CN107099348A - The method that synthetic natural gas is produced using underground coal gasification(UCG) product gas - Google Patents
The method that synthetic natural gas is produced using underground coal gasification(UCG) product gas Download PDFInfo
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- CN107099348A CN107099348A CN201710304488.0A CN201710304488A CN107099348A CN 107099348 A CN107099348 A CN 107099348A CN 201710304488 A CN201710304488 A CN 201710304488A CN 107099348 A CN107099348 A CN 107099348A
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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
- C10L3/08—Production of synthetic natural gas
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
- C10K1/00—Purifying combustible gases containing carbon monoxide
- C10K1/002—Removal of contaminants
- C10K1/003—Removal of contaminants of acid contaminants, e.g. acid gas removal
- C10K1/004—Sulfur containing contaminants, e.g. hydrogen sulfide
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
- C10K1/00—Purifying combustible gases containing carbon monoxide
- C10K1/002—Removal of contaminants
- C10K1/003—Removal of contaminants of acid contaminants, e.g. acid gas removal
- C10K1/005—Carbon dioxide
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
- C10K1/00—Purifying combustible gases containing carbon monoxide
- C10K1/08—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors
- C10K1/16—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors with non-aqueous liquids
- C10K1/18—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors with non-aqueous liquids hydrocarbon oils
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
- C10K1/00—Purifying combustible gases containing carbon monoxide
- C10K1/34—Purifying combustible gases containing carbon monoxide by catalytic conversion of impurities to more readily removable materials
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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
- C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
- C10L2290/04—Gasification
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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
- C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
- C10L2290/06—Heat exchange, direct or indirect
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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
- C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
- C10L2290/08—Drying or removing water
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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
- C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
- C10L2290/44—Deacidification step, e.g. in coal enhancing
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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
- C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
- C10L2290/54—Specific separation steps for separating fractions, components or impurities during preparation or upgrading of a fuel
- C10L2290/545—Washing, scrubbing, stripping, scavenging for separating fractions, components or impurities during preparation or upgrading of a fuel
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
- Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
Abstract
The present invention relates to a kind of method that utilization underground coal gasification(UCG) product gas produces synthetic natural gas, step is as follows：（1）Underground coal gasification(UCG) produces the crude synthesis gas of appropriate economic scale；（2）Obtain dry synthesis gas；（3）Dry synthesis gas is delivered to acid Water gas shift/WGS and cooling unit, adjusts the desired C/Hratio of downstream methanation reaction；（4）Synthesis gas after cooling is delivered to acid gas removal unit, absorbs the sour gas H in synthesis gas2S and CO2；（5）Unnecessary carbon dioxide is further removed by acid gas removal unit in synthesis gas, and limits the excessive CO remained in synthetic natural gas2；（6）Synthesis gas obtains final products synthetic natural gas by methanation unit synthesizing methane.The method that the utilization underground coal gasification(UCG) product gas that the present invention is provided produces synthetic natural gas, makes full use of the principal by product in coal underground gasifying technology to extend downstream finished product scope, reduces the cost of post-production processing and discharge.
Description
Technical field
The present invention relates to a kind of method that utilization underground coal gasification(UCG) product gas produces synthetic natural gas, belong to coal underground
Gasification product gas technical field of comprehensive utilization.
Background technology
Underground coal gasification(UCG)（ISC）Be one by oxidant, burning and gasification reaction by subterranean coal are straight coal
Switch through the process for turning to product gas.Product gas is commonly known as synthesis gas, can be used as fuel production, Chemical Manufacture, generating etc.
The raw material of downstream process.The technical process set shaft building completion, underground coal mining and coal gasification process technology, with security
Well, the advantages of investing small, high efficiency, pollution less.
Coal gasification process is the process that coal is changed into synthesis gas by a series of chemical reaction.It is wherein main
Reaction includes：
C+H20 → H2+CO（Steam gasification reacts）
CO+H20 ↔ H2+CO2（Water gas shift reaction）
CO+3H2↔ CH4+H20 （Methanation reaction）
C+2H2 → CH4（Hydrogen gasification reaction）
C+½O2→ CO （Partial oxidation reaction）
C+O2 → CO2（Complete oxidation）
C+CO2→ 2CO（Carbon dioxide gasification reacts）
One drilling well for being used for oxidant injection is referred to as " injection well ", and another drilling well for being used to produce product gas is referred to as " production
Product well ".Directed drilling and vertical drilling can all be used as injection well or product well.Underground coal gasification(UCG)（ISC）May be in injection well
Also need to use one or more peupendicular holes between product well（For example：Functional well and service well）.
When having injection well, product well and horizontal channel to connect the two in coal seam, this construction is referred to as a coal
Charcoal underground gasification（ISC）Unit or well pair.ISC units include combustion zone, gasification zone and pyrolysis zone.Wherein, combustion zone is in coal seam
Near middle oxidant decanting point；Gasification zone is centered around around combustion zone with radial form or in combustion zone downstream, and coal exists
Gasification zone is gasified, part is oxidized, so as to generate product gas；Pyrolysis zone typically exists in gasification zone downstream, the pyrolytic reaction of coal
Here occur.The product gas of high temperature is finally transported to ground from gasification zone toward downstream flow from product well well head.In coal combustion
Or while gasification, it is big that the ISC burned out area in coal seam can grow change.
The product gas generated by underground coal gasification(UCG)（Crude synthesis gas）Usually contain synthesis gas（CO、CO2、H2、CH4And its
The mixture of his gas）And other compositions（Solid particle, water, coal tar, hydrocarbon vapours, other microcomponents include H2S、
NH4, COS etc.）.Its complicated component degree depends on many aspects：Oxidant used in underground coal gasification(UCG)（Air or other
Oxidant, such as oxygen, oxygen-enriched air or vapour mixture）, inherent water in coal seam or surrounding formations penetrate into coal seam water,
The operating parameter of ature of coal and coal underground gasifying technology, including temperature, pressure etc..
According to existing patent document, the comprehensive utilization of current underground coal gasification(UCG) product gas is still faced with many problems,
It is specific as follows：
A) small-scale air gasification synthesis gas power generating demonstration project is removed（Including the direct generation of electricity and mix burning generate electricity）Outside, lack extensive
Industrialize project implementation and operation.
B) all kinds of byproducts of underground coal gasification(UCG) production, such as hydrogen sulfide/sulphur, process water, carbon dioxide, coal tar
Oil etc. reduces or removed these byproducts without clear and definite and ripe industrialization method of comprehensive utilization or technique.
C) the downstream syngas production synthetic natural gas SNG for coal underground gasifying technology is lacked（Gaseous fuel）Work
Skill flow scheme.
D) air gasification, three kinds of different process of oxygen-rich gasification and pure oxygen gasification in coal underground gasifying technology are produced
Synthesis gas product quality difference it is larger, directly affect processing condition and method downstream, it is impossible to lump together.
E) downstream syngas is not considered and the beneficial byproduct coal bed gas in Optimum utilization coal seam in detail using technique.
The content of the invention
It is an object of the invention to solve the deficiencies in the prior art to produce using underground coal gasification(UCG) product gas there is provided one kind
The method of synthetic natural gas.The method that the utilization underground coal gasification(UCG) product gas that the present invention is provided produces synthetic natural gas, fully
Using in coal underground gasifying technology principal by product extend downstream finished product scope, not only reduce post-production processing and
The cost of discharge, also add Project Product yield and income from sales.
The technical solution adopted for the present invention to solve the technical problems is：
The method that synthetic natural gas is produced using underground coal gasification(UCG) product gas, methods described is comprised the following steps：
（1）Multiple underground gasification furnaces or gasification furnace group are thick by oxygen-rich gasification or the appropriate economic scale of pure oxygen gasification technique productions
Synthesis gas；
（2）Crude synthesis gas is delivered to ground by product well, and enters crude synthesis gas cooling, washing and separative element, is done
Synthesis gas, the dry synthesis gas includes H2、CO、CO2、CH4、H2S, COS and HCN composition；
（3）Dry synthesis gas is delivered to CO excessive in acid Water gas shift/WGS and cooling unit, dry synthesis gas and carried out with water vapour
Catalytic reaction, generates H2And CO2, adjust the desired C/Hratio of downstream methanation reaction；
（4）Synthesis gas after cooling is delivered to acid gas removal unit, and the porch of the acid gas removal unit is provided with
Mercury removal reactor, using counter-current gas absorption process, the sour gas in synthesis gas is absorbed in absorption tower using renewable solvent
Body H2S and CO2, obtain and meet downstream synthesis technique requirement H2S contents<1ppmv synthesis gas；
（5）Unnecessary carbon dioxide is further removed by acid gas removal unit in synthesis gas, further to verify methane
Change H in the synthesis gas that reaction is required2:CO2Stoichiometric proportion is 4 or H2:CO stoichiometric proportions are 3, and are limited in synthetic natural gas
The excessive CO of residual2；
（6）Synthesis gas is provided with cobalt molybdenum zinc oxide catalyst by methanation unit synthesizing methane, the methanation unit entrance
Protect reactor, it is ensured that the sulphur of any residual in removing synthesis gas；Wet synthetic natural gas is delivered to dewatering unit removing moisture,
Obtain final products synthetic natural gas.
It is preferred that, step（2）The direct cooling technique that the middle step of use cooling water washing one is carried out, or use cooling water washing two
Walk the indirect cooling technique carried out.
It is preferred that, step（3）Synthesis gas after middle catalytic reaction is after supercooling, and the liquids recovery of condensation is simultaneously delivered to acid
Water steam stripping unit is handled, and the waste heat of cooling procedure is used to produce low-pressure steam or preboiler feedwater, by directly or
Connect the reactor of heating sour water stripping (SWS) unit and separate the sour gas condensed in acidic liquid while adding caustic soda, then
Sour gas is delivered to sulfur cream unit, by H2S changes into sulphur.
It is preferred that, step（4）It is molten with the physics of SELEXOL techniques that middle acid gas removal unit uses low-temp methanol to wash
Agent adsorption technology, the solvent rich in sour gas for leaving absorption tower bottom is sent in regeneration reactor, passes through low-pressure steam
Strip the H that desolvation absorbs2S, then converts it into sulphur, is handled by multi-step pressure reduction and nitrogen stripping, will be with H2S mono-
Absorbed carbon dioxide is played to remove from solvent.
It is preferred that, step（1）The coal tar of acquisition, into coal tar processing unit, is divided into coal by distilling by coal tar
Tar naphtha and coal tar distillate, then by removing the sulphur of residual to coal tar naphtha hydrotreating, after desulfurization
Coal tar naphtha be delivered to pre-reforming unit, gas stream of the production rich in methane is simultaneously delivered to self-heating recapitalization unit, from
In thermal reforming unit, the gas stream rich in methane is reformed using carbon dioxide or steam and oxygen, self-heating recapitalization unit
Synthesis gas enters acid water gas conversion after being mixed with dry synthesis gas with suitable proportion and cooling unit carries out subsequent treatment.
It is preferred that, H in steam autothermal reforming reaction, steam self-heating recapitalization product gas is selected in self-heating recapitalization unit2:COization
Metering is learned than being 2.5:1, the H in carbon dioxide self-heating recapitalization product gas2:CO stoichiometric proportions are 1:1.
It is furthermore preferred that step（3）Dry synthesis gas, is firstly transferred to acid gas removal cell processing, the sour gas
The porch of removal unit includes COS hydrolysis units, and in the porch of self-heating recapitalization unit, dry synthesis gas passes through a catalyst
Protection reactor, removes residual impurity, to protect self-heating recapitalization unit catalyst and downstream methanation catalyst, then synthesis gas
Into self-heating recapitalization unit, the height of the oxygen produced with air-separating plant, the steam of boiler for producing and pre-reforming unit production
The product solid/liquid/gas reactions of methane content, produce self-heating recapitalization unit synthesis gas, afterwards, self-heating recapitalization unit synthesis gas enters back into water coal
Gas is converted and cooling unit, the H needed for adjustment methanation unit2:CO stoichiometric proportions.
It is preferred that, the process water of self-heating recapitalization unit generation is delivered to recycling after process water processing unit processes,
Excessive carbon dioxide is removed by decarburization unit, the decarbonization process used include chemisorbed, physical absorption, adsorbent bed,
Absorption regeneration method, low temperature processing or membrane separation process.
The beneficial effects of the invention are as follows：The utilization underground coal gasification(UCG) product gas production synthetic natural gas that the present invention is provided
Method, makes full use of the principal by product in coal underground gasifying technology to extend downstream finished product scope, not only reduces the later stage
Working process and the cost of discharge, also add Project Product yield and income from sales.
Brief description of the drawings
Retouched to more clearly describe the accompanying drawing used required in the technology flow of the present invention, specific embodiment
State as follows.It should be evident that drawings in the following description are only some embodiments of the present invention, for the common skill in this area
For art personnel, on the premise of not paying creative work, other accompanying drawings can also be obtained according to these accompanying drawings.
Fig. 1 is underground coal gasification(UCG) pure oxygen gasification product gas production synthetic natural gas（SNG）Square process chart, side
Case one；
Fig. 2 is underground coal gasification(UCG) pure oxygen gasification product gas production synthetic natural gas（SNG）Square process chart, scheme
Two；
Fig. 3 is underground coal gasification(UCG) pure oxygen gasification product gas production synthetic natural gas（SNG）Square process chart, scheme
Three.
In the accompanying drawings, identical reference refers to same parts.
1st, air-separating plant（ASU）；2nd, oxygen；3rd, nitrogen；4th, ISC underground gasification furnaces；5th, crude synthesis gas；6th, thick synthesis
Air cooling, washing and separative element；7th, dry synthesis gas；8th, process water；9th, technique unit for treating water；10th, raw water；11st, Waste
Material；12nd, the process water of processing；13rd, gasify unit for treating water；14th, gasified water；15th, coal tar；16th, coal tar processing unit；
17th, the coal tar of processing；17a, coal tar naphtha；17b, coal tar distillate；18th, acid Water gas shift/WGS（SWGS）/ water
Gas conversion（WGS）And cooling unit；19th, sour water stripping (SWS)（SWS）Unit；20th, sour gas；21st, acid gas removal（AGR）
Unit；22nd, carbon dioxide；23rd, sulfur cream unit；24th, sulphur；25th, methanation unit；26th, dewatering unit；27th, methane pressure
Contracting unit；28th, synthetic natural gas（SNG）；29th, pre-reforming unit；30th, self-heating recapitalization unit（ATR）；31st, ATR synthesis gas；32、
Boiler；33rd, steam；34th, flammable boiler exhaust gas.
Embodiment
Below by specific embodiment, and with reference to accompanying drawing, technical scheme is described in further detail.
In one embodiment, ISC pure oxygen gasifications（Fig. 1）, air-separating plant（ASU）1 is higher than for producing concentration
90mole% liquid oxygen（LOX）2 are used for underground coal gasification(UCG) pure oxygen gasification.Meanwhile, air-separating plant（ASU）1 also produces nitrogen
Gas 3, can be used as the public work of whole technique, and such as ISC underground gasification furnaces 4 are purged, and pipeline and equipment purging, project are driven and stopped
Car purging etc..When needing the nitrogen of higher pressure, required supply pressure is provided using booster compressor.High concentration liquid oxygen
（LOX）2 also pass through booster pump, increase oxygen supply pressure.Then by evaporator, carried to the injection well of ISC underground gasification furnaces 4
Supply state oxygen（GOX）2.For ISC pure oxygen gasifications, air compressor is only used for the debugging of downstream process Interruption period between The following article, started
And shutoff operation, and can be shared between multiple ISC underground gasification furnaces 4.Therefore, it is unlisted in the normal operation process flows of Fig. 1
Air compressor.Single air-separating plant（ASU）1 can provide multiple ISC underground gasification furnaces 4 simultaneously, be specifically dependent upon list
Individual air-separating plant（ASU）The oxygen demand of 1 production capacity and single ISC underground gasification furnaces 4.High concentration gaseous state oxygen（GOX）2 notes
Enter after ISC underground gasification furnaces 4 and to be reacted with coal seam, produce the extremely low crude synthesis gas 5 of nitrogen content, be relatively more suitable for downstream
High pressure and pyrolytic conversion application.Crude synthesis gas 5 is delivered to ground by product well, and enters crude synthesis gas cooling, washing and divide
From unit 6.Crude synthesis gas 5 passes through direct cooling technique（Liquid or gas cooling, Venturi, cooling tower etc.）Or it is indirectly cold
But technique（Blade fan, heat exchanger etc.）It is quickly cooled to<150oC.Wherein, direct cooling technique contains crude synthesis gas and washed
The step of washing, and cooling technique then needs at least one scrubbing tower by the trace contaminant in crude synthesis gas indirectly（Particulate matter, chlorine
Compound, mercury, ammonia etc.）Removed from crude synthesis gas.Synthesis gas after washing is removed in synthesis gas subsequently into gas-liquid separator
The free fluid of residual, generates temperature<100oC dry synthesis gas 7.The process water 8 isolated from scrubbing tower and gas-liquid separator
It is delivered to technique unit for treating water 9.Pass through Mechanical Method（Gravitational settling, oil skimmer, filtering, counter-infiltration）, chemical method（As condensed
Agent, antisludging agent, corrosion inhibiter, pH nertralizers etc.）And bioanalysis（Aerobic bacteria, anaerobic bacteria, activated sludge process, circulation activity are dirty
Mud method, the fixed film activity sludge of integration, membrane bioreactor etc.）Handled.Raw water 10, is used as whole technological process
Water is supplemented, is also handled in the lump into technique unit for treating water 9.Process residue 11, including solid waste, sludge and dense salt
Water is handled, it is necessary to carry out specialty by garbage loading embeading, burning or third party's facility and extract.The process water 12 of processing can use
In all downstream applications or be directly entered gasification unit for treating water 13, produce the gasified water 14 for ISC underground gasification furnaces 4.Coal
Tar 15 is delivered in coal tar processing unit 16 and is processed further, and removes all remaining moisture in coal tar 15（Process water
8）, such as handled by demulsification, precipitation and water-oil separating etc..Dry coal tar 15 is by screening and is filtered to remove consolidating for its residual
After body particle, naphtha 17a and distillate 17b is produced by distillation technique, available for boiler and generating set（For example it is reciprocating
Engine, turbine etc.）Fuel or direct marketing.The dry main component of synthesis gas 7 is H2, CO, CO2And CH4, contain simultaneously
H2S, COS and HCN trace impurity.
Dry synthesis gas 7 is firstly transferred to acid Water gas shift/WGS（SWGS）With cooling unit 18.It is excessive in dry synthesis gas 7
CO carries out catalytic reaction with water vapour（Such as cobalt-molybdenum catalyst or other suitable catalyst）, generate H2And CO2, with realization
Swim the desired C/Hratio of methanation reaction, H2:CO2Stoichiometric proportion is 4 or H2:CO stoichiometric proportions are 3（Depending on synthesis gas
Component）.Change with water-gas after traditional desulfurization（WGS）Technique is compared, using acid Water gas shift/WGS（SWGS）Technique can be by
Nitric sulfid（COS）It is hydrogen sulfide with other organic sulfur conversions（H2S）, be conducive to downstream sulfur removal technology, it is not necessary to extra vulcanization
Carbon（COS）Hydrolysis process.In addition, acid Water gas shift/WGS（SWGS）The optimum position of unit 18 positioned at crude synthesis gas cooling down, water
Wash with after separative element 6, higher water content is conducive to improving the conversion ratio of Water gas shift/WGS and reduced anti-in synthesis gas
Answer vapor consumption.Wherein, as the CO contents in dried fruit synthesis gas 7 are relatively low, without converting more CO with needed for realizing
H2:CO stoichiometric proportions, then can select acid Water gas shift/WGS（SWGS）Unit branch road skips the processing procedure（Fig. 1 is not marked
Go out）.Synthesis gas after conversion is after supercooling, and the liquids recovery of condensation is simultaneously delivered to sour water stripping (SWS) unit 19 and handled.It is cold
But the waste heat of process can be used for production low-pressure steam or preboiler feedwater.By directly or indirectly heating sour water stripping (SWS) unit 19
Reactor and simultaneously add caustic soda will condense acidic liquid in sour gas 20（H2S, a small amount of CO2And NH3）Separation.So
Sour gas 20 is delivered to sulfur cream unit 23 afterwards（Such as claus sulphur recovery units）, by H2S changes into sulphur 24.Cooling
Synthesis gas afterwards is delivered to acid gas removal unit（AGR）21, wherein there is mercury removal reactor in the porch of the unit
（Fig. 1 is not marked）.The unit uses counter-current gas absorption process, and the acid in synthesis gas is absorbed using renewable solvent in absorption tower
Property gas（H2S and CO2）, obtain and meet downstream synthesis technique requirement H2S contents<1ppmv synthesis gas, preferably H2S contents<
0.1ppmv.The technology that the unit is used is that low-temp methanol washes physical solvent adsorption technology with SELEXOL techniques.Leave suction
The solvent rich in sour gas for receiving tower bottom is sent in regeneration reactor, strips what desolvation absorbed by low-pressure steam
H2S, then converts it into sulphur 24.Handled by multi-step pressure reduction and nitrogen stripping, can by with H2S absorbed dioxies together
Change carbon 22 to remove from solvent.
For 200-600 meters of ub-bituminous coal-bituminous coal of buried depth, the synthesis gas H of underground coal gasification(UCG) ISC productions2:CO chemistry meters
Amount is than usually 2:1-3:1, H2:CO2Stoichiometric proportion is usually 1:1.2-1:2.5.If underground combustion and the water burst of gasification zone
Amount is higher and when still keeping optimal gasification condition, then the H of synthesis gas2And CO2Content increase, while CO contents are reduced（Similar water coal
Gas converter unit 18）.If likewise, implementing underground coal gasification(UCG) in the deeper coal seam of buried depth, due to methanation reaction tendency
In higher operating pressure condition, so the H of synthesis gas2Reduced with CO contents, while CH4And CO2Content increase.
Using underground coal gasification(UCG) product gas, ISC synthesis gas 7 produces synthetic natural gas（SNG）, its methanation lead to
Often it is constrained to H in synthesis gas2Content.Unnecessary carbon dioxide 22 passes through acid gas removal in synthesis gas 7（AGR）Unit 21
Removing, to provide the H of methanation reaction requirement2:CO2Stoichiometric proportion is 4:1（Or H2:CO stoichiometric proportions are 3:1）, and limit
The excessive CO remained in synthetic natural gas processed2.The carbon dioxide 22 of removing can be used for fertilizer production, carbon dioxide drive（EOR）
Or further sale after purification.Because sulphur can cause the poisoning of methanation process catalyst（Such as Ni-Al2O3）, in methanation unit
25 porch need to generally install the protection reactor for being loaded with cobalt molybdenum zinc oxide catalyst, it is ensured that any residual in removing synthesis gas
Sulphur.Methanation reaction is generally carried out under 20-40barg high pressure, and the conversion ratio of the higher methanation reaction of operating pressure is also more
It is high to synthesize atmospheric pressure, it is necessary to pass through synthesic gas compressor and lifted.Methanation reaction is mainly comprising two highly exothermic chemical reactions
（CO2 + 4H2↔CH4 + 2H2O, Δ H298K= -165 kJ/mol；CO + 3H2↔ CH4 + 2H2O, Δ H298K = -206
kJ/mol）.After vapor is generated in course of reaction, water gas shift reaction（CO + H2O ↔ CO2 + H2）With above-mentioned two
Individual reaction is carried out simultaneously.Due to the high exothermic heat of methanation reaction, heat energy can be reclaimed using multistage methanator
And comprehensive utilization（Fig. 1 is not marked）.Wet synthetic natural gas（SNG）It is delivered to dewatering unit 26, wherein conduct after condensate moisture
Process water 8 is removed, and is delivered to technique unit for treating water 9 and is handled and recycled.Finally, by final products synthesis of natural
Gas（SNG）28 are compressed storage, pipeline and direct marketing.
In another embodiment, technological process as shown in Figure 2, improves and utilizes the production of underground coal gasification(UCG) product gas
The by-product utilization rate of synthetic natural gas.In coal tar processing unit 16, coal tar is divided into coal tar oilstone brain by distilling
Oily 17a（240 DEG C of boils up till）With coal tar distillate 17b.Then by being removed to coal tar naphtha 17a hydrotreatings
The sulphur of residual, its sour gas product can be incorporated into existing sulfur cream unit 23.Coal tar naphtha 17a after desulfurization
Pre-reforming unit 29 is delivered to, gas stream of the production rich in methane is simultaneously delivered to self-heating recapitalization unit（ATR）30.In self-heating recapitalization
Unit（ATR）In 30, reformed using 2 pairs of gas streams rich in methane of carbon dioxide 22 or steam 33 and oxygen（2CH4 +
O2 + CO2 → 3H2 + 3CO + H2O；4CH4 + O2 + 2H2O → 10H2+ 4CO）.Due to H in ISC synthesis gas2Contain
Amount is limited, and it is advantageous to steam self-heating recapitalization（ATR）H in reaction, its ATR synthesis gas 312:CO stoichiometric proportions are 2.5:1
（H in carbon dioxide self-heating recapitalization product gas2:CO stoichiometric proportions are 1:1）.ATR synthesis gas 31 is mixed with ISC synthesis gas 7
Enter acid water gas conversion afterwards（SWGS）With cooling unit 18.Self-heating recapitalization unit（ATR）Steam 33 needed for 30 is by pot
The production of stove 32 is provided, and its fuel can select coal tar fraction 17b, synthetic natural gas（SNG）Product or other fuel oil.Required
Boiler feedwater is provided by gasification unit for treating water 13.
In another embodiment, Fig. 3 is shown with high methane and gaseous state hydrocarbon content（Such as ethane, ethene, third
Alkane, propylene etc.）Underground coal gasification(UCG) product gas produce synthetic natural gas technological process.It can be avoided using the technological process
Gaseous hydrocarbons, which enters methanation unit 25, to be increased equipment investment and reduces the product quality of final products natural gas, while can be with
Downstream cryogenic separation and purified natural gas equipment investment are reduced, production cost is reduced.Underground coal gasification(UCG) pure oxygen gasification product gas,
Dry synthesis gas 7, is firstly transferred to acid gas removal（AGR）Unit 21 is handled.The flow will be in acid gas removal unit 21
Porch include COS hydrolysis units（Fig. 3 is not marked）.In self-heating recapitalization unit（ATR）30 porch, synthesis gas passes through one
Individual catalyst protection reactor（Fig. 3 is not marked）, remove the mercury of residual, other heavy metals, sulphur, the impurity such as chloride, to protect
ATR catalyst and downstream methanation catalyst.Then synthesis gas enters self-heating recapitalization unit（ATR）30, with air-separating plant
（ASU）The product gas for the high methane content that the steam 33 and pre-reforming unit 29 that oxygen 2, the boiler 32 of 1 production are produced are produced is anti-
Should, production ATR synthesis gas 31.Afterwards, ATR synthesis gas 31 enters Water gas shift/WGS（WGS）With cooling unit 18（Fig. 3 is not marked
Branch road）, the H needed for adjustment methanation unit 252:CO stoichiometric proportions.Self-heating recapitalization unit（ATR）The technique of 30 generations simultaneously
Water 8, is delivered to recycling after technique unit for treating water 9 is handled.Excessive carbon dioxide 22 is removed by decarburization unit 35.
The decarbonization process used includes chemisorbed（Methylethanolamine, Benfield etc.）, physical absorption（Low-temp methanol is washed, SELEXOL
Technique）, adsorbent bed（Aluminum oxide, zeolite, activated carbon）, absorption regeneration method（Transformation, alternating temperature, washing）, low temperature processing or film point
From method.According to practical operation situation, wherein most easy integration, the method with Optimum Economic benefit are chosen.Synthesis gas after decarburization
It is delivered to after methanation unit 25, dewatering unit 26 and methane compression unit 27, final products pressure synthesis natural gas（SNG）28
Available for storing, pipeline and direct marketing.
Embodiment described above is a kind of preferably scheme of the present invention, not makees any formal to the present invention
Limitation, also has other variants and remodeling on the premise of without departing from the technical scheme described in claim.
Claims (8)
1. the method for synthetic natural gas is produced using underground coal gasification(UCG) product gas, it is characterised in that：Methods described includes as follows
Step：
（1）Multiple underground gasification furnaces or gasification furnace group are thick by oxygen-rich gasification or the appropriate economic scale of pure oxygen gasification technique productions
Synthesis gas；
（2）Crude synthesis gas is delivered to ground by product well, and enters crude synthesis gas cooling, washing and separative element, is done
Synthesis gas, the dry synthesis gas includes H2、CO、CO2、CH4、H2S, COS and HCN composition；
（3）Dry synthesis gas is delivered to CO excessive in acid Water gas shift/WGS and cooling unit, dry synthesis gas and carried out with water vapour
Catalytic reaction, generates H2And CO2, adjust the desired C/Hratio of downstream methanation reaction；
（4）Synthesis gas after cooling is delivered to acid gas removal unit, and the porch of the acid gas removal unit is provided with
Mercury removal reactor, using counter-current gas absorption process, the sour gas in synthesis gas is absorbed in absorption tower using renewable solvent
Body H2S and CO2, obtain and meet downstream synthesis technique requirement H2S contents<1ppmv synthesis gas；
（5）Unnecessary carbon dioxide is further removed by acid gas removal unit in synthesis gas, further to verify methane
Change H in the synthesis gas that reaction is required2:CO2Stoichiometric proportion is 4 or H2:CO stoichiometric proportions are 3, and are limited in synthetic natural gas
The excessive CO of residual2；
（6）Synthesis gas is provided with cobalt molybdenum zinc oxide catalyst by methanation unit synthesizing methane, the methanation unit entrance
Protect reactor, it is ensured that the sulphur of any residual in removing synthesis gas；Wet synthetic natural gas is delivered to dewatering unit removing moisture,
Obtain final products synthetic natural gas.
2. the method that utilization underground coal gasification(UCG) product gas according to claim 1 produces synthetic natural gas, its feature exists
In：Step（2）The direct cooling technique that the middle step of use cooling water washing one is carried out, or using the indirect of the step of cooling water washing two progress
Cooling technique.
3. the method that utilization underground coal gasification(UCG) product gas according to claim 1 produces synthetic natural gas, its feature exists
In：Step（3）Synthesis gas after middle catalytic reaction is after supercooling, and the liquids recovery of condensation is simultaneously delivered to sour water stripping (SWS) unit and entered
Row processing, the waste heat of cooling procedure is used to produce low-pressure steam or preboiler feedwater, by directly or indirectly heating sour water vapour
The reactor of bill of lading member and simultaneously addition caustic soda separate the sour gas condensed in acidic liquid, then that sour gas is defeated
Sulfur cream unit is delivered to, by H2S changes into sulphur.
4. the method that utilization underground coal gasification(UCG) product gas according to claim 1 produces synthetic natural gas, its feature exists
In：Step（4）Middle acid gas removal unit uses low-temp methanol to wash the physical solvent adsorption technology with SELEXOL techniques,
The solvent rich in sour gas for leaving absorption tower bottom is sent in regeneration reactor, and desolvation is stripped by low-pressure steam
The H of absorption2S, then converts it into sulphur, is handled by multi-step pressure reduction and nitrogen stripping, will be with H2S together absorbed two
Carbonoxide is removed from solvent.
5. the method that utilization underground coal gasification(UCG) product gas according to claim 1 produces synthetic natural gas, its feature exists
In：Step（2）The coal tar of acquisition, into coal tar processing unit, by distill by coal tar be divided into coal tar naphtha and
Coal tar distillate, then by removing the sulphur of residual to coal tar naphtha hydrotreating, the coal tar oilstone brain after desulfurization
Oil is delivered to pre-reforming unit, and gas stream of the production rich in methane is simultaneously delivered to self-heating recapitalization unit, in self-heating recapitalization unit,
The gas stream rich in methane is reformed using carbon dioxide or steam and oxygen, self-heating recapitalization unit synthesis gas and dry synthesis
Gas enters acid water gas conversion after being mixed with suitable proportion and cooling unit carries out subsequent treatment.
6. the method that utilization underground coal gasification(UCG) product gas according to claim 5 produces synthetic natural gas, its feature exists
In：H in steam self-heating recapitalization product gas2:CO stoichiometric proportions are 2.5:1, the H in carbon dioxide self-heating recapitalization product gas2:CO
Stoichiometric proportion is 1:1.
7. the method that utilization underground coal gasification(UCG) product gas according to claim 1 produces synthetic natural gas, its feature exists
In：Step（3）Dry synthesis gas, is firstly transferred to acid gas removal cell processing, the entrance of the acid gas removal unit
Place includes COS hydrolysis units, and in the porch of self-heating recapitalization unit, dry synthesis gas is removed by a catalyst protection reactor
Residual impurity is removed, to protect self-heating recapitalization unit catalyst and downstream methanation catalyst, then synthesis gas enters self-heating recapitalization
Unit, the production of the high methane content of the oxygen produced with air-separating plant, the steam of boiler for producing and pre-reforming unit production
Product solid/liquid/gas reactions, produce self-heating recapitalization unit synthesis gas, afterwards, self-heating recapitalization unit synthesis gas enters back into Water gas shift/WGS and cooling
Unit, the H needed for adjustment methanation unit2:CO stoichiometric proportions.
8. the method that utilization underground coal gasification(UCG) product gas according to claim 7 produces synthetic natural gas, its feature exists
In：The process water of self-heating recapitalization unit generation, is delivered to recycling after process water processing unit processes, excessive titanium dioxide
Carbon is removed by decarburization unit, and the decarbonization process used includes chemisorbed, physical absorption, adsorbent bed, absorption regeneration method, low
Warm partition method or membrane separation process.
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108485722A (en) * | 2018-03-12 | 2018-09-04 | 崔静思 | The device and method that mercury recycles in a kind of coal gasification course |
| CN110628478A (en) * | 2019-09-20 | 2019-12-31 | 成都聚实节能科技有限公司 | Method for co-producing fuel oil aromatic hydrocarbon by coal-based natural gas through pressurized moving bed |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2010067077A1 (en) * | 2008-12-11 | 2010-06-17 | Bp P.L.C. | Integrated gas refinery |
| AU2012101312A4 (en) * | 2011-12-23 | 2012-09-27 | Linc Energy Ltd | Apparatus and method for syngas processing |
| CN102977959A (en) * | 2012-12-10 | 2013-03-20 | 中国五环工程有限公司 | Technology for producing natural gas through underground coal gasification |
| CN106433828A (en) * | 2016-10-26 | 2017-02-22 | 中石化宁波工程有限公司 | Method for preparing natural gas through straw gasification |
-
2017
- 2017-05-03 CN CN201710304488.0A patent/CN107099348A/en active Pending
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2010067077A1 (en) * | 2008-12-11 | 2010-06-17 | Bp P.L.C. | Integrated gas refinery |
| AU2012101312A4 (en) * | 2011-12-23 | 2012-09-27 | Linc Energy Ltd | Apparatus and method for syngas processing |
| CN102977959A (en) * | 2012-12-10 | 2013-03-20 | 中国五环工程有限公司 | Technology for producing natural gas through underground coal gasification |
| CN106433828A (en) * | 2016-10-26 | 2017-02-22 | 中石化宁波工程有限公司 | Method for preparing natural gas through straw gasification |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108485722A (en) * | 2018-03-12 | 2018-09-04 | 崔静思 | The device and method that mercury recycles in a kind of coal gasification course |
| CN110628478A (en) * | 2019-09-20 | 2019-12-31 | 成都聚实节能科技有限公司 | Method for co-producing fuel oil aromatic hydrocarbon by coal-based natural gas through pressurized moving bed |
| CN110628478B (en) * | 2019-09-20 | 2023-11-21 | 成都聚实节能科技有限公司 | Method for preparing natural gas and co-producing fuel aromatic hydrocarbon by using pressurized moving bed coal |
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Application publication date: 20170829 |