CN105802672A - Method for production of 1.0-2.2MPa water gas by fixed bed gasification - Google Patents
Method for production of 1.0-2.2MPa water gas by fixed bed gasification Download PDFInfo
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/02—Fixed-bed gasification of lump fuel
- C10J3/06—Continuous processes
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/02—Fixed-bed gasification of lump fuel
- C10J3/20—Apparatus; Plants
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/02—Fixed-bed gasification of lump fuel
- C10J3/20—Apparatus; Plants
- C10J3/30—Fuel charging devices
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/72—Other features
- C10J3/723—Controlling or regulating the gasification process
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/72—Other features
- C10J3/74—Construction of shells or jackets
- C10J3/76—Water jackets; Steam boiler-jackets
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/72—Other features
- C10J3/82—Gas withdrawal means
- C10J3/84—Gas withdrawal means with means for removing dust or tar from the gas
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0913—Carbonaceous raw material
- C10J2300/093—Coal
- C10J2300/0933—Coal fines for producing water gas
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0953—Gasifying agents
- C10J2300/0959—Oxygen
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0953—Gasifying agents
- C10J2300/0973—Water
- C10J2300/0976—Water as steam
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/16—Integration of gasification processes with another plant or parts within the plant
- C10J2300/1603—Integration of gasification processes with another plant or parts within the plant with gas treatment
- C10J2300/1615—Stripping
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/18—Details of the gasification process, e.g. loops, autothermal operation
- C10J2300/1807—Recycle loops, e.g. gas, solids, heating medium, water
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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
Abstract
The invention belongs to the field of coal and coke chemical gasification and discloses a method for production of 1.0-2.2MPa water gas by fixed bed gasification. The method includes steps: adding feed coal and/or coke into a gasification furnace; feeding oxygen and steam into the gasification furnace, wherein the oxygen is 1.2-2.4MPa in pressure, concentration of the oxygen is larger than or equal to 99.6%, and the steam is 240-270 DEG C in average temperature and 1.2-2.2MPa in pressure; controlling the gasification furnace to be 1100-1250 DEG C in internal temperature and 1.0-2.2MPa in pressure, reacting to generate crude gas, washing and cooling to obtain the water gas. The supply quantity of the feed coal and/or coke is 380-420kg per kNm<3> of gas, the oxygen feeding quality is 190-220Nm<3> per kNm<3> of gas, and the steam feeding quantity is 600-650Nm<3> per kNm<3> of gas. By the method for production of 1.0-2.2MPa water gas by fixed bed gasification, the conversion rate of the feed coal and/or coke can be increased to further increase the content of effective ingredients in the gas, and the water gas produced according to the method can be directly sent to a conversion section without compression, so that remarkable energy saving and consumption reduction effects are achieved.
Description
Technical field
The present invention relates to a kind of method that fixed bed gasification produces 1.0～2.2MPa water gas, belong to coal, coke chemical field of gasification.
Background technology
Coal gasification reaction is to occur at the gasifying agent (O of carbon and oxygen carrier2、H2O、CO2) between a kind of chemical reaction.Widely, its Main Ingredients and Appearance is hydrogen and carbon monoxide to water gas purposes, is mainly used as combustion gas in the past, is primarily now used for preparing chemical products, as the unstripped gas producing methanol, ethylene glycol, polyhydric alcohol, acetic acid, synthesis ammonia, connection alkali etc..
Existing more than 100 year of the developing history of Coal Gasification Technology, gasification furnace type successively also has nearly hundred kinds, and China also attaches great importance to the research and development of Coal Gasification Technology, relies on self scientific and technological strength to develop multiple fixing bed, fluid bed and entrained flow bed gasification technology.But, domestic at present middle-size and small-size fertilizer enterprises, smeltery, Metal Processing Factory, Foundry Works, ceramics factory, glass factory etc. are most still adopts old-fashioned coal gasifier, i.e. fixed bed atmospheric pressure batch furnace, during use, coal gas needs pressurization, power consumption is higher, and this production efficiency is low, feed stock conversion is low, lime-ash carbon residue high, potential safety hazard is many, causes enterprise's production cost to raise, and economic benefit reduces.
For increasing economic efficiency, China successively introduces Winkler fluidization the 1950's, introduces the strange fixed bed gasification technology in Shandong the seventies, introduces Texaco's pressure (hydraulic) water coal slurry gasification technology the eighties, introduce the nineties such as shell coal dust gasification technology etc..But every kind of Coal Gasification Technology has adaptability and the limitation of self, as different raw material sources need the corresponding different type of furnaces etc..And external gasification furnace great majority are only applicable to large-size chemical manufacturing enterprise, up-front investment is relatively big, and general enterprises is difficult to bear.
For regulating gas componant, middle-size and small-size chemical fertilizer manufacturing enterprise is provided with CO Varying Process, conversion pressure mainly has 0.8～1.0MPa, 2.0～2.2MPa two kinds, and the water at atmospheric pressure coal gas that batch furnace produces must utilize gas compression pump to be pressurized to above-mentioned pressure could to use, it is thus desirable to consume substantial amounts of electric energy, power consumption expense accounts for nearly the 30% of ammonia cost, is unfavorable for reducing production cost.Enjoying preferential electricity price at past chemical fertilizer production business electrical, and this preferential policy all will be cancelled before in June, 2016, this will bring baptism to enterprise.But the vapor pressure of large-scale gasification furnace such as lurgi gasifier, Texaco, shell, space flight stove, Tsing-Hua University's stove, section's woods stove etc. is all at more than 4.0MPa, and the pressure of fixed bed atmospheric pressure batch furnace is less than 0.01MPa.If the water gas pressure that gasification furnace is produced can be made to maintain 1.0～2.2MPa scope, can not only meeting CO change pressure needs, power consumption is greatly reduced, other consumptions of materials also can decrease simultaneously.And, 1.0～2.2MPa middle gear press water coal gas is also had the demand in production by the enterprises such as metallurgy, pottery, papermaking, building materials, these enterprises adopt natural gas in the past, and production cost is higher, and waiting the cost of water gas in calorific value situation is only about the 1/2 of gas cost.
The patent of invention of publication number CN104673390A discloses a kind of high-temperature coke direct gasification technique, including: 1) entered high-temperature coke tank with the high-temperature coke without quenching by coke oven coke-pusher, deliver to winding shaft by tractor and be promoted to gasification furnace roof by elevator；2) high-temperature coke tank is opened discharge gate by the high temperature storage bin para-position of automatic decimal alignment system and furnace roof portion simultaneously and high-temperature coke is automatically fallen into storage bin, storage bin is provided simultaneously with storing, the reinforced function of disintegrating machine, can realize self-timing and quantitatively be added in stove by coke；3) the oxidant oxygen of gas processed is from space division operation, oxygen concentration requires arbitrarily to select in 40%～100% scope according to rear operation gas, steam is from boiler and self-produced steam, oxygen and gasifying agent enter mixing in blending tank, Gas-making Furnace is entered from bottom, when furnace high-temperature, carry out redox reaction with high-temperature coke, produce water gas continuously；4) water gas that reaction generates is discharged from furnace roof, carries out after dedusting through hot precipitator, enters waste heat boiler and reclaims high-temperature gas waste heat, the steam of by-product pressure 0.4～3.9MPa；5) water gas going out waste heat boiler temperature 80～160 DEG C enters bottom aeration tower, tower cools down washing by the closed cycle cool water shower from wastewater treatment system, after being cooled to 40～45 DEG C and washing the dust wherein carried secretly, enter gas main and go to follow-up workshop section, the gas making sewage discharged at the bottom of tower drains into wastewater treatment system by trench, and recirculated cooling water after treatment is used by pumped back gas making gasification system closed cycle.The method utilizes the temperature of high-temperature coke to form integral high-temperature district in gasification furnace, is beneficial to the carrying out of gasification reaction, can produce the coal gas of high effective ingredient, and reduce the consumption of carbon and gasifying agent.But this reaction carries out at ambient pressure, the water gas of output need to send to follow-up workshop section after gas compression pump compresses.
Summary of the invention
It is an object of the invention to provide a kind of method that fixed bed gasification produces 1.0～2.2MPa water gas, the method can improve the conversion ratio of feed coal and/or coke, increases active constituent content in coal gas, and water produced coal gas is without compression, can being routed directly to conversion section, energy conservation and consumption reduction effects is notable.
In order to realize object above, the technical solution adopted in the present invention is:
Fixed bed gasification produces the method for 1.0～2.2MPa water gas, comprise the following steps: feed coal and/or coke are added in gasification furnace, pressure 1.2～2.4MPa, the oxygen of concentration >=99.6% and the steam of mean temperature 240～270 DEG C, pressure 1.2～2.4MPa are passed in gasification furnace simultaneously, control gasification in-furnace temperature 1100～1250 DEG C, pressure 1.0～2.2MPa, reaction generates raw gas, washing, cooling, to obtain final product；The quantity delivered of described feed coal and/or coke is 380～420kg/kNm3Coal gas, oxygen intake is 190～220Nm3/kNm3Coal gas, steam intake is 600～650kg/kNm3Coal gas.
Described oxygen, steam (entering stove) pressure higher than gasification furnace pressure about 0.2MPa, in order to material enters stove smoothly.(entering stove) temperature of steam is higher than saturation temperature 40～50 DEG C under corresponding pressure, to avoid the generation of condensed water.
The charge door of described gasification furnace is connected with coal lock hopper, and feed coal and/or coke are by, after Belt Conveying to feed bin, joining in coal lock hopper, and coal lock hopper carries out pressurising process, and (pressurising medium is CO2), to pressure slightly above gasification furnace pressure, subsequently feed coal and/or coke by charge door enter in stove with gasifying agent generation redox reaction.Reinforced complete, coal lock hopper is carried out pressure release process, after pressure release gas removing dust, is directly discharged into air, alternative coal lock gas recovery system, and then simple flow, minimizing investment, raising gas producing efficiency, finally realize energy-saving and cost-reducing.
Described oxygen, steam can pass into the form of gaseous mixture.Wherein oxygen is from space division workshop section, pressurization (to 1.5～2.7MPa, 80 DEG C) by regulating valve regulating flow (1.2～2.4MPa, 80 DEG C), enter back in oxygen/steam mixer.Steam is made up of exogenous steam and endogenous steam two parts, exogenous steam supplies official website from factory or is the boiler of gasification system separate configurations, such as the superheated steam (1.8～3.0MPa, 320～350 DEG C, press through vapours in namely) from boiler gas transmission pipeline net work.There is the endogenous steam (such as the saturated vapor of heat exchange drum by-product, 1.1～2.3MPa, 184～219 DEG C) of by-product after heat exchange in endogenous steam and cooling water and gasification furnace furnace wall.Described oxygen first mixes with exogenous steam, and mixed gas passes in gasification furnace with endogenous steam again, with the feed coal in stove and/or coke generation redox reaction.Concrete, oxygen mixes in oxygen/steam mixer with exogenous steam elder generation, mixed gas after spark arrester with endogenous steam.
In gasification furnace, main chemical reactions formula is shown in formula 1)～5):
1)C+O2=CO2+Q；
2)2C+O2=2CO+Q；
3)C+CO2=2CO-Q；
4)C+2H2O (g)=CO2+2H2-Q；
5)C+H2O (g)=CO+H2-Q。
Described gasification furnace includes body of heater and is located at outside body of heater in order to realize the heat exchange structure of body of heater heat exchange, described heat exchange structure is connected with heat exchange drum, after cooling water, with gasification furnace furnace wall, heat exchange occurs, then in heat exchange drum, carry out steam-water separation, endogenous steam described in by-product.Heat exchange drum is mainly gasification furnace and provides cooling water, simultaneously by-product middle pressure steam.The heat exchange structure of gasification furnace includes the cylinder heat exchange structure be located at outside cylinder and is located at heat exchange structure at the bottom of the cone outside Failure of Gasifier Conical Bottom.When described redox reaction carries out, from pipe network come boiler feedwater (1.8～3.0MPa, 104 DEG C, i.e. desalination deaerated water) enter in Failure of Gasifier Conical Bottom heat exchange structure by pipeline, reduce bottom temperature on the one hand, prevent that ash temperature is too high causes furnace bottom overtemperature, affect equipment intensity, on the other hand boiler water is preheated (to temperature about 112.5 DEG C).Boiler water after preheating enters heat exchange drum moisturizing, drum water after moisturizing enters back into gasification furnace cylinder heat exchange structure and carries out heat exchange, heat exchange drum is returned after absorbing the partial heat of gasification furnace furnace wall, heat exchange drum carries out steam-water separation, and the endogenous steam of by-product (1.1～2.3MPa, 184～219 DEG C, i.e. saturated vapor).
The gas outlet of described gasification furnace is connected with Venturi scrubber, the raw gas (1.0～2.2MPa, temperature 450～500 DEG C) that gasification reaction produces from gas outlet out after, enter in Venturi scrubber and carry out being humidified, wash and cooling processes.In scrubber, slurry is provided by circulating water for gasification pipe network, enters Venturi scrubber (temperature≤45 DEG C) after intensified process.Venturi scrubber is connected with gas washing separator, enters gas washing separator from Venturi scrubber water gas (temperature about 250 DEG C) out and carries out gas-water separation.The top of gas washing separator is provided with spray equipment and packing layer, and water gas enters in gas washing separator, and after secondary washing and cooling process, (temperature is down to 200 DEG C) sends battery limit (BL).In separator, spray-water is provided by circulating water for gasification pipe network equally, scrubbed, cooling after water (temperature about 85 DEG C) enter trench from the bottom of gas washing separator, go to circulating water for gasification and process system, after the measures such as sedimentation, cooling process, enter back in circulating water for gasification pipe network, be pumped into Venturi scrubber and the use of gas washing separator internal recycle through circulating water for gasification.
The ash hole of described gasification furnace is connected with ash lock hopper, and the lime-ash that gasification reaction produces is broken through fire grate, rotation is scraped in laggard ash charge lock hopper, ash lock hopper is carried out steam pressurising and the pressure release that adds water processes, and utilizes pressurising, pressure discharge operations to realize the ash discharge of ash lock hopper is processed.Waste water after process is gone to circulating water for gasification and is processed system, can be directly discharged into air after waste gas removing dust.Pressurising steam (1.8～3.0MPa, 320～350 DEG C, press through vapours in namely), from boiler gas transmission pipeline net work, lets out hydraulic water from circulating water for gasification pipe network.
Beneficial effects of the present invention:
In the present invention, gasification furnace adopts steam intensification-oxygen igniting driving technology, improve lurgi gasifier steam intensification-air ignition-oxygen driving technology, startup procedure and related process flow process can be simplified, reduce air driving equipment pipe and investment, shorten the driving time, reduce the discharge gas pollution to environment that goes into operation, increase the safety of operation of driving.Further, in reaction by-product, pressure saturated vapor is incorporated to middle pressure steam pipe network through high-order drum, mixes with external superheated steam and is used as gasification furnace gasifying agent, can reduce fresh middle pressure steam consumption.Meanwhile, the buck that gasification system produces recycles, can simple flow, go out workshop section coal gas water saturation high, downstream transforms workshop section maybe can add steam less without adding steam again, small investment, consume energy low.Due to gas ash water circulation use, wherein most water-soluble gas such as ammonia (NH3), hydrocyanic acid (HCN), hydrogen sulfide (H2Etc. S) taken out of by raw gas stripping, make harmful gas contained by buck be greatly reduced.Further, the lime-ash after gasification adopts hydraulic slag discharging method punching ash, and workload is little, and operating environment is clean and tidy, and is easy to operation maintenance, is better than other method for discharging residue.
Fixed bed gasification of the present invention produces the method for 1.0～2.2MPa water gas and has the advantage that 1) adjustment reaction of coal is wide, smokeless small coal, brown coal, bituminous coal, metallurgical coke, chemical industry Jiao, semi-coke, semicoke can be burnt, it is possible to burn the coal rod or coal briquette be made up of fine coal；2) coal combustion is thorough, and charcoal conversion ratio is high, and unit coal consumption is low, operation gasification below ash fusion point, and unit oxygen consumption is low, relative batch furnace, Texaco's water-coal slurry furnace, shell powder coal stove steam decomposition rate high；3) on-the-spot clean hygiene, noiseless, without waste water and toxic emission, slag can be used for making cement or hollow brick, without environmental issue, meets national industrial policies；4) coal gas effective ingredient (includes CO, H2And CH4) content height, calorific value of gas is high；5) water gas enters that temperature before conversion section is high, moisture content is high, and conversion energy consumption is low, and without carrying out transformation process, energy conservation and consumption reduction effects is notable, ton ammonia power consumption more than decline 400kWh.
Accompanying drawing explanation
Fig. 1 is the structural representation of water gas two-stage gasifier system in embodiment；
Fig. 2 is water gas two-stage gasifier process flow diagram in embodiment.
Detailed description of the invention
The present invention is only described in further detail by following embodiment, but does not constitute any limitation of the invention.
Embodiment 1
The method that fixing bed pure oxygen continuous gasification produces 2.0MPa water gas, comprises the following steps:
By smokeless small coal (analysis indexes is shown in table 1 below) (383kg/kNm3Coal gas) add in gasification furnace, simultaneously by the oxygen (202Nm of pressure 2.2MPa3/kNm3Coal gas) and the exogenous steam (330kg/kNm of temperature 350 DEG C, pressure 2.2MPa3Coal gas) and the endogenous steam of temperature 215 DEG C, pressure 2.1MPa passes in gasification furnace, and (it is 633kg/kNm that steam passes into total amount3Coal gas), control gasification in-furnace temperature 1100～1200 DEG C, pressure 2.0MPa (pressure measurement of furnace roof portion), reaction generates the raw gas of temperature about 470 DEG C, and raw gas is scrubbed, cooling, obtains the water gas that temperature is 200 DEG C cleaner.
As it is shown in figure 1, water gas two-stage gasifier system includes gasification furnace 7 in the present embodiment, the charge door of gasification furnace 7 is connected with coal lock hopper 6, and ash hole is connected with ash lock hopper 8.Time reinforced, smokeless small coal elder generation to feed bin by Belt Conveying, is then added in coal lock hopper 6, utilizes CO2(by CO2Storage tank 15 supplies) or in press through vapours coal lock hopper 6 carried out pressurising process, maintenance pressure is 2.1MPa, slightly above pressure in gasification furnace 7 (furnace pressure 2.0MPa).Smokeless small coal is entered in stove by charge door subsequently, with gasifying agent generation redox reaction.Reinforced complete, coal lock hopper 6 is carried out pressure release process, after pressure release gas removing dust, is directly discharged into air.
Described gasifying agent is oxygen and steam, in the present embodiment, oxygen from space division workshop section 1, first through oxygen compressor be forced into 2.5MPa, 80 DEG C send into gasification battery limit (BL)s, enter in oxygen/steam mixer 4 then through (2.2MPa, 80 DEG C) after regulating valve regulating flow.The a part of steam of steam from boiler gas transmission pipeline net work 2, in press through vapours (3.0MPa, 350 DEG C), be adjusted after valve is decompressed to 2.2MPa and enter in oxygen/steam mixer 4.This tow channel gas mixes in oxygen/steam mixer, mixed gas is incorporated to furnace bottom inlet manifold through spark arrester, with middle pressure steam (namely the endogenous steam of by-product in heat exchange drum 9,2.1MPa, 215 DEG C) together enter in gasification furnace 7, with the smokeless small coal generation redox reaction in stove.In Fig. 1, Ling You mono-road middle pressure steam is directly entered in gasification furnace through ring pipe, and this road steam also serves as gasifying agent and uses, and when there is serious overtemperature in order to quickly to regulate the temperature of gasification layer, but relative usage is less, also infrequently use, can not calculate.
Described gasification furnace 7 includes body of heater and is located in order to realize the heat exchange structure of body of heater heat exchange outside body of heater, and heat exchange structure is connected with heat exchange drum 9, and heat exchange drum 9 is mainly gasification furnace and carries Cooling Water, simultaneously the endogenous steam of by-product.nullThe heat exchange structure of gasification furnace includes the cylinder heat exchange structure be located at outside gasification furnace cylinder and is located at heat exchange structure at the bottom of the cone outside Failure of Gasifier Conical Bottom，When in stove, gasification reaction carries out，From the desalination deaerated water (3.0MPa of boiler water supply pipe network 3、104 DEG C) it is adjusted valve and is introduced in Failure of Gasifier Conical Bottom heat exchange structure，Reduce bottom temperature on the one hand，Prevent that ash temperature is too high causes furnace bottom overtemperature，Affect equipment intensity，On the other hand boiler water is preheated，To temperature about 112.5 DEG C，Boiler water after preheating enters moisturizing in heat exchange drum 9，Drum water after moisturizing enters back in gasification furnace cylinder heat exchange structure and carries out cooling heat transferring，Saturation water is formed after absorbing the partial heat of gasification furnace furnace wall，Return in heat exchange drum 9 and carry out steam-water separation，By-product pressure 2.1MPa、The middle pressure saturated vapor of temperature 215 DEG C.The lime-ash produced in stove is discharged by ash hole, and, rotation broken through fire grate is scraped in laggard ash charge lock hopper 8.Ash lock hopper 8 is carried out steam pressurising and the pressure release that adds water processes, utilize pressurising, pressure discharge operations to realize the ash discharge of ash lock hopper 8 is processed.Wherein pressurising steam presses through vapours in being, from boiler gas transmission pipeline net work 2, lets out hydraulic water from circulating water for gasification pipe network 12, and the waste water after process is gone to circulating water for gasification and processed system 13, is directly discharged into air after waste gas removing dust.
The gas outlet of described gasification furnace 7 is connected with Venturi scrubber 10, the raw gas (2.0MPa, temperature about 470 DEG C) that in stove, gasification reaction produces from the gas outlet of gasification furnace 7 out after, enter humidification in Venturi scrubber 10, washing and cooling.Slurry in Venturi scrubber 10 is provided by circulating water for gasification pipe network 12, enters in scrubber (temperature≤45 DEG C) after the intensified process of water.
Described Venturi scrubber 10 is also connected with gas washing separator 11, enters in gas washing separator 11 from scrubber's water gas (temperature about 250 DEG C) out and carries out gas-water separation.The top of gas washing separator 11 is provided with spray equipment and packing layer, and the washing of scrubbed device, the water gas cooled down enter in separator, are cooled to 200 DEG C after secondary washing and cooling process, and send battery limit (BL) and enter next workshop section 16.In separator, spray-water is provided by circulating water for gasification pipe network 12 equally, scrubbed, cooling after water (temperature about 85 DEG C) enter trench from the bottom of gas washing separator 11, go to circulating water for gasification and process system 12, after the measures such as sedimentation, cooling process, enter back in circulating water for gasification pipe network, send into through circulating water for gasification pump 14 in Venturi scrubber 10 and gas washing separator 11 and recycle.
The water gas composition that the present embodiment produces is shown in table 2 below, and gasification reaction consumption indicators is shown in table 3 below, and process chart is shown in Fig. 2.The few (≤0.2kg/KNm of stove carry-over3Water gas), lime-ash carbon residue low (≤3%).
The analysis indexes (average) of the smokeless small coal of table 1
Table 2 burns the water gas composition (average) of smokeless small coal
| Composition | CO2 | CO | H2 | N2 | O2 | CH4 | H2+CO |
| Content % | 17.1 | 37.2 | 41.9 | 0.2 | 0.3 | 3.3 | >=79% |
Table 3 gasification reaction consumption indicators (average)
| Project | Index |
| Unpurifed gas/kg coal | 2.611Nm3/ kg coal |
| Oxygen consumption gas/kg coal | 0.527Nm3/ kg coal |
| Consumption steam/kg coal | 1.653kg/kg coal |
| Consumption coal/Nm3Coal gas | 0.383kg |
| Oxygen consumption gas/Nm3Coal gas | 0.202Nm3 |
| Consumption steam/Nm3Coal gas | 0.633kg (containing self-produced) |
Embodiment 2
The method that fixing bed pure oxygen continuous gasification produces 2.0MPa water gas, comprises the following steps:
By granule coke (analysis indexes is shown in table 4 below) (411kg/kNm3Coal gas) add in gasification furnace, simultaneously by the oxygen (219Nm of pressure 2.2MPa3/kNm3Coal gas) and the exogenous steam (302kg/kNm of temperature 350 DEG C, pressure 2.2MPa3Coal gas) and the endogenous steam of temperature 215 DEG C, pressure 2.1MPa passes in gasification furnace, and (it is 602kg/kNm that steam passes into total amount3Coal gas), control gasification in-furnace temperature 1100～1200 DEG C, pressure 2.0MPa (pressure measurement of furnace roof portion), reaction generates the raw gas of temperature about 480 DEG C, and raw gas is scrubbed, cooling, obtains the water gas that temperature is 200 DEG C cleaner.Water gas two-stage gasifier system is with embodiment 1, and water gas composition is shown in table 5 below, and gasification reaction consumption indicators is shown in table 6 below.The few (≤0.2kg/KNm of stove carry-over3Water gas), lime-ash carbon residue low (≤3%).
The analysis indexes (average) of table 4 granule coke
Table 5 burns the water gas composition (average) of granule coke
| Composition | CO2 | CO | H2 | N2 | O2 | CH4 | H2+CO |
| Content % | 18.9 | 45 | 35 | 0.2 | 0.3 | 0.5～0.7 | >=80% |
Table 6 gasification reaction consumption indicators (average)
| Unpurifed gas/kg coke | 2.433Nm3/ kg coke |
| Oxygen consumption gas/kg coke | 0.533Nm3/ kg coke |
| Consumption steam/kg coke | 1.465kg/kg coke |
| Consumption coke/Nm3Coal gas | 0.411kg |
| Oxygen consumption gas/Nm3Coal gas | 0.219Nm3 |
| Consumption steam/Nm3Coal gas | 0.602kg (containing self-produced) |
Claims (10)
1. the method that fixed bed gasification produces 1.0～2.2MPa water gas, it is characterized in that: comprise the following steps: feed coal and/or coke are added in gasification furnace, pressure 1.2～2.4MPa, the oxygen of concentration >=99.6% and the steam of temperature 240～270 DEG C, pressure 1.2～2.4MPa are passed in gasification furnace simultaneously, control gasification in-furnace temperature 1100～1250 DEG C, pressure 1.0～2.2MPa, reaction generates raw gas, washing, cooling, to obtain final product；The quantity delivered of described feed coal and/or coke is 380～420kg/kNm3Coal gas, oxygen intake is 190～220Nm3/kNm3Coal gas, steam intake is 600～650kg/kNm3Coal gas.
2. method according to claim 1, it is characterized in that: the charge door of described gasification furnace is connected with coal lock hopper, first feed coal and/or coke are added in coal lock hopper, coal lock hopper is carried out pressurising process, maintained at higher than gasification furnace pressure, subsequently feed coal and/or coke are added in gasification furnace.
3. method according to claim 1, it is characterised in that: described steam is made up of exogenous steam and endogenous steam two parts, and exogenous steam is from gas transmission pipeline net work, and endogenous steam and cooling water absorb the steam of by-product after gasification furnace generation heat exchange.
4. method according to claim 3, it is characterized in that: described gasification furnace includes body of heater and is located at outside body of heater in order to realize the heat exchange structure of body of heater heat exchange, described heat exchange structure is connected with heat exchange drum, cooling water carries out steam-water separation after there is heat exchange with gasification furnace furnace wall in heat exchange drum, endogenous steam described in by-product.
5. method according to claim 4, it is characterised in that: described oxygen first mixes with exogenous steam, and mixed gas passes into gasification furnace with endogenous steam again.
6. method according to claim 4, it is characterized in that: described heat exchange structure includes being located at the cylinder heat exchange structure outside cylinder and is located at heat exchange structure at the bottom of the cone outside Failure of Gasifier Conical Bottom, when reaction carries out, external feedwater is introduced into cone end heat exchange structure preheating, feedwater after preheating enters moisturizing in heat exchange drum, drum water after moisturizing enters cylinder heat exchange structure and carries out heat exchange, returns in heat exchange drum and carry out steam-water separation after absorbing the partial heat of gasification furnace furnace wall.
7. method according to claim 1, it is characterised in that: the gas outlet of described gasification furnace is connected with Venturi scrubber, the raw gas that gasification reaction produces from gas outlet out after, enter in Venturi scrubber and carry out being humidified, wash and cooling processes.
8. method according to claim 7, it is characterised in that: described Venturi scrubber is connected with gas washing separator, enters from Venturi scrubber water gas out and carries out gas washing separator washing, cools down and gas-water separation processes.
9. method according to claim 8, it is characterized in that: described Venturi scrubber and in gas washing separator with water by circulating water for gasification pipe network supply, water after process is gone to circulating water for gasification and is processed system, enters back into after treatment in circulating water for gasification pipe network and recycles.
10. method according to claim 1, it is characterised in that: the ash hole of described gasification furnace is connected with ash lock hopper, and the lime-ash that reaction produces enters in ash lock hopper through fire grate, ash lock hopper is carried out steam pressurising and the pressure release that adds water processes to discharge coal ash.
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| CN107446626A (en) * | 2017-08-08 | 2017-12-08 | 北京众联盛化工工程有限公司 | A kind of coke pressurization continuous gasification production method |
| CN108913216A (en) * | 2018-08-06 | 2018-11-30 | 唐山科源环保技术装备有限公司 | The method for controlling the self-produced vapor superpressure discharge of gas generator |
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| CN114410352A (en) * | 2022-02-24 | 2022-04-29 | 安徽科达洁能股份有限公司 | Adjustable waste heat recovery device and method |
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| CN108913216A (en) * | 2018-08-06 | 2018-11-30 | 唐山科源环保技术装备有限公司 | The method for controlling the self-produced vapor superpressure discharge of gas generator |
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