
Sour gas absorptive unit: including ethanol amine absorption tower and water tourie, unstripped gas is connected to the ethanol amine absorption tower, Ethanol amine absorption tower is connected to the water tourie；
Pre-water removal unit: including compressor, cooler and gas-liquid separator, the compressor is connected to water tourie, described cold But device is communicated with compressor；
Depth removes water unit: including mole sieve drier and filter, the mole sieve drier is connected to gas-liquid separator, institute Filter is stated to be connected to molecular sieve drying；
Nitrogen unit processed: including nitrogen making machine and nitrogen storage tank, the nitrogen storage tank is connected to nitrogen making machine output end；
Liquefaction unit: including expanding machine and heat exchanger, the expanding machine is connected to nitrogen storage tank, and the heat exchanger and expanding machine connect It is logical；
Separative unit: including LNG storage tank and separator, the LNG storage tank is connected to separator.
A kind of coal gas gasification system of the invention, it is preferred that the mole sieve drier is three groups.
A kind of coal gas gasification system of the invention, the separator top are provided with cold recovery pipeline, cold recovery Pipeline output end is connected to cooler, and cooler bottom is provided with oxygen-enriched air pipeline, oxygen-enriched air pipeline and nitrogen making machine Connection.
A kind of coal gas gasification system of the invention, the heat exchanger bottom end is provided with nitrogen pipeline and nitrogen storage tank connects It is logical.
A kind of coal gas gasification system of the invention, the filter are bag-type dust filter.
Compared with prior art the invention has the benefit that unstripped gas goes removing carbon dioxide and hydrogen sulfide etc. acid first Gas, then fluid under pressure removes unstripped gas inner most water, further removes original subsequently into three groups of mole sieve driers A possibility that expecting that the moisture of gas inner inclusion, three groups of molecular sieve filters are used alternatingly, reducing line clogging, improves utilization of hour Rate, then the molecular sieve dust being mingled in unstripped gas is removed by bag-type dust filter, make carbon dioxide, the sulphur in coal bed gas product Change hydrogen and dust minimizes, and during coal gas gasification, the oxygen-enriched air that unstripped gas is separated be can be used as A part of cooling capacity source of cooler, and can be used as the gas source of nitrogen making machine, raw material recycling rate of waterused is improved, environment is reduced Pollution, is conducive to environmental protection, by above-mentioned process, improves LNG purity, reduces the other impurities ingredient in LNG.
Detailed description of the invention:
Fig. 1 is a kind of schematic diagram of coal gas gasification system of the invention.
Specific embodiment
With reference to embodiment, the embodiment of the present invention is furthur described in detail.Following embodiment is used for Illustrate the present invention, but is not intended to limit the scope of the invention.
Embodiment 1:
Unstripped gas (40% methane, 55% air, 5% other) enter ethanol amine absorption tower, ethanol amine absorption tower use 15% ethyl alcohol Amine aqueous solution is drenched from ethanol amine absorbing tower top spray, and coal bed gas enters the ethanol amine of water tourie removal coal bed gas entrainment after purification Mist, compressor carry out coal bed gas after purification to be forced into 0.3Mpa, and the coal bed gas of 0.3Mpa enters cooler cooling, cooler Cold source is provided by extraneous chilled water, most of water after then being purified by gas-liquid separator removal in coal bed gas, then coal bed gas By one group of mole sieve drier, the moisture removal that this group of mole sieve drier carries coal bed gas secretly, second set of molecules sieve is done Dry device carries out ramp regeneration, and the sieve drier regeneration of third component is finished in cooling state, three groups of molecular sieve drying machines It is used alternatingly, the coal bed gas after drying enters bag-type dust filter, point carried secretly in bag-type dust filter removal coal bed gas Son sieve dust, and periodic cleaning bag-type dust filter interior filter cloth bag, outside air enter nitrogen making machine, nitrogen making machine production High-purity nitrogen out, stores spare to nitrogen storage tank, and expanding machine is by high-purity nitrogen greenhouse cooling to the following shape of natural gas boiling point At low temperature nitrogen, low temperature nitrogen temperature is -140 degrees Celsius, carries out heat exchange, low temperature nitrogen subsequently into heat exchanger and coal bed gas Enter nitrogen storage tank after heat exchange, gaseous state coal bed gas is changed into gas-liquid mixed state coal bed gas, and gas-liquid mixed state coal bed gas, which enters, divides From device, gaseous state mixed state coal bed gas gas-liquid two-phase is separated, and liquid LNG enters LNG storage tank and stores, and gas phase is returned along cooling capacity Closed tube road provides a part of cold source for cooler, enters nitrogen making machine input terminal along oxygen-enriched air pipeline after gas phase heat exchange.
Embodiment 2:
Unstripped gas (40% methane, 55% air, 5% other) enter ethanol amine absorption tower, ethanol amine absorption tower use 15% ethyl alcohol Amine aqueous solution is drenched from ethanol amine absorbing tower top spray, and coal bed gas enters the ethanol amine of water tourie removal coal bed gas entrainment after purification Mist, compressor carry out coal bed gas after purification to be forced into 0.3Mpa, and the coal bed gas of 0.3Mpa enters cooler cooling, cooler Cold source is provided by extraneous chilled water, most of water after then being purified by gas-liquid separator removal in coal bed gas, then coal bed gas By one group of mole sieve drier, the moisture removal that this group of mole sieve drier carries coal bed gas secretly, second set of molecules sieve is done Dry device carries out ramp regeneration, and the sieve drier regeneration of third component is finished in cooling state, three groups of molecular sieve drying machines It is used alternatingly, the coal bed gas after drying enters bag-type dust filter, point carried secretly in bag-type dust filter removal coal bed gas Son sieve dust, and periodic cleaning bag-type dust filter interior filter cloth bag, outside air enter nitrogen making machine, nitrogen making machine production High-purity nitrogen out, stores spare to nitrogen storage tank, and expanding machine is by high-purity nitrogen greenhouse cooling to the following shape of natural gas boiling point At low temperature nitrogen, low temperature nitrogen temperature is -160 degrees Celsius, carries out heat exchange, low temperature nitrogen subsequently into heat exchanger and coal bed gas Enter nitrogen storage tank after heat exchange, gaseous state coal bed gas is changed into gas-liquid mixed state coal bed gas, and gas-liquid mixed state coal bed gas, which enters, divides From device, gaseous state mixed state coal bed gas gas-liquid two-phase is separated, and liquid LNG enters LNG storage tank and stores, and gas phase is returned along cooling capacity Closed tube road provides a part of cold source for cooler, enters nitrogen making machine input terminal along oxygen-enriched air pipeline after gas phase heat exchange.
Embodiment 3:
Unstripped gas (40% methane, 55% air, 5% other) enter ethanol amine absorption tower, ethanol amine absorption tower use 15% ethyl alcohol Amine aqueous solution is drenched from ethanol amine absorbing tower top spray, and coal bed gas enters the ethanol amine of water tourie removal coal bed gas entrainment after purification Mist, compressor carry out coal bed gas after purification to be forced into 0.3Mpa, and the coal bed gas of 0.3Mpa enters cooler cooling, cooler Cold source is provided by extraneous chilled water, most of water after then being purified by gas-liquid separator removal in coal bed gas, then coal bed gas By one group of mole sieve drier, the moisture removal that this group of mole sieve drier carries coal bed gas secretly, second set of molecules sieve is done Dry device carries out ramp regeneration, and the sieve drier regeneration of third component is finished in cooling state, three groups of molecular sieve drying machines It is used alternatingly, the coal bed gas after drying enters bag-type dust filter, point carried secretly in bag-type dust filter removal coal bed gas Son sieve dust, and periodic cleaning bag-type dust filter interior filter cloth bag, outside air enter nitrogen making machine, nitrogen making machine production High-purity nitrogen out, stores spare to nitrogen storage tank, and expanding machine is by high-purity nitrogen greenhouse cooling to the following shape of natural gas boiling point At low temperature nitrogen, low temperature nitrogen temperature is -152 degrees Celsius, carries out heat exchange, low temperature nitrogen subsequently into heat exchanger and coal bed gas Enter nitrogen storage tank after heat exchange, gaseous state coal bed gas is changed into gas-liquid mixed state coal bed gas, and gas-liquid mixed state coal bed gas, which enters, divides From device, gaseous state mixed state coal bed gas gas-liquid two-phase is separated, and liquid LNG enters LNG storage tank and stores, and gas phase is returned along cooling capacity Closed tube road provides a part of cold source for cooler, enters nitrogen making machine input terminal along oxygen-enriched air pipeline after gas phase heat exchange.
Comparative example 1:
Unstripped gas (40% methane, 55% air, 5% other) initially enter bag-type dust filter except dust, coal bed gas after dedusting Moisture in coal bed gas is removed into gas-liquid separator, then coal bed gas removes moisture removal into one group of molecular sieve drying machine depth, this The moisture removal that one group of mole sieve drier carries coal bed gas secretly, second set of molecules sieve drier progress ramp regeneration, and the Three groups of mole sieve drier regeneration are finished in cooling state, and three groups of molecular sieve drying machines are used alternatingly, and outside air enters system Nitrogen machine, nitrogen making machine produce high-purity nitrogen, store spare to nitrogen storage tank, and expanding machine is by high-purity nitrogen greenhouse cooling to day Right gas boiling point low temperature nitrogen formed below, low temperature nitrogen temperature are -152 degrees Celsius, are carried out subsequently into heat exchanger and coal bed gas Heat exchange, enters nitrogen storage tank after low temperature nitrogen heat exchange, gaseous state coal bed gas is changed into gas-liquid mixed state coal bed gas, gas-liquid mixed State coal bed gas enters separator, and gaseous state mixed state coal bed gas gas-liquid two-phase is separated, and liquid LNG enters LNG storage tank and stores Come, gas phase provides a part of cold source along cold recovery pipeline for cooler, enters system along oxygen-enriched air pipeline after gas phase heat exchange Nitrogen machine input terminal.
Zincizing will be passed through in above-described embodiment and comparative example and handle metal component progress salt spray test obtained, obtain result It is as follows:
The above is only a preferred embodiment of the present invention, it is noted that those skilled in the art are come It says, without departing from the technical principles of the invention, several improvements and modifications can also be made, these improvements and modifications are also answered It is considered as protection scope of the present invention.

Claims (9)

1. a kind of coal gas gasification method, which comprises the following steps:
(1) remove the sour gas such as carbon dioxide and the hydrogen sulfide in unstripped gas: unstripped gas enters ethanol amine absorption tower, ethanol amine Absorption tower is drenched using the aqueous ethanolamine of 10%-20% from ethanol amine absorbing tower top spray, and coal bed gas enters water absorption after purification Tank removes the ethanol amine mist of coal bed gas entrainment；
(2) it removes most of water: coal bed gas after purification being carried out to be forced into 0.1-0.4Mpa, is then cooled down, then by gas-liquid point From most of water in coal bed gas after device removal purification；
(3) depth removes water: make coal bed gas by mole sieve drier, the moisture removal that mole sieve drier carries coal bed gas secretly, Coal bed gas after drying enters filter, the molecular sieve dust carried secretly in filter removal coal bed gas；
(4) nitrogen processed: outside air enters nitrogen making machine, and nitrogen making machine produces high-purity nitrogen, stores spare to nitrogen storage tank；
(5) coal gas gasification；Expanding machine is by high-purity nitrogen greenhouse cooling to natural gas boiling point low temperature nitrogen formed below, low temperature Nitrogen temperature is -140 degrees Celsius to -170 degrees Celsius, carries out heat exchange, coal bed gas transformation subsequently into heat exchanger and coal bed gas For gas-liquid mixed state coal bed gas；
(6) LNG is purified: gas-liquid mixed state coal bed gas enters separator, and gaseous state mixed state coal bed gas gas-liquid two-phase is separated, liquid State LNG enters LNG storage tank and stores.
2. a kind of coal gas gasification method as described in claim 1, which is characterized in that preferred, coal seam in the step (2) Gas is forced into 0.3Mpa.
3. a kind of coal gas gasification method as described in claim 1, which is characterized in that preferred, ethyl alcohol in the step (1) Amine aqueous solution concentration is 15%.
4. a kind of coal gas gasification method as described in claim 1, which is characterized in that it is preferred, it is mentioned in the step (5) Low temperature nitrogen temperature be -140 degrees Celsius to -160 degrees Celsius.
5. a kind of coal gas gasification system, which is characterized in that including with lower unit:
Sour gas absorptive unit: including ethanol amine absorption tower and water tourie, unstripped gas is connected to the ethanol amine absorption tower, Ethanol amine absorption tower is connected to the water tourie；
Pre-water removal unit: including compressor, cooler and gas-liquid separator, the compressor is connected to water tourie, described cold But device is communicated with compressor；
Depth removes water unit: including mole sieve drier and filter, the mole sieve drier is connected to gas-liquid separator, institute Filter is stated to be connected to molecular sieve drying；
Nitrogen unit processed: including nitrogen making machine and nitrogen storage tank, the nitrogen storage tank is connected to nitrogen making machine output end；
Liquefaction unit: including expanding machine and heat exchanger, the expanding machine is connected to nitrogen storage tank, and the heat exchanger and expanding machine connect It is logical；
Separative unit: including LNG storage tank and separator, the LNG storage tank is connected to separator.
6. a kind of coal gas gasification system as claimed in claim 5, which is characterized in that preferred, the mole sieve drier It is three groups.
7. a kind of coal gas gasification system as claimed in claim 5, which is characterized in that be provided with cooling capacity at the top of the separator Recovery pipe, cold recovery pipeline output end are connected to cooler, and cooler bottom is provided with oxygen-enriched air pipeline, oxygen-enriched Air pipe line is connected to nitrogen making machine.
8. a kind of coal gas gasification system as claimed in claim 5, which is characterized in that the heat exchanger bottom end is provided with nitrogen Pipeline is connected to nitrogen storage tank.
9. a kind of coal gas gasification system as claimed in claim 5, which is characterized in that the filter is bag-type dust filter.
CN201811444660.3A 2018-11-29 2018-11-29 A kind of Method and system for coalbed methane liquefaction Pending CN109654807A (en)

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