CN104804774A - Method and device for preparing fuel gas by utilizing ash coal as raw material - Google Patents

Method and device for preparing fuel gas by utilizing ash coal as raw material Download PDF

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Publication number
CN104804774A
CN104804774A CN201510189127.7A CN201510189127A CN104804774A CN 104804774 A CN104804774 A CN 104804774A CN 201510189127 A CN201510189127 A CN 201510189127A CN 104804774 A CN104804774 A CN 104804774A
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temperature
unit
gas
ash
fuel gas
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CN104804774B (en
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裴培
王其成
吴道洪
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Shenwu Technology Group Corp Co Ltd
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Beijing Shenwu Environmental and Energy Technology Co Ltd
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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
    • C10J3/46—Gasification of granular or pulverulent flues in suspension
    • 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
    • C10J3/46—Gasification of granular or pulverulent flues in suspension
    • C10J3/463—Gasification of granular or pulverulent flues in suspension in stationary fluidised beds
    • 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
    • C10J3/46—Gasification of granular or pulverulent flues in suspension
    • C10J3/466—Entrained flow processes
    • 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
    • C10J3/46—Gasification of granular or pulverulent flues in suspension
    • C10J3/48—Apparatus; Plants
    • 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
    • C10J3/46—Gasification of granular or pulverulent flues in suspension
    • C10J3/48—Apparatus; Plants
    • C10J3/482—Gasifiers with stationary fluidised bed
    • 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
    • C10J3/46—Gasification of granular or pulverulent flues in suspension
    • C10J3/48—Apparatus; Plants
    • C10J3/485—Entrained flow gasifiers
    • 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
    • C10J3/46—Gasification of granular or pulverulent flues in suspension
    • C10J3/54—Gasification of granular or pulverulent fuels by the Winkler technique, i.e. by fluidisation
    • 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
    • C10J3/46—Gasification of granular or pulverulent flues in suspension
    • C10J3/54—Gasification of granular or pulverulent fuels by the Winkler technique, i.e. by fluidisation
    • C10J3/56—Apparatus; Plants
    • 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
    • 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
    • C10J3/80—Other features with arrangements for preheating the blast or the water vapour
    • 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
    • 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
    • C10J2300/0903—Feed preparation
    • C10J2300/0906—Physical processes, e.g. shredding, comminuting, chopping, sorting
    • 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
    • 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
    • C10J2300/0956—Air or oxygen enriched air
    • 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

Abstract

The invention relates to a method for preparing fuel gas by utilizing ash coal as a raw material, and further relates to a device for preparing the fuel gas by utilizing the ash coal as the raw material. The device comprises a pretreatment unit, a gasification gas-making unit, a high-temperature fuel gas dedusting unit, a high-temperature fuel gas afterheat recovering unit, a fuel gas dedusting unit, a fuel gas cooling unit and a fuel gas desulfurizing unit which are sequentially connected with one another, and further comprises a high-temperature fuel gas ash residue recovering unit. The method and the device have the advantages that through technologies such as sufficient recovering of gasification residues, multi-stage utilization of high-temperature gas heat and two-stage gasifiers, the problem that the ash coal raw material adaptability of the conventional fuel gas preparation technology is poor can be solved; meanwhile, the cost can be reduced, pollutant emission can be reduced, the energy utilization rate and system heat efficiency are improved, and then such an inferior resource like the ash coal can be efficiently utilized on a large scale.

Description

A kind of take dirty coal as the method and apparatus that combustion gas prepared by raw material
Technical field
The present invention relates to combustion-gas jet test field, be specifically related to high coal ash as the method and apparatus of combustion gas prepared by raw material.
Background technology
China is coal production big country of the world, produces coal more than 1,000,000,000 tons per year.Coal is the main energy sources of China and important industrial chemicals.In China's coal, ash oontent is general higher, and change greatly, spy's low culm whole nation that ash content is less than 10% only accounts for about 17% of proven reserve, and obviously improve the utilization ratio of coal resources, especially the national economy of utilization ratio to development China of ash coal is significant.But pit ash is high, traffic capacity and freight charges can be increased.When burning, ash content is higher, and thermo-efficiency is lower, and can increase smoke discharge amount and slag amount, the coal-fired pollution to air of aggravation.During coking, cleans ash is higher, and the ash content of coke is higher, and the coke ratio of ironmaking just increases, and the capacity factor of a blast furnace just reduces, and produces iron and reduces.If this part ash coal can be cleaned, efficiently, the clean gas that is converted into of low cost is used for industrial production or domestic fuel, to low-quality coal resources efficiency utilization, reduce environmental pollution and play positive promoter action.
Current gas maked coal technology mainly comprises fixed bed, fluidized-bed and entrained flow bed gasification technology.But utilize aspect for dirty coal (ash oontent >25%), with regard to current technology, air flow bed technology affects by factors such as slag tap and oxygen consumptions, also there is certain difficulty to the gasification of ash coal; Although pressurization static bed gasification technology can process dirty coal, but its homogeneity to bed, gas permeability requirements are higher, thus raw material range is limited, only can process the satisfactory block dirty coal of a part, such gasification needs to consume a large amount of chilled water simultaneously, increase sewage purification link containing material demands such as tar, phenol, ammonia in water, therefore increase investment and raw materials consumption.Although fluidized-bed gasification technology is not state-of-the-art gasification technology, vapor pressure does not increase yet, and is relatively applicable to utilizing dirty coal to prepare combustion gas.But still there is a series of problem in existing fluidized-bed gasification technology in process dirty coal process.As, ash oontent increases the heat increase that lime-ash fusing absorbs, and in order to ensure the smooth deslagging of vapourizing furnace and the heat balance maintaining vapourizing furnace, needs to increase oxygen amount to the more carbon atom that burns, therefore, and the oxygen consumption of gasification system and coal consumption increase.Under same gasification condition, ash content often increases by 1%, and oxygen consumption increases 0.7-0.8%, and coal consumption increases 1.3-1.5%.The sensible heat of dreg removing system lime-ash is got rid of with lime-ash, and this part heat cannot be recycled, and the increase of bed drain purge increases the thermosteresis of system, decreases high pressure steam output, and lime-ash Quench consumes the Quench water yield greatly simultaneously, aggravation lock hopper thermal load.Therefore, in raw coal, during ash content height, equipment maintenance cost, deslagging transport charge increase, thus increase enterprise's production cost and energy consumption.
Summary of the invention
The present invention is directed to above-mentioned dirty coal and utilize technical problem in process, propose to utilize dirty coal to prepare the method and apparatus of combustion gas, the abundant recovery system heat of the high feature of dirty coal self ash oontent can be utilized and then realize the object that dirty coal cleans, efficiently prepares purified gas.This technology has that adaptability to raw material is wide, treatment capacity is large, efficiency of carbon conversion and the feature such as high, the pollution-free energy consumption of thermo-efficiency is little, simple to operate, cost is low.
The object of the present invention is to provide a kind of is raw material with dirty coal, low cost, clean, the high efficiency method preparing combustion gas.The present invention passes through fully to reclaim residue after gasifying, high-temperature gas multi-stage heat utilizes technology and two-stage gasifier technology solves existing combustion gas technology of preparing to the problem of the bad adaptability of dirty coal raw material, can reduce costs simultaneously, decreasing pollution thing discharges, improve energy utilization rate and system thermal efficiency, and then realize extensive, the efficiency utilization of this resource inferior of dirty coal.
Specifically, said method comprising the steps of:
(I) get dirty coal, successively after broken and screening pre-treatment, obtain the gasified raw material that particle that particle diameter is greater than 6mm is less than total amount 3%;
(II) gasified raw material is under the effect of vaporized chemical, carries out one-level, secondary pyrolytic gasification successively, obtains high-temperature fuel gas and hot lime-ash;
Hot lime-ash and softening cold water carry out heat exchange, obtain water at low temperature; After lime-ash after heat exchange is further cooled to room temperature, obtain cold lime-ash;
(III) high-temperature fuel gas is carried out high-temperature dust removal, remove flying dust, obtain the high-temperature fuel gas of primary purification;
(IV) high-temperature fuel gas of primary purification is carried out Multi-stage heat exchange with air at room temperature, saturation steam, high-temperature water and water at low temperature successively, obtain low temperature combustion gas;
After the high-temperature fuel gas of described primary purification and air at room temperature carry out heat exchange, also obtain high temperature air, use as the described vaporized chemical of step (II);
Meanwhile, the described Multi-stage heat of the reverse participation of step (II) gained water at low temperature exchanges, and obtains high-temperature water, saturation steam and superheated vapour successively, and described superheated vapour uses as the described vaporized chemical of step (II);
(V) by after low temperature combustion gas removing fine solid particle, cooling, desulfurizing and purifying, clean combustion gas is obtained.
Step (II) high-temperature fuel gas of gained after two-stage pyrolytic gasification is gaseous state, and remaining lime-ash is solid-state, high-temperature fuel gas and lime-ash because of different in kind can natural separation.In described high-temperature fuel gas, be mixed with tiny solid granular dust, i.e. the flying dust of non-pyrolytic gasification, need through step (III), flying dust to be removed from high-temperature fuel gas.
Described method can also comprise the recycle to step (III) gained flying dust, is specially: flying dust is carried out gas processed again.
The temperature of step (II) described vaporized chemical is 500 ~ 650 DEG C; The temperature of described one-level pyrolytic gasification is 850 ~ 950 DEG C, and the temperature of secondary pyrolytic gasification is 950 ~ 1100 DEG C.
As a kind of preferred version, the temperature of step (II) described vaporized chemical is 650 DEG C; The temperature of described one-level pyrolytic gasification is 850 DEG C, and the temperature of secondary pyrolytic gasification is 950 ~ 1050 DEG C.
The described Multi-stage heat of step (IV) exchanges and is specially: the high-temperature fuel gas of primary purification is carried out Multi-stage heat exchange with the water at low temperature of air at room temperature, the saturation steam of 150 ~ 200 DEG C, the high-temperature water of 95 ~ 200 DEG C and 60 ~ 100 DEG C successively, and to be combustion gas, the temperature of 450 ~ 500 DEG C the be combustion gas of 250 ~ 300 DEG C that to obtain temperature be successively combustion gas, the temperature of 650 ~ 750 DEG C and temperature are the low temperature combustion gas of 150 ~ 200 DEG C.Simultaneously, the water at low temperature of step (II) gained 60 ~ 100 DEG C, the described Multi-stage heat of reverse participation step (IV) exchanges, obtain the high-temperature water of 95 ~ 200 DEG C, the saturation steam of 150 ~ 200 DEG C and the superheated vapour of 500 ~ 650 DEG C successively, described superheated vapour uses as the described vaporized chemical of step (II).
Meanwhile, the air of step (IV) described room temperature, after carrying out heat exchange with the high-temperature fuel gas of the primary purification of 950 ~ 1100 DEG C, also obtains the air of 500 ~ 650 DEG C, can be used as the pyrolytic gasification of vaporized chemical for step (II).
The described low temperature combustion gas cooling of step (V), for being cooled to 20 ~ 50 DEG C.
Present invention also offers a kind of take dirty coal as the device that combustion gas prepared by raw material, and described device comprises the pretreatment unit, gasification gas making unit, high-temperature fuel gas dust removing units, high-temperature fuel gas waste heat recovery unit, combustion gas dust removing units, combustion gas cooling unit and the gas desulfurization unit that are linked in sequence successively.
Described pretreatment unit comprises connected shredder assembly and screening plant.Shredder assembly is provided with the opening for feed of dirty coal.
Described gasification gas making unit comprises gas unit processed.Connected one-level gasifier and secondary gasifier is comprised in described gas unit processed; Described one-level gasifier is connected with screening plant.
Described high-temperature fuel gas dust removing units comprises high-temperature dust removal unit, and is connected with the secondary gasifier of gas unit processed.High-temperature cyclone dust extractor is comprised in high-temperature dust removal unit.According to the actual needs of dedusting, described high-temperature cyclone dust extractor can be the multistage of one-level or series connection, and progression is higher, and efficiency of dust collection is higher.
Described high-temperature fuel gas waste heat recovery unit comprises the air preheater, superheated vapour unit, saturation steam unit and the economizer that are linked in sequence successively.
Described combustion gas dust removing units comprises nonaqueous dust cleaner.
Described combustion gas cooling unit comprises indirect cooler.
Described gas desulfurization unit comprises desulfurizer, and described desulfurizer is provided with purified gas outlet.
Raw material dirty coal, successively after shredder assembly, screening plant, gas unit processed, high-temperature dust removal unit, air preheater, superheated vapour unit, saturation steam unit, economizer, nonaqueous dust cleaner, indirect cooler and desulfurizer, can obtain clean combustion gas.
In order to realize the recycle of waste material, high-temperature dust removal unit can also be connected with gas unit processed by flying dust circulating line, thus realizes the circulation pyrolytic gasification to flying dust.
In order to improve energy utilization rate and system thermal efficiency, air preheater can also arrange air inlet, and is connected with gas unit processed by air gasification agent pipeline.The air of room temperature is passed into air preheater, and after heat exchange, the warm air obtained as vaporized chemical, can pass into gas unit processed.
In order to improve energy utilization rate and system thermal efficiency, described device can further include high-temperature ash waste heat recovery unit, and described high temperature recrement waste heat recovery unit can comprise lime-ash cooling unit.
Described lime-ash cooling unit is provided with the outlet of cold lime-ash; Gas unit processed can also be connected with lime-ash cooling unit by lime-ash cooling duct.After lime-ash cooling, take out, the sustainable utilization of waste material can be realized.
Described lime-ash cooling unit also can arrange the water-in of softening cold water further, and by steam gasification agent pipeline, successively via economizer, saturation steam unit and superheated vapour unit, is connected with gas unit processed.
The method preparing clean fuel gas of the present invention, can adopt device provided by the invention to realize.
The method of the invention can more preferably:
(I) get dirty coal, successively after shredder assembly and screening plant pre-treatment, obtain the gasified raw material that particle that particle diameter is greater than 6mm is less than total amount 1%;
(II) step (I) gained gasified raw material is passed into gas unit processed, in gas unit processed, temperature is the one-level gasifier of 850 DEG C, under the effect of vaporized chemical, carry out pyrolysis; Gained pyrolysis gas and remaining solid material are together passed into the secondary gasifier that temperature is 950 ~ 1050 DEG C, fully gasifies under the effect of vaporized chemical, obtain the high-temperature fuel gas of 900 ~ 950 DEG C and the lime-ash of 920 ~ 980 DEG C;
Described lime-ash passes into lime-ash cooling unit by lime-ash cooling duct, carries out heat exchange with softening cold water wherein; After lime-ash cool to room temperature, take out, obtain cold lime-ash, transport outward and use as building materials;
(III) step (II) gained high-temperature fuel gas is passed into high-temperature dust removal unit, one or more levels high-temperature cyclone dust extractor in high-temperature dust removal unit, remove flying dust, obtain the high-temperature fuel gas that temperature is the primary purification of 900 ~ 950 DEG C;
Described flying dust passes into gas unit processed by flying dust circulating line, carries out circulation pyrolytic gasification;
(IV) high-temperature fuel gas of step (III) gained primary purification is passed into air preheater, carry out heat exchange with the air at room temperature in it, obtain the combustion gas that temperature is 750 DEG C; Pass into superheated vapour unit again, the saturation steam of interior with it 195 DEG C carries out heat exchange, obtains the combustion gas that temperature is 480 ~ 500 DEG C; Pass into saturation steam unit again, the high-temperature water of interior with it 95 ~ 100 DEG C carries out heat exchange, obtains the combustion gas that temperature is 280 ~ 300 DEG C; Pass into economizer again, the water at low temperature of interior with it 80 ~ 90 DEG C carries out heat exchange, obtains the combustion gas that temperature is 150 DEG C;
Meanwhile, the air of room temperature is passed into air preheater, after carrying out heat exchange with the high-temperature fuel gas of primary purification, obtain the air of 650 DEG C, pass into gas unit processed as vaporized chemical by air gasification agent pipeline;
Meanwhile, softening cold water is passed into lime-ash cooling unit, after heat exchange, obtain the water at low temperature that temperature is 80 ~ 90 DEG C; Described water at low temperature is by steam gasification agent pipeline, be warming up to 95 ~ 100 DEG C through economizer successively, form the saturation steam of 195 DEG C through supersaturated vapor unit again, again through the superheated vapour of superheated vapour unit formation 600 ~ 650 DEG C, described superheated vapour passes into gas unit processed as vaporized chemical;
(V) combustion gas being 150 DEG C by step (IV) gained temperature passes into nonaqueous dust cleaner, removing fine solid particle; Pass into indirect cooler again, obtain the combustion gas that temperature is 30 DEG C; Pass into desulfurizer again, after desulfurizing and purifying, obtain clean combustion gas.
In actual production process, above-mentioned steps is and continues to carry out.
The present invention is heated up by the heat fully reclaiming high-temperature ash and high-temperature fuel gas can effectively reduce gasification than coal consumption for vaporized chemical, improves system thermal efficiency, and then improves fuel gases calorific value and reduce combustion-gas jet test cost.
Present invention achieves excellent effect.Specifically, present invention achieves the object with dirty coal is extensive, low cost, clean and effective prepare combustion gas, gasification does not produce the pollutent such as tar and phenol water; The invention provides a kind of high-temperature fuel gas heat fully reclaim and obtain the apparatus and method of high temperature gasification agent, the Multi-stage heat-exchanging devices such as air preheater, superheated vapour unit, saturation steam unit, economizer are adopted fully to reclaim high-temperature gas heat on the one hand, improve system thermal efficiency, on the one hand air and steam gasification agent are preheating to comparatively high temps, the high ashy substance heat demand of gasification can be met and reduce than oxygen consumption with than coal consumption, and then reducing combustion gas cost; Because the grey quantity of slag after dirty coal gasification is larger, temperature is higher, carry a large amount of sensible heats, direct cooling causes very large waste, therefore, apparatus and method provided by the invention fully reclaim high-temperature ash, adopt ash cooling device that most of heat is passed to water at low temperature by the mode of indirect heat exchange, intensification water goes pre-thermogenesis superheated vapour as vaporized chemical further, further increases the thermo-efficiency of system and reduces combustion gas cost.
Accompanying drawing explanation
Fig. 1 is the schematic diagram of device described in embodiment 6; Wherein: 1, shredder assembly, 2, screening plant, 3, gas unit processed, 4, high-temperature dust removal unit, 5, air preheater, 6, superheated vapour unit, 7, saturation steam unit, 8, economizer, 9, nonaqueous dust cleaner, 10, indirect cooler, 11, desulfurizer, 12, lime-ash cooling unit; A, flying dust circulating line, b, air gasification agent pipeline, c, lime-ash cooling duct, d, steam gasification agent pipeline.
Embodiment
Following examples for illustration of the present invention, but are not used for limiting the scope of the invention.
Embodiment 1
Combustion gas is prepared according to following steps:
(I) get dirty coal, successively after broken and screening pre-treatment, obtain the gasified raw material that particle that particle diameter is greater than 6mm is less than total amount 1%;
(II) gasified raw material is under the vaporized chemical effect of 600 DEG C, carries out one-level pyrolytic gasification at 850 DEG C, then carries out secondary pyrolytic gasification at 1000 DEG C, obtains high-temperature fuel gas and lime-ash;
Meanwhile, gained lime-ash and softening cold water are carried out heat exchange, after lime-ash cool to room temperature, obtain cold lime-ash;
(III) high-temperature fuel gas is carried out high-temperature dust removal, remove flying dust, obtain the high-temperature fuel gas that temperature is the primary purification of 1000 DEG C;
Meanwhile, gained flying dust, as gasified raw material, carries out circulation pyrolytic gasification through step (II);
(IV) high-temperature fuel gas of primary purification and air at room temperature are carried out heat exchange, obtain the combustion gas that temperature is 700 DEG C; Carry out heat exchange with the saturation steam of 175 DEG C again, obtain the combustion gas that temperature is 480 DEG C; Carry out heat exchange with the high-temperature water of 150 DEG C again, obtain the combustion gas that temperature is 280 DEG C; Carry out heat exchange with the water at low temperature of 80 DEG C again, obtain the combustion gas that temperature is 180 DEG C;
After the high-temperature fuel gas of described primary purification and air at room temperature carry out heat exchange, also obtain the air of 600 DEG C, use as the described vaporized chemical of step (II);
Simultaneously, softening cold water and lime-ash are carried out the water at low temperature of gained 80 DEG C after heat exchange, heat exchange described in reverse this step of participation, obtain the high-temperature water of 150 DEG C, the superheated vapour of 175 DEG C of saturation steams and 600 DEG C successively, the superheated vapour of described 600 DEG C uses as the described vaporized chemical of step (II);
(V) by temperature be 180 DEG C combustion gas removing fine solid particle, be cooled to 30 DEG C, after desulfurizing and purifying, obtain clean combustion gas.
Embodiment 2
Combustion gas is prepared according to following steps:
(I) get dirty coal, successively after broken and screening pre-treatment, obtain the gasified raw material that particle that particle diameter is greater than 6mm is less than total amount 2%;
(II) gasified raw material is under the vaporized chemical effect of 500 DEG C, carries out one-level pyrolytic gasification at 850 DEG C, then carries out secondary pyrolytic gasification at 950 DEG C, obtains high-temperature fuel gas and lime-ash;
Meanwhile, gained lime-ash and softening cold water are carried out heat exchange, after lime-ash cool to room temperature, obtain cold lime-ash;
(III) high-temperature fuel gas is carried out high-temperature dust removal, remove flying dust, obtain the high-temperature fuel gas that temperature is the primary purification of 900 DEG C;
Meanwhile, gained flying dust, as gasified raw material, carries out circulation pyrolytic gasification through step (II);
(IV) high-temperature fuel gas of primary purification and air at room temperature are carried out heat exchange, obtain the combustion gas that temperature is 650 DEG C; Carry out heat exchange with the saturation steam of 150 DEG C again, obtain the combustion gas that temperature is 450 DEG C; Carry out heat exchange with the high-temperature water of 95 DEG C again, obtain the combustion gas that temperature is 250 DEG C; Carry out heat exchange with the water at low temperature of 60 DEG C again, obtain the combustion gas that temperature is 150 DEG C;
After the high-temperature fuel gas of described primary purification and air at room temperature carry out heat exchange, also obtain the air of 500 DEG C, use as the described vaporized chemical of step (II);
Softening cold water and lime-ash are carried out the water at low temperature of gained 60 DEG C after heat exchange, heat exchange described in reverse this step of participation, obtain the high-temperature water of 95 DEG C, the superheated vapour of 150 DEG C of saturation steams and 500 DEG C successively, the superheated vapour of described 500 DEG C uses as the described vaporized chemical of step (II);
(V) by temperature be 150 DEG C combustion gas removing fine solid particle, be cooled to 20 DEG C, after desulfurizing and purifying, obtain clean combustion gas.
Embodiment 3
Combustion gas is prepared according to following steps:
(I) get dirty coal, successively after broken and screening pre-treatment, obtain the gasified raw material that particle that particle diameter is greater than 6mm is less than total amount 3%;
(II) gasified raw material is under the vaporized chemical effect of 650 DEG C, carries out one-level pyrolytic gasification at 950 DEG C, then carries out secondary pyrolytic gasification at 1100 DEG C, obtains high-temperature fuel gas and lime-ash;
Meanwhile, gained lime-ash and softening cold water are carried out heat exchange, after lime-ash cool to room temperature, obtain cold lime-ash;
(III) high-temperature fuel gas is carried out high-temperature dust removal, remove flying dust, obtain the high-temperature fuel gas that temperature is the primary purification of 1100 DEG C;
Meanwhile, gained flying dust, as gasified raw material, carries out circulation pyrolytic gasification through step (II);
(IV) high-temperature fuel gas of primary purification and air at room temperature are carried out heat exchange, obtain the combustion gas that temperature is 750 DEG C; Carry out heat exchange with the saturation steam of 200 DEG C again, obtain the combustion gas that temperature is 500 DEG C; Carry out heat exchange with the high-temperature water of 200 DEG C again, obtain the combustion gas that temperature is 300 DEG C; Carry out heat exchange with the water at low temperature of 100 DEG C again, obtain the combustion gas that temperature is 200 DEG C;
After the high-temperature fuel gas of described primary purification and air at room temperature carry out heat exchange, also obtain the air of 650 DEG C, use as the described vaporized chemical of step (II);
Softening cold water and lime-ash are carried out the water at low temperature of gained 100 DEG C after heat exchange, heat exchange described in reverse this step of participation, obtain the high-temperature water of 200 DEG C, the superheated vapour of 200 DEG C of saturation steams and 650 DEG C successively, the superheated vapour of described 650 DEG C uses as the described vaporized chemical of step (II);
(V) by temperature be 200 DEG C combustion gas removing fine solid particle, be cooled to 50 DEG C, after desulfurizing and purifying, obtain clean combustion gas.
Embodiment 4
Take dirty coal as the device (part is with reference to figure 1) that combustion gas prepared by raw material, be linked in sequence successively by shredder assembly 1, screening plant 2, gas unit 3 processed, high-temperature dust removal unit 4, air preheater 5, superheated vapour unit 6, saturation steam unit 7, economizer 8, nonaqueous dust cleaner 9, indirect cooler 10 and desulfurizer 11 and form;
Described shredder assembly 1 is provided with dirty coal opening for feed;
Comprise connected one-level gasifier and secondary gasifier in described gas unit 3 processed, wherein, one-level gasifier is connected with screening plant 2, and secondary gasifier is connected with high-temperature dust removal unit 4;
High-temperature cyclone dust extractor is comprised in described high-temperature dust removal unit 4; High-temperature dust removal unit 4 is also connected with gas unit 3 processed by flying dust circulating line a;
Described air preheater 5 is provided with air inlet; Air preheater 5 is also connected with gas unit 3 processed by air gasification agent pipeline b;
Described desulfurizer 11 is provided with purified gas outlet.
Embodiment 5
Take dirty coal as the device (part is with reference to figure 1) that combustion gas prepared by raw material, be linked in sequence successively by shredder assembly 1, screening plant 2, gas unit 3 processed, high-temperature dust removal unit 4, air preheater 5, superheated vapour unit 6, saturation steam unit 7, economizer 8, nonaqueous dust cleaner 9, indirect cooler 10 and desulfurizer 11 and form; This device is also provided with lime-ash cooling unit 12;
Described shredder assembly 1 is provided with dirty coal opening for feed;
Comprise connected one-level gasifier and secondary gasifier in described gas unit 3 processed, wherein, one-level gasifier is connected with screening plant 2, and secondary gasifier is connected with high-temperature dust removal unit 4; Gas unit 3 processed is also connected with lime-ash cooling unit 12 by lime-ash cooling duct c, and lime-ash cooling unit 12 is provided with the outlet of cold lime-ash;
High-temperature cyclone dust extractor is comprised in described high-temperature dust removal unit 4; High-temperature dust removal unit 4 is also connected with gas unit 3 processed by flying dust circulating line a;
Described air preheater 5 is provided with air inlet; Air preheater 5 is also connected with gas unit 3 processed by air gasification agent pipeline b;
Described desulfurizer 11 is provided with purified gas outlet.
Embodiment 6
Take dirty coal as the device (as shown in Figure 1) that combustion gas prepared by raw material, being linked in sequence successively by shredder assembly 1, screening plant 2, gas unit 3 processed, high-temperature dust removal unit 4, air preheater 5, superheated vapour unit 6, saturation steam unit 7, economizer 8, nonaqueous dust cleaner 9, indirect cooler 10 and desulfurizer 11 forms; This device is also provided with lime-ash cooling unit 12;
Described shredder assembly 1 is provided with dirty coal opening for feed;
Comprise connected one-level gasifier and secondary gasifier in described gas unit 3 processed, wherein, one-level gasifier is connected with screening plant 2, and secondary gasifier is connected with high-temperature dust removal unit 4; Gas unit 3 processed is also connected with lime-ash cooling unit 12 by lime-ash cooling duct c, and lime-ash cooling unit 12 is provided with the outlet of cold lime-ash;
High-temperature cyclone dust extractor is comprised in described high-temperature dust removal unit 4; High-temperature dust removal unit 4 is also connected with gas unit 3 processed by flying dust circulating line a;
Described air preheater 5 is provided with air inlet; Air preheater 5 is also connected with gas unit 3 processed by air gasification agent pipeline b;
Described desulfurizer 11 is provided with purified gas outlet;
Described lime-ash cooling unit 12 is provided with the water-in of softening cold water; Lime-ash cooling unit 12 also by steam gasification agent pipeline d, is connected with gas unit 3 processed via economizer 8, saturation steam unit 7 and superheated vapour unit 6 successively.
Embodiment 7
The device adopting embodiment 6 to provide prepares combustion gas:
Dirty coal (character is in table 1) is through shredder assembly 1, after screening plant 2 processes, particle diameter 2-6mm, the particle being greater than 6mm be 1% dirty coal be introduced into the one-level gasifier of gas unit 3 processed and a small amount of high temperature gasification agent (650 DEG C) carries out high temperature pyrolysis (850 DEG C) pyrolysis gas subsequently, Gu product together enters secondary gasifier fully gasify (950 DEG C) with the high temperature gasification agent (650 DEG C) from air preheater 5 and superheated vapour unit 6, the high-temperature fuel gas (900 DEG C) produced is through the tornado dust collector removing flying dust of high-temperature dust removal unit 4, the flying dust collected returns gas unit 3 Cyclic Gas-making processed, lime-ash (920 DEG C) enters lime-ash cooling unit 12 and carries out heat recuperation with softening cold water (20 DEG C) indirect heat exchange, make softening temperature of cold water rises to 80 DEG C, lime-ash cools to 100 DEG C, in ash silo, be further cooled to room temperature to transport outward again use as building materials, the combustion gas heat exchange that the softening water being warmed up to 80 DEG C through lime-ash cooling unit 12 is introduced into economizer 8 and 280 DEG C is warming up to 95 DEG C, then the high-temperature fuel gas heat exchange that enters superheated vapour unit 6 and 750 DEG C of the combustion gas heat exchange entering saturation steam unit 7 and the 480 DEG C saturation steam that produces 195 DEG C finally obtains 650 DEG C of superheated vapours and enters gas unit 3 processed as vaporized chemical, first combustion gas after dedusting enters air preheater 5 makes preheating of air enter gas unit 3 processed to 650 DEG C as vaporized chemical with Cryogenic air (20 DEG C) heat exchange, after combustion gas cooling, (750 DEG C) successively enter superheated vapour unit 6, saturation steam unit 7 and economizer 8 respectively with the saturation steam of 195 DEG C, the water of the water of 95 DEG C and 80 DEG C carries out heat exchange and reclaims combustion gas surplus heat, fuel gas temperature is made to be down to 480 DEG C respectively, 280 DEG C, 150 DEG C and enter to enter after nonaqueous dust cleaner 9 removes the thin dirt carried enter desulfurizer 11 desulfurizing and purifying after indirect cooler 10 is cooled to 30 DEG C further after obtain clean fuel gas product, exchangeability is in table 2.
Table 1: the industry of dirty coal sample and ultimate analysis
Table 2: exchangeability analysis
Component CO 2 CO CH 4 C 2H 4 H 2 H 2S N 2
V.％ 12.15 15.14 2.83 0.67 21.29 1.46 45.16
Embodiment 8
The device adopting embodiment 6 to provide prepares combustion gas:
Dirty coal (character is in table 3) is first through shredder assembly 1, after screening plant 2 processes, particle diameter 2-6mm, the particle being greater than 6mm be 1% dirty coal be introduced into the one-level gasifier of gas unit 3 processed and a small amount of high temperature gasification agent (650 DEG C) carries out high temperature pyrolysis (850 DEG C) pyrolysis gas subsequently, Gu product together enters secondary gasifier fully gasify (1050 DEG C) with the high temperature gasification agent (650 DEG C) from air preheater 5 and superheated vapour unit 6, the high-temperature fuel gas (950 DEG C) produced is through the tornado dust collector removing flying dust of high-temperature dust removal unit 4, the flying dust collected returns gas unit 3 Cyclic Gas-making processed, lime-ash (980 DEG C) enters lime-ash cooling unit 12 and carries out heat recuperation with softening cold water (20 DEG C) indirect heat exchange, make softening temperature of cold water rises to 90 DEG C, lime-ash cools to 100 DEG C, in ash silo, be further cooled to room temperature to transport outward again use as building materials, the combustion gas heat exchange that the softening water being warmed up to 90 DEG C through lime-ash cooling unit 12 is introduced into economizer 8 and 300 DEG C is warming up to 100 DEG C, then the high-temperature fuel gas heat exchange that enters superheated vapour unit 6 and 750 DEG C of the combustion gas heat exchange entering saturation steam unit 7 and the 500 DEG C saturation steam that produces 195 DEG C finally obtains 650 DEG C of superheated vapours and enters gas unit 3 processed as vaporized chemical, first combustion gas after dedusting enters air preheater 5 makes preheating of air enter gas unit 3 processed to 650 DEG C as vaporized chemical with Cryogenic air (20 DEG C) heat exchange, after combustion gas cooling, (750 DEG C) successively enter superheated vapour unit 6, saturation steam unit 7 and economizer 8 respectively with the saturation steam of 195 DEG C, the water of the water of 100 DEG C and 90 DEG C carries out heat exchange and reclaims combustion gas surplus heat, fuel gas temperature is made to be down to 500 DEG C respectively, 300 DEG C, 150 DEG C and enter to enter after nonaqueous dust cleaner 9 removes the thin dirt carried enter desulfurizer 11 desulfurizing and purifying after indirect cooler 10 is cooled to 30 DEG C further after obtain clean fuel gas product, exchangeability is in table 4.
Table 3: the industry of dirty coal sample and ultimate analysis
Table 4: exchangeability analysis
Component CO 2 CO CH 4 C 2H 4 H 2 H 2S N 2
V.％ 15.66 11.47 2.38 0.47 17.92 0.46 48.61
Although above with general explanation, embodiment and test, the present invention is described in detail, and on basis of the present invention, can make some modifications or improvements it, this will be apparent to those skilled in the art.Therefore, these modifications or improvements without departing from theon the basis of the spirit of the present invention, all belong to the scope of protection of present invention.

Claims (10)

1. be the method that combustion gas prepared by raw material with dirty coal, it is characterized in that, said method comprising the steps of:
(I) get dirty coal, successively after broken and screening pre-treatment, obtain the gasified raw material that particle that particle diameter is greater than 6mm is less than total amount 3%;
(II) described gasified raw material is under the effect of vaporized chemical, carries out one-level, secondary pyrolytic gasification successively, obtains high-temperature fuel gas and hot lime-ash;
Described hot lime-ash and softening cold water carry out heat exchange, obtain water at low temperature; After lime-ash after heat exchange is further cooled to room temperature, obtain cold lime-ash;
(III) described high-temperature fuel gas is carried out high-temperature dust removal, remove flying dust, obtain the high-temperature fuel gas of primary purification;
(IV) high-temperature fuel gas of described primary purification is carried out Multi-stage heat exchange with air at room temperature, saturation steam, high-temperature water and water at low temperature successively, obtain low temperature combustion gas;
After the high-temperature fuel gas of described primary purification and air at room temperature carry out heat exchange, also obtain high temperature air, use as the described vaporized chemical of step (II);
The described Multi-stage heat of the reverse participation of step (II) described water at low temperature exchanges, and obtains high-temperature water, saturation steam and superheated vapour successively, and described superheated vapour uses as the described vaporized chemical of step (II);
(V) by after described low temperature combustion gas removing fine solid particle, cooling, desulfurizing and purifying, clean combustion gas is obtained.
2. method according to claim 1, is characterized in that, step (III) described flying dust, as gasified raw material, carries out circulation pyrolytic gasification through step (II).
3. method according to claim 1, is characterized in that, the temperature of step (II) described vaporized chemical is 500 ~ 650 DEG C; The temperature of described one-level pyrolytic gasification is 850 ~ 950 DEG C, and the temperature of secondary pyrolytic gasification is 950 ~ 1100 DEG C.
4. the method according to claims 1 to 3 any one, it is characterized in that, the described Multi-stage heat of step (IV) exchanges and is specially: the high-temperature fuel gas of primary purification is carried out Multi-stage heat exchange with the water at low temperature of air at room temperature, the saturation steam of 150 ~ 200 DEG C, the high-temperature water of 95 ~ 200 DEG C and 60 ~ 100 DEG C successively, and to be combustion gas, the temperature of 450 ~ 500 DEG C the be combustion gas of 250 ~ 300 DEG C that to obtain temperature be successively combustion gas, the temperature of 650 ~ 750 DEG C and temperature are the low temperature combustion gas of 150 ~ 200 DEG C.
5. method according to claim 4, is characterized in that, step (II) described water at low temperature is 60 ~ 100 DEG C;
The described Multi-stage heat of water at low temperature reverse participation step (IV) of described 60 ~ 100 DEG C exchanges, obtain the high-temperature water of 95 ~ 200 DEG C, the saturation steam of 150 ~ 200 DEG C and the superheated vapour of 500 ~ 650 DEG C successively, described superheated vapour uses as the described vaporized chemical of step (II).
6. one kind is the device that combustion gas prepared by raw material with dirty coal, it is characterized in that, described device comprises the pretreatment unit, gasification gas making unit, high-temperature fuel gas dust removing units, high-temperature fuel gas waste heat recovery unit, combustion gas dust removing units, combustion gas cooling unit and the gas desulfurization unit that are linked in sequence successively;
Described pretreatment unit comprises connected shredder assembly (1) and screening plant (2);
Described gasification gas making unit comprises gas unit (3) processed; Comprise connected one-level gasifier and secondary gasifier in described gas unit (3) processed, described one-level gasifier is connected with screening plant (2);
Described high-temperature fuel gas dust removing units comprises high-temperature dust removal unit (4), and is connected with the secondary gasifier of gas unit (3) processed; High-temperature dust removal unit (4) is also connected with gas unit (3) processed by flying dust circulating line (a); High-temperature cyclone dust extractor is comprised in described high-temperature dust removal unit (4);
Described high-temperature fuel gas waste heat recovery unit comprises the air preheater (5), superheated vapour unit (6), saturation steam unit (7) and the economizer (8) that are linked in sequence successively;
Described combustion gas dust removing units comprises nonaqueous dust cleaner (9);
Described combustion gas cooling unit comprises indirect cooler (10);
Described gas desulfurization unit comprises desulfurizer (11).
7. device according to claim 6, is characterized in that, air preheater (5) is provided with air inlet; Described air preheater (5) is also connected with gas unit (3) processed by air gasification agent pipeline (b).
8. the device according to claim 6 or 7, is characterized in that, described device also comprises high-temperature ash waste heat recovery unit;
Described high temperature recrement waste heat recovery unit comprises lime-ash cooling unit (12); Described lime-ash cooling unit (12) is provided with the outlet of cold lime-ash;
Gas unit (3) processed is connected with lime-ash cooling unit (12) by lime-ash cooling duct (c).
9. the device according to claim 6 ~ 8 any one, is characterized in that, described lime-ash cooling unit (12) is provided with the water-in of softening cold water;
Described lime-ash cooling unit (12) is also by steam gasification agent pipeline (d), successively via economizer (8), saturation steam unit (7) and superheated vapour unit (6), be connected with gas unit (3) processed.
10. the method according to Claims 1 to 5 any one, is characterized in that, utilizes device described in claim 6 ~ 9 any one to prepare combustion gas.
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