CN104804774B - A kind of method and apparatus for preparing combustion gas as raw material with dirty coal - Google Patents
A kind of method and apparatus for preparing combustion gas as raw material with dirty coal Download PDFInfo
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- CN104804774B CN104804774B CN201510189127.7A CN201510189127A CN104804774B CN 104804774 B CN104804774 B CN 104804774B CN 201510189127 A CN201510189127 A CN 201510189127A CN 104804774 B CN104804774 B CN 104804774B
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- 239000000567 combustion gas Substances 0.000 title claims abstract description 92
- 239000003245 coal Substances 0.000 title claims abstract description 57
- 239000002994 raw material Substances 0.000 title claims abstract description 34
- 238000000034 method Methods 0.000 title claims abstract description 29
- 239000000428 dust Substances 0.000 claims abstract description 85
- 239000007789 gas Substances 0.000 claims abstract description 72
- 238000002309 gasification Methods 0.000 claims abstract description 61
- 239000002737 fuel gas Substances 0.000 claims abstract description 55
- 238000001816 cooling Methods 0.000 claims abstract description 38
- 238000011084 recovery Methods 0.000 claims abstract description 13
- 239000002918 waste heat Substances 0.000 claims abstract description 10
- 238000006477 desulfuration reaction Methods 0.000 claims abstract description 5
- 230000023556 desulfurization Effects 0.000 claims abstract description 5
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 64
- 239000003795 chemical substances by application Substances 0.000 claims description 50
- 239000012467 final product Substances 0.000 claims description 42
- 229920006395 saturated elastomer Polymers 0.000 claims description 34
- 238000000746 purification Methods 0.000 claims description 22
- 239000002245 particle Substances 0.000 claims description 21
- 238000012216 screening Methods 0.000 claims description 20
- 230000008859 change Effects 0.000 claims description 8
- 230000003009 desulfurizing effect Effects 0.000 claims description 8
- 239000007787 solid Substances 0.000 claims description 7
- 239000002893 slag Substances 0.000 claims description 4
- 238000002485 combustion reaction Methods 0.000 claims description 2
- 238000005516 engineering process Methods 0.000 abstract description 15
- 239000003344 environmental pollutant Substances 0.000 abstract description 3
- 231100000719 pollutant Toxicity 0.000 abstract description 3
- 239000002956 ash Substances 0.000 description 82
- 241000196324 Embryophyta Species 0.000 description 10
- 238000004140 cleaning Methods 0.000 description 5
- 230000000694 effects Effects 0.000 description 5
- 238000000197 pyrolysis Methods 0.000 description 5
- 230000008569 process Effects 0.000 description 4
- 235000002918 Fraxinus excelsior Nutrition 0.000 description 3
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 3
- 239000004566 building material Substances 0.000 description 3
- 238000004519 manufacturing process Methods 0.000 description 3
- 229910052760 oxygen Inorganic materials 0.000 description 3
- 239000001301 oxygen Substances 0.000 description 3
- 238000010792 warming Methods 0.000 description 3
- 239000002699 waste material Substances 0.000 description 3
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 2
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 2
- 238000004458 analytical method Methods 0.000 description 2
- 239000000571 coke Substances 0.000 description 2
- 125000004122 cyclic group Chemical group 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 230000036284 oxygen consumption Effects 0.000 description 2
- 239000000047 product Substances 0.000 description 2
- 238000010791 quenching Methods 0.000 description 2
- 238000004064 recycling Methods 0.000 description 2
- 239000012265 solid product Substances 0.000 description 2
- 238000012360 testing method Methods 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- 235000006508 Nelumbo nucifera Nutrition 0.000 description 1
- 240000002853 Nelumbo nucifera Species 0.000 description 1
- 235000006510 Nelumbo pentapetala Nutrition 0.000 description 1
- ISWSIDIOOBJBQZ-UHFFFAOYSA-N Phenol Chemical compound OC1=CC=CC=C1 ISWSIDIOOBJBQZ-UHFFFAOYSA-N 0.000 description 1
- 229910021529 ammonia Inorganic materials 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 125000004432 carbon atom Chemical group C* 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 239000010883 coal ash Substances 0.000 description 1
- 239000003034 coal gas Substances 0.000 description 1
- 238000004939 coking Methods 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 238000009776 industrial production Methods 0.000 description 1
- 239000003317 industrial substance Substances 0.000 description 1
- 229910052742 iron Inorganic materials 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 230000035699 permeability Effects 0.000 description 1
- KSSNXJHPEFVKHY-UHFFFAOYSA-N phenol;hydrate Chemical compound O.OC1=CC=CC=C1 KSSNXJHPEFVKHY-UHFFFAOYSA-N 0.000 description 1
- 238000010926 purge Methods 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 239000010865 sewage Substances 0.000 description 1
- 239000000779 smoke Substances 0.000 description 1
- 239000011343 solid material Substances 0.000 description 1
- 230000003068 static effect Effects 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 239000003643 water by type Substances 0.000 description 1
Classifications
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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
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- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Combustion & Propulsion (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Organic Chemistry (AREA)
- Industrial Gases (AREA)
Abstract
The present invention relates to a kind of method for preparing combustion gas as raw material with dirty coal.The invention further relates to a kind of device for preparing combustion gas as raw material with dirty coal, described device includes 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, and described device still further comprises high-temperature fuel gas waste heat recovery unit.The apparatus and method that the present invention is provided utilize the technology such as technology and two-stage gasifier by fully reclaiming residue after gasifying, high-temperature gas multi-stage heat, solve the problems, such as bad adaptability of the existing combustion gas technology of preparing to dirty coal raw material, simultaneously can reduces cost, reduce pollutant emission, energy utilization rate and system thermal efficiency are improved, and then realizes extensive, the efficient utilization of this resource inferior of dirty coal.
Description
Technical field
The present invention relates to combustion-gas jet test field, and in particular to the method and apparatus for preparing combustion gas as raw material with coal ash high.
Background technology
China is coal production big country of the world, produces coal per year more than 1,000,000,000 tons.Coal is main energy sources of China and important
Industrial chemicals.Content of ashes is universal higher in China's coal, and changes greatly, and the special low culm whole nation of the ash content less than 10% only accounts for spy
17% or so of bright reserves, it is clear that improve the utilization rate of coal resources, the especially utilization rate of ash coal are to development China
National economy is significant.But pit ash is high, freight volume and freight charges can be increased.In burning, ash content is higher, and the thermal efficiency is got over
It is low, and smoke discharge amount and slag amount can be increased, the coal-fired pollution to air of aggravation.During coking, cleans ash is higher, coke
Ash content it is higher, the coke ratio of ironmaking is increased by, and the capacity factor of a blast furnace is just reduced, produce iron reduce.If can be by this part
Ash coal cleaning, the clean gas that are converted into efficiently, inexpensive are used for industrial production or domestic fuel then to low-quality coal resources
Efficiently utilize, positive facilitation is played in reduction environmental pollution.
Current coal gas technology mainly includes fixed bed, fluid bed and entrained flow bed gasification technology.But for dirty coal (ash
Divide content>25%) utilization aspect, for current technology, air-flow bed technique is influenceed by the factor such as slag tap and oxygen consumption,
Also there is certain difficulty to the gasification of ash coal；Although pressurization static bed gasification technology can process dirty coal, it is to bed
The uniformity of layer, gas permeability requirements are higher, thus limit raw material range, can only process a part of satisfactory block ash high
Coal, while such gasification needs to consume a large amount of chilled waters, sewage purification is increased in water containing material demands such as tar, phenol, ammonia
Link, therefore increase investment and raw materials consumption.Although fluidized gasification technology is not state-of-the-art gasification technology, vapor pressure
Do not increase, but be relatively adapted to prepare combustion gas using dirty coal yet.But existing fluidized gasification technology is in treatment dirty coal process
In a series of problem is still present.Such as, the heat increase that the fusing of content of ashes increase lime-ash absorbs, in order to ensure that gasification furnace is suitable
Sharp deslagging and the heat balance of gasification furnace is maintained, it is necessary to increase oxygen amount come more carbon atoms that burn, therefore, the oxygen of gasification system
Consumption and coal consumption increase.Ash content often increases by 1% under same gasification condition, 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 excluded with lime-ash, and this partial heat cannot be recycled, and the increase of bed drain purge increases
The big heat loss of system, reduces high steam yield, while lime-ash Quench consumption Quench water is big, aggravation lock hopper heat is negative
Lotus.Therefore, equipment maintenance cost, deslagging traffic expense increase when ash content is high in raw coal, so as to increase enterprise's production capacity and energy consumption.
The content of the invention
The present invention is for the technical problem during the utilization of above-mentioned dirty coal, the method for proposing to prepare combustion gas using dirty coal
And device, using dirty coal itself content of ashes it is high the characteristics of abundant recovery system heat and then realize dirty coal cleaning, high
Effect prepares the purpose of purified gas.The technology has that adaptability to raw material is wide, treating capacity big, efficiency of carbon con version and the thermal efficiency are high, pollution-free
Energy consumption is small, simple to operate, low cost the features such as.
It is an object of the invention to provide one kind with dirty coal as raw material, low cost, cleaning, efficient combustion gas is prepared
Method.The present invention is solved by fully reclaiming residue after gasifying, high-temperature gas multi-stage heat using technology and two-stage gasifier technology
The problem of bad adaptability of the existing combustion gas technology of preparing to dirty coal raw material, at the same can reduces cost, reduce pollutant emission, carry
High energy source utilization rate and system thermal efficiency, and then realize extensive, the efficient utilization of this resource inferior of dirty coal.
Specifically, the described method comprises the following steps：
(I) dirty coal is taken, successively after crushing and screening is pre-processed, particle of the particle diameter more than 6mm is obtained and is less than total amount 3%
Gasified raw material；
(II) gasified raw material carries out one-level, two grades of pyrolytic gasifications in the presence of gasifying agent, successively, obtain final product high-temperature fuel gas and
Hot lime-ash；
Hot lime-ash carries out heat exchange with cold water is softened, and obtains water at low temperature；After lime-ash after heat exchange is further cooled to room temperature,
Obtain final product cold lime-ash；
(III) high-temperature fuel gas are carried out into high-temperature dust removal, removes flying dust, obtain final product the high-temperature fuel gas of primary purification；
(IV) high-temperature fuel gas of primary purification are carried out with air at room temperature, saturated vapor, high-temperature water and water at low temperature successively many
Level heat exchange, obtains final product low temperature combustion gas；
After the high-temperature fuel gas of the primary purification carry out heat exchange with air at room temperature, high temperature air is also obtained, as step
(II) gasifying agent is used；
Meanwhile, step (II) gained water at low temperature inversely participates in the multistage heat exchange, and high-temperature water, saturated vapor are obtained successively
And superheated steam, the superheated steam uses as step (II) described gasifying agent；
(V) after low temperature combustion gas being removed into fine solid particle, cooling, desulfurizing and purifying, net combustion gas is obtained final product.
The high-temperature fuel gas of step (II) gained after two-stage pyrolytic gasification are gaseous state, and remaining lime-ash is solid-state, high temperature combustion
Gas is with lime-ash because property difference can natural separation.In the high-temperature fuel gas, tiny solid granular dust is mixed with, that is, be not pyrolyzed
The flying dust of gasification from high-temperature fuel gas, it is necessary to remove flying dust by step (III).
Methods described can also include recycling step (III) gained flying dust, specially：Flying dust is made again
Gas.
The temperature of step (II) described gasifying agent is 500~650 DEG C；The temperature of the one-level pyrolytic gasification is 850~950
DEG C, two grades of temperature of pyrolytic gasification are 950~1100 DEG C.
Used as a kind of preferred scheme, the temperature of step (II) described gasifying agent is 650 DEG C；The temperature of the one-level pyrolytic gasification
It is 850 DEG C to spend, and two grades of temperature of pyrolytic gasification are 950~1050 DEG C.
Step (IV) the multistage heat exchange is specially：By the high-temperature fuel gas of primary purification successively with air at room temperature, 150~
200 DEG C of saturated vapor, 95~200 DEG C of high-temperature water and 60~100 DEG C of water at low temperature carry out multistage heat exchange, and temperature is obtained successively
It is 150 to spend combustion gas, the combustion gas that temperature is 250~300 DEG C that the combustion gas for 650~750 DEG C, temperature are 450~500 DEG C and temperature
~200 DEG C of low temperature combustion gas.Meanwhile, the water at low temperature of 60~100 DEG C of step (II) gained inversely participates in step (IV) described multistage
Heat exchange, obtains 95~200 DEG C of high-temperature water, 150~200 DEG C of saturated vapor and 500~650 DEG C of superheated steam successively,
The superheated steam is used as step (II) described gasifying agent.
Meanwhile, the air of step (IV) described room temperature is carried out by the high-temperature fuel gas with 950~1100 DEG C of primary purification
After heat exchange, 500~650 DEG C of air is also obtained, the pyrolytic gasification of step (II) can be used for as gasifying agent.
Step (V) the low temperature combustion gas cooling, to be cooled to 20~50 DEG C.
Present invention also offers a kind of device for preparing combustion gas as raw material with dirty coal, described device includes sequentially connecting successively
Pretreatment unit, gasification gas making unit, high-temperature fuel gas dust removing units, high-temperature fuel gas waste heat recovery unit, the combustion gas dedusting list for connecing
Unit, combustion gas cooling unit and gas desulfurization unit.
The pretreatment unit includes connected breaker and screening plant.Breaker is provided with the charging of dirty coal
Mouthful.
The gasification gas making unit includes gas unit processed.The one-level gasifier and two grades being connected are included in the gas unit processed
Gasifier；The one-level gasifier is connected with screening plant.
Described high-temperature fuel gas dust removing units include high-temperature dust removal unit, and are connected with two grades of gasifiers of gas unit processed.
High-temperature cyclone dust extractor is included in high-temperature dust removal unit.According to being actually needed for dedusting, the high-temperature cyclone dust extractor can be
One-level or the multistage of series connection, series are higher, and efficiency of dust collection is higher.
The high-temperature fuel gas waste heat recovery unit includes the air preheater being linked in sequence successively, superheated steam unit, satisfies
With steam unit and economizer.
The combustion gas dust removing units include nonaqueous dust cleaner.
The combustion gas cooling unit includes indirect cooler.
The gas desulfurization unit includes desulfurizer, and the desulfurizer is provided with purified gas outlet.
Raw material dirty coal sequentially pass through breaker, screening plant, gas unit processed, high-temperature dust removal unit, air preheater,
After superheated steam unit, saturated vapor unit, economizer, nonaqueous dust cleaner, indirect cooler and desulfurizer, you can obtain
Clean combustion gas.
In order to realize recycling for waste material, high-temperature dust removal unit can also be by flying dust circulating line and gas unit phase processed
Even, so as to realize the circulation pyrolytic gasification to flying dust.
In order to improve energy utilization rate and system thermal efficiency, air preheater can also set air inlet, and pass through
Air gasification agent pipeline is connected with gas unit processed.The air of room temperature is passed through air preheater, through heat exchange after, resulting heat
Air can be passed through gas unit processed as gasifying agent.
In order to improve energy utilization rate and system thermal efficiency, described device can further include high-temperature ash waste heat and return
Unit is received, the high temperature recrement waste heat recovery unit may include lime-ash cooling unit.
The lime-ash cooling unit is provided with cold lime-ash outlet；Gas unit processed can also be cold by lime-ash cooling pipe and lime-ash
But unit is connected.After lime-ash cooling, take out, be capable of achieving the sustainable utilization of waste material.
The lime-ash cooling unit may further be provided the water inlet for softening cold water, and by steam gasification agent pipeline,
Successively via economizer, saturated vapor unit and superheated steam unit, it is connected with gas unit processed.
The method for preparing clean fuel gas of the present invention, the device that can be provided using the present invention is realized.
The method of the invention can be more preferably：
(I) dirty coal is taken, after being pre-processed through breaker and screening plant successively, particle of the particle diameter more than 6mm is obtained few
In the gasified raw material of total amount 1%；
(II) step (I) gained gasified raw material is passed through gas unit processed, through the one-level gas that temperature in gas unit processed is 850 DEG C
Change device, be pyrolyzed in the presence of gasifying agent；By gained pyrolysis gas and remaining solid material be together passed through temperature for 950~
1050 DEG C of two grades of gasifiers, fully gasify in the presence of gasifying agent, obtain final product 900~950 DEG C high-temperature fuel gas and 920~
980 DEG C of lime-ash；
The lime-ash is passed through lime-ash cooling unit by lime-ash cooling pipe, and heat exchange is carried out with softening cold water therein；
After lime-ash is cooled to room temperature, take out, obtain final product cold lime-ash, outward transport is used as building materials；
(III) step (II) gained high-temperature fuel gas are passed through high-temperature dust removal unit, by the one-level in high-temperature dust removal unit
Or multistage high-temperature cyclone dust extractor, flying dust is removed, obtain final product the high-temperature fuel gas of the primary purification that temperature is 900~950 DEG C；
The flying dust is passed through gas unit processed by flying dust circulating line, is circulated pyrolytic gasification；
(IV) high-temperature fuel gas of step (III) gained primary purification are passed through air preheater, with the air at room temperature in it
Heat exchange is carried out, the combustion gas that temperature is 750 DEG C is obtained final product；Superheated steam unit is passed through again, is carried out with its interior 195 DEG C saturated vapor
Heat exchange, obtains final product the combustion gas that temperature is 480~500 DEG C；Saturated vapor unit is passed through again, with its interior 95~100 DEG C of high-temperature water
Heat exchange is carried out, the combustion gas that temperature is 280~300 DEG C is obtained final product；Economizer is passed through again, is carried out with its interior 80~90 DEG C water at low temperature
Heat exchange, obtains final product the combustion gas that temperature is 150 DEG C；
Meanwhile, the air of room temperature is passed through air preheater, after the high-temperature fuel gas with primary purification carry out heat exchange,
650 DEG C of air is obtained, gas unit processed is passed through by air gasification agent pipeline as gasifying agent；
Meanwhile, by soften cold water be passed through lime-ash cooling unit, through heat exchange after, obtain the low temperature that temperature is 80~90 DEG C
Water；The water at low temperature by steam gasification agent pipeline, sequentially pass through economizer be warming up to 95~100 DEG C, again through supersaturated vapor
Unit forms 195 DEG C of saturated vapor, through superheated steam unit forms 600~650 DEG C of superheated steam, the superheated steam again
Gas unit processed is passed through as gasifying agent；
(V) combustion gas that step (IV) gained temperature is 150 DEG C is passed through nonaqueous dust cleaner, removes fine solid particle；It is passed through again
Indirect cooler, obtains the combustion gas that temperature is 30 DEG C；Desulfurizer is passed through again, after desulfurizing and purifying, obtains final product the combustion gas of cleaning.
In actual production process, above-mentioned steps are persistently to be carried out.
The present invention is heated up by the heat supply agent of fully recovery high-temperature ash and high-temperature fuel gas and is effectively reduced gasification
Process improves system thermal efficiency, and then improve fuel gases calorific value and reduce combustion-gas jet test cost than coal consumption.
The present invention realizes excellent effect.Specifically, the present invention realizes extensive, inexpensive, clear with dirty coal
The clean efficient purpose for preparing combustion gas, gasification does not produce the pollutant such as tar and phenol water；The invention provides a kind of combustion of high temperature
The apparatus and method that gas heat fully reclaimed and obtained high temperature gasification agent, using air preheater, superheated steam unit, saturation
On the one hand the Multi-stage heat-exchanging devices such as steam unit, economizer have fully reclaimed high-temperature gas heat, improve system thermal efficiency, a side
Air and steam gasification agent are preheating to higher temperature by face, can be met gasification ashy substance heat demand high and be reduced and be consumed than oxygen
With than coal consumption, and then combustion gas cost is reduced；Because the grey quantity of slag after dirty coal gasification is larger, temperature is higher, carries substantial amounts of aobvious
Heat, directly cooling causes very big waste, therefore, the apparatus and method that the present invention is provided fully reclaim high-temperature ash, using lime-ash
Most of heat is passed to water at low temperature by cooling device by way of indirect heat exchange, is risen warm water and is further gone preheating to produce overheat
Steam further increases the thermal efficiency of system and reduces combustion gas cost as gasifying agent.
Brief description of the drawings
Fig. 1 is the schematic diagram of the described device of embodiment 6；Wherein：1st, breaker, 2, screening plant, 3, gas unit processed, 4,
High-temperature dust removal unit, 5, air preheater, 6, superheated steam unit, 7, saturated vapor unit, 8, economizer, 9, dry method dust
Device, 10, indirect cooler, 11, desulfurizer, 12, lime-ash cooling unit；A, flying dust circulating line, b, air gasification agent pipeline,
C, lime-ash cooling pipe, d, steam gasification agent pipeline.
Specific embodiment
Following examples are used to illustrate the present invention, but are not limited to the scope of the present invention.
Embodiment 1
Combustion gas is prepared according to following steps：
(I) dirty coal is taken, successively after crushing and screening is pre-processed, particle of the particle diameter more than 6mm is obtained and is less than total amount 1%
Gasified raw material；
(II) gasified raw material carries out one-level pyrolytic gasification at 850 DEG C under 600 DEG C of gasifying agent effect, then at 1000 DEG C
Two grades of pyrolytic gasifications are carried out, high-temperature fuel gas and lime-ash is obtained final product；
Meanwhile, gained lime-ash is carried out into heat exchange with cold water is softened, after lime-ash is cooled to room temperature, obtain final product cold lime-ash；
(III) high-temperature fuel gas are carried out into high-temperature dust removal, removes flying dust, obtain final product the high temperature of the primary purification that temperature is 1000 DEG C
Combustion gas；
Meanwhile, gained flying dust is circulated pyrolytic gasification as gasified raw material by step (II)；
(IV) high-temperature fuel gas of primary purification and air at room temperature are carried out into heat exchange, obtains final product the combustion gas that temperature is 700 DEG C；Again
Saturated vapor with 175 DEG C carries out heat exchange, obtains final product the combustion gas that temperature is 480 DEG C；The high-temperature water with 150 DEG C carries out hot friendship again
Change, obtain final product the combustion gas that temperature is 280 DEG C；The water at low temperature with 80 DEG C carries out heat exchange again, obtains final product the combustion gas that temperature is 180 DEG C；
After the high-temperature fuel gas of the primary purification carry out heat exchange with air at room temperature, 600 DEG C of air is also obtained, as step
Suddenly (II) described gasifying agent is used；
Meanwhile, will soften cold water carries out the water at low temperature of 80 DEG C of gained after heat exchange with lime-ash, inversely participates in described in this step
Heat exchange, obtains 150 DEG C of high-temperature water, 175 DEG C of saturated vapors and 600 DEG C of superheated steam successively, and described 600 DEG C of overheat is steamed
Vapour is used as step (II) described gasifying agent；
(V) combustion gas that temperature is 180 DEG C is removed into fine solid particle, is cooled to 30 DEG C, after desulfurizing and purifying, obtain final product net combustion gas.
Embodiment 2
Combustion gas is prepared according to following steps：
(I) dirty coal is taken, successively after crushing and screening is pre-processed, particle of the particle diameter more than 6mm is obtained and is less than total amount 2%
Gasified raw material；
(II) gasified raw material carries out one-level pyrolytic gasification at 850 DEG C, then enter at 950 DEG C under 500 DEG C of gasifying agent effect
Two grades of pyrolytic gasifications of row, obtain final product high-temperature fuel gas and lime-ash；
Meanwhile, gained lime-ash is carried out into heat exchange with cold water is softened, after lime-ash is cooled to room temperature, obtain final product cold lime-ash；
(III) high-temperature fuel gas are carried out into high-temperature dust removal, removes flying dust, obtain final product the high temperature of the primary purification that temperature is 900 DEG C
Combustion gas；
Meanwhile, gained flying dust is circulated pyrolytic gasification as gasified raw material by step (II)；
(IV) high-temperature fuel gas of primary purification and air at room temperature are carried out into heat exchange, obtains final product the combustion gas that temperature is 650 DEG C；Again
Saturated vapor with 150 DEG C carries out heat exchange, obtains final product the combustion gas that temperature is 450 DEG C；The high-temperature water with 95 DEG C carries out heat exchange again,
Obtain final product the combustion gas that temperature is 250 DEG C；The water at low temperature with 60 DEG C carries out heat exchange again, obtains final product the combustion gas that temperature is 150 DEG C；
After the high-temperature fuel gas of the primary purification carry out heat exchange with air at room temperature, 500 DEG C of air is also obtained, as step
Suddenly (II) described gasifying agent is used；
Cold water will be softened carries out the water at low temperature of 60 DEG C of gained after heat exchange with lime-ash, inversely participates in heat friendship described in this step
Change, 95 DEG C of high-temperature water, 150 DEG C of saturated vapors and 500 DEG C of superheated steam is obtained successively, described 500 DEG C of superheated steam is made
For step (II) described gasifying agent is used；
(V) combustion gas that temperature is 150 DEG C is removed into fine solid particle, is cooled to 20 DEG C, after desulfurizing and purifying, obtain final product net combustion gas.
Embodiment 3
Combustion gas is prepared according to following steps：
(I) dirty coal is taken, successively after crushing and screening is pre-processed, particle of the particle diameter more than 6mm is obtained and is less than total amount 3%
Gasified raw material；
(II) gasified raw material carries out one-level pyrolytic gasification at 950 DEG C under 650 DEG C of gasifying agent effect, then at 1100 DEG C
Two grades of pyrolytic gasifications are carried out, high-temperature fuel gas and lime-ash is obtained final product；
Meanwhile, gained lime-ash is carried out into heat exchange with cold water is softened, after lime-ash is cooled to room temperature, obtain final product cold lime-ash；
(III) high-temperature fuel gas are carried out into high-temperature dust removal, removes flying dust, obtain final product the high temperature of the primary purification that temperature is 1100 DEG C
Combustion gas；
Meanwhile, gained flying dust is circulated pyrolytic gasification as gasified raw material by step (II)；
(IV) high-temperature fuel gas of primary purification and air at room temperature are carried out into heat exchange, obtains final product the combustion gas that temperature is 750 DEG C；Again
Saturated vapor with 200 DEG C carries out heat exchange, obtains final product the combustion gas that temperature is 500 DEG C；The high-temperature water with 200 DEG C carries out hot friendship again
Change, obtain final product the combustion gas that temperature is 300 DEG C；The water at low temperature with 100 DEG C carries out heat exchange again, obtains final product the combustion gas that temperature is 200 DEG C；
After the high-temperature fuel gas of the primary purification carry out heat exchange with air at room temperature, 650 DEG C of air is also obtained, as step
Suddenly (II) described gasifying agent is used；
Cold water will be softened carries out the water at low temperature of 100 DEG C of gained after heat exchange with lime-ash, inversely participates in heat friendship described in this step
Change, 200 DEG C of high-temperature water, 200 DEG C of saturated vapors and 650 DEG C of superheated steam is obtained successively, described 650 DEG C of superheated steam is made
For step (II) described gasifying agent is used；
(V) combustion gas that temperature is 200 DEG C is removed into fine solid particle, is cooled to 50 DEG C, after desulfurizing and purifying, obtain final product net combustion gas.
Embodiment 4
The device (partly with reference to Fig. 1) of combustion gas is prepared as raw material with dirty coal, by breaker 1, screening plant 2, gas processed
Unit 3, high-temperature dust removal unit 4, air preheater 5, superheated steam unit 6, saturated vapor unit 7, economizer 8, dry method dust
Device 9, indirect cooler 10 and desulfurizer 11 are linked in sequence form successively；
The breaker 1 is provided with dirty coal charging aperture；
Comprising connected one-level gasifier and two grades of gasifiers in the gas unit 3 processed, wherein, one-level gasifier and screening
Device 2 is connected, and two grades of gasifiers are connected with high-temperature dust removal unit 4；
High-temperature cyclone dust extractor is included in the high-temperature dust removal unit 4；High-temperature dust removal unit 4 also passes through flying dust circulating line
A is connected with gas unit 3 processed；
The air preheater 5 is provided with air inlet；Air preheater 5 is also by air gasification agent pipeline b and gas processed
Unit 3 is connected；
The desulfurizer 11 is provided with purified gas outlet.
Embodiment 5
The device (partly with reference to Fig. 1) of combustion gas is prepared as raw material with dirty coal, by breaker 1, screening plant 2, gas processed
Unit 3, high-temperature dust removal unit 4, air preheater 5, superheated steam unit 6, saturated vapor unit 7, economizer 8, dry method dust
Device 9, indirect cooler 10 and desulfurizer 11 are linked in sequence form successively；The device is additionally provided with lime-ash cooling unit 12；
The breaker 1 is provided with dirty coal charging aperture；
Comprising connected one-level gasifier and two grades of gasifiers in the gas unit 3 processed, wherein, one-level gasifier and screening
Device 2 is connected, and two grades of gasifiers are connected with high-temperature dust removal unit 4；Gas unit 3 processed is also cold with lime-ash by lime-ash cooling pipe c
But unit 12 is connected, and lime-ash cooling unit 12 is provided with cold lime-ash outlet；
High-temperature cyclone dust extractor is included in the high-temperature dust removal unit 4；High-temperature dust removal unit 4 also passes through flying dust circulating line
A is connected with gas unit 3 processed；
The air preheater 5 is provided with air inlet；Air preheater 5 is also by air gasification agent pipeline b and gas processed
Unit 3 is connected；
The desulfurizer 11 is provided with purified gas outlet.
Embodiment 6
The device (as shown in Figure 1) of combustion gas is prepared as raw material with dirty coal, by breaker 1, screening plant 2, gas list processed
Unit 3, high-temperature dust removal unit 4, air preheater 5, superheated steam unit 6, saturated vapor unit 7, economizer 8, nonaqueous dust cleaner
9th, indirect cooler 10 and desulfurizer 11 are linked in sequence form successively；The device is additionally provided with lime-ash cooling unit 12；
The breaker 1 is provided with dirty coal charging aperture；
Comprising connected one-level gasifier and two grades of gasifiers in the gas unit 3 processed, wherein, one-level gasifier and screening
Device 2 is connected, and two grades of gasifiers are connected with high-temperature dust removal unit 4；Gas unit 3 processed is also cold with lime-ash by lime-ash cooling pipe c
But unit 12 is connected, and lime-ash cooling unit 12 is provided with cold lime-ash outlet；
High-temperature cyclone dust extractor is included in the high-temperature dust removal unit 4；High-temperature dust removal unit 4 also passes through flying dust circulating line
A is connected with gas unit 3 processed；
The air preheater 5 is provided with air inlet；Air preheater 5 is also by air gasification agent pipeline b and gas processed
Unit 3 is connected；
The desulfurizer 11 is provided with purified gas outlet；
The lime-ash cooling unit 12 is provided with the water inlet for softening cold water；Lime-ash cooling unit 12 also passes through steam gasification agent
Pipeline d, is connected via economizer 8, saturated vapor unit 7 and superheated steam unit 6 with gas unit 3 processed successively.
Embodiment 7
The device provided using embodiment 6 prepares combustion gas：
After dirty coal (property is shown in Table 1) is processed through breaker 1, screening plant 2, particle diameter 2-6mm, the particle more than 6mm
Dirty coal for 1% is introduced into the one-level gasifier of gas unit 3 processed and a small amount of high temperature gasification agent (650 DEG C) and carries out high temperature pyrolysis
(850 DEG C) then pyrolysis gas, solid product together enter two grades of gasifiers with from air preheater 5 and superheated steam unit 6
High temperature gasification agent (650 DEG C) fully gasify (950 DEG C), and the high-temperature fuel gas (900 DEG C) of generation are through the rotation of high-temperature dust removal unit 4
Wind deduster removes flying dust, and the flying dust being collected into returns to the Cyclic Gas-making of gas unit 3 processed, and (920 DEG C) of lime-ash enters lime-ash and cools down list
Unit 12 carries out heat recovery with cold water (20 DEG C) indirect heat exchange is softened, and makes softening temperature of cold water rises to 80 DEG C, and lime-ash cools to 100
DEG C, then it is further cooled to room temperature outward transport to be used as building materials in ash silo；80 DEG C soft is warmed up to through lime-ash cooling unit 12
Change water is introduced into economizer 8 and 280 DEG C of combustion gas heat exchange is warming up to 95 DEG C, enters back into saturated vapor unit 7 and 480 DEG C of combustion gas
Heat exchange produces 195 DEG C of saturated vapor to finally give 650 DEG C of mistakes into superheated steam unit 6 and the heat exchange of 750 DEG C of high-temperature fuel gas
Vapours enters gas unit 3 processed as gasifying agent；Combustion gas after dedusting initially enters air preheater 5 and Cryogenic air (20 DEG C)
Heat exchange makes air preheat enter gas unit 3 processed as gasifying agent to 650 DEG C, and (750 DEG C) successively enter overheat and steam after combustion gas cooling
Vapour unit 6, saturated vapor unit 7 and economizer 8 saturated vapor respectively with 195 DEG C, 95 DEG C of water and 80 DEG C of water are changed
Recuperation of heat combustion gas after-heat, makes fuel gas temperature be down to 480 DEG C, 280 DEG C, 150 DEG C respectively and be removed into nonaqueous dust cleaner 9 and takes
Cleaning is obtained after entering the desulfurizing and purifying of desulfurizer 11 after being further cooled to 30 DEG C into indirect cooler 10 after the thin dirt of band
Fuel gas product, exchangeability is shown in Table 2.
Table 1：The industry and elementary analysis of dirty coal sample
Table 2：Exchangeability is analyzed
| Component | CO | ||||||
| V.% | 12.15 | 15.14 | 2.83 | 0.67 | 21.29 | 1.46 | 45.16 |
Embodiment 8
The device provided using embodiment 6 prepares combustion gas：
Dirty coal (property is shown in Table 3) first through breaker 1, screening plant 2 treatment after, particle diameter 2-6mm, more than 6mm
Grain is introduced into the one-level gasifier of gas unit 3 processed and a small amount of high temperature gasification agent (650 DEG C) and carries out high temperature pyrolysis for 1% dirty coal
(850 DEG C) then pyrolysis gas, solid product together enter two grades of gasifiers with from air preheater 5 and superheated steam unit 6
High temperature gasification agent (650 DEG C) fully gasify (1050 DEG C), and the high-temperature fuel gas (950 DEG C) of generation are through high-temperature dust removal unit 4
Cyclone dust collectors remove flying dust, and the flying dust being collected into returns to the Cyclic Gas-making of gas unit 3 processed, and (980 DEG C) of lime-ash enters lime-ash and cools down
Unit 12 carries out heat recovery with cold water (20 DEG C) indirect heat exchange is softened, and makes softening temperature of cold water rises to 90 DEG C, and lime-ash cools to 100
DEG C, then it is further cooled to room temperature outward transport to be used as building materials in ash silo；90 DEG C soft is warmed up to through lime-ash cooling unit 12
Change water is introduced into economizer 8 and 300 DEG C of combustion gas heat exchange is warming up to 100 DEG C, enters back into saturated vapor unit 7 and 500 DEG C of combustion
Gas heat exchange produces 195 DEG C of saturated vapor to finally give 650 DEG C into superheated steam unit 6 and the heat exchange of 750 DEG C of high-temperature fuel gas
Superheated steam enters gas unit 3 processed as gasifying agent；Combustion gas after dedusting initially enters air preheater 5 and Cryogenic air (20
DEG C) exchanging heat makes air preheat enter gas unit 3 processed as gasifying agent to 650 DEG C, (750 DEG C) successively enter overheat after combustion gas cooling
Steam unit 6, saturated vapor unit 7 and economizer 8 saturated vapor respectively with 195 DEG C, 100 DEG C of water and 90 DEG C of water are carried out
Combustion gas after-heat is reclaimed in heat exchange, fuel gas temperature is down to 500 DEG C, 300 DEG C, 150 DEG C respectively and is removed into nonaqueous dust cleaner 9
Obtain clean after entering the desulfurizing and purifying of desulfurizer 11 after being further cooled to 30 DEG C into indirect cooler 10 after the thin dirt for carrying
Net fuel gas product, exchangeability is shown in Table 4.
Table 3：The industry and elementary analysis of dirty coal sample
Table 4：Exchangeability is analyzed
| Component | CO | ||||||
| V.% | 15.66 | 11.47 | 2.38 | 0.47 | 17.92 | 0.46 | 48.61 |
Although above having used general explanation, specific embodiment and experiment, the present invention is made to retouch in detail
State, but on the basis of the present invention, it can be made some modifications or improvements, this is to those skilled in the art apparent
's.Therefore, these modifications or improvements without departing from theon the basis of the spirit of the present invention, belong to claimed
Scope.
Claims (10)
1. it is a kind of with dirty coal as raw material prepare combustion gas method, it is characterised in that the described method comprises the following steps：
(I) dirty coal is taken, successively after crushing and screening is pre-processed, gas of particle of the particle diameter more than 6mm less than total amount 3% is obtained
Change raw material；
(II) gasified raw material carries out one-level, two grades of pyrolytic gasifications in the presence of gasifying agent, successively, obtain final product high-temperature fuel gas and
Hot lime-ash；
The hot lime-ash carries out heat exchange with cold water is softened, and obtains water at low temperature；After lime-ash after heat exchange is further cooled to room temperature,
Obtain final product cold lime-ash；
(III) high-temperature fuel gas are carried out into high-temperature dust removal, removes flying dust, obtain final product the high-temperature fuel gas of primary purification；
(IV) high-temperature fuel gas of the primary purification are carried out with air at room temperature, saturated vapor, high-temperature water and water at low temperature successively many
Level heat exchange, obtains final product low temperature combustion gas；
After the high-temperature fuel gas of the primary purification carry out heat exchange with air at room temperature, high temperature air is also obtained, as step (II)
The gasifying agent is used；
Step (II) described water at low temperature inversely participates in the multistage heat exchange, high-temperature water, saturated vapor and overheat is obtained successively and is steamed
Vapour, the superheated steam is used as step (II) described gasifying agent；
(V) after the low temperature combustion gas being removed into fine solid particle, cooling, desulfurizing and purifying, net combustion gas is obtained final product.
2. method according to claim 1, it is characterised in that step (III) described flying dust as gasified raw material, by step
Suddenly (II) is circulated pyrolytic gasification.
3. method according to claim 1, it is characterised in that the temperature of step (II) described gasifying agent is 500~650
℃；The temperature of the one-level pyrolytic gasification is 850~950 DEG C, and two grades of temperature of pyrolytic gasification are 950~1100 DEG C.
4. the method according to claims 1 to 3 any one, it is characterised in that step (IV) the multistage heat exchange tool
Body is：By the high-temperature fuel gas of primary purification successively with air at room temperature, 150~200 DEG C of saturated vapor, 95~200 DEG C of high temperature
Water and 60~100 DEG C of water at low temperature carry out multistage heat exchange, and it is 450 that combustion gas, temperature that temperature is 650~750 DEG C are obtained successively
~500 DEG C of combustion gas, the combustion gas that temperature is 250~300 DEG C and the low temperature combustion gas that temperature is 150~200 DEG C.
5. method according to claim 4, it is characterised in that step (II) described water at low temperature is 60~100 DEG C；
Described 60~100 DEG C of water at low temperature inversely participates in step (IV) the multistage heat exchange, and 95~200 DEG C of height is obtained successively
Warm water, 150~200 DEG C of saturated vapor and 500~650 DEG C of superheated steam, the superheated steam is used as step (II) Suo Shu
Gasifying agent is used.
6. a kind of device for preparing combustion gas as raw material with dirty coal, it is characterised in that described device includes successively being linked in sequence
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
Air cooling unit and gas desulfurization unit；
The pretreatment unit includes connected breaker (1) and screening plant (2)；
The gasification gas making unit includes gas unit (3) processed；Comprising connected one-level gasifier and two in the gas unit (3) processed
Level gasifier, the one-level gasifier is connected with screening plant (2)；
Described high-temperature fuel gas dust removing units include high-temperature dust removal unit (4), and with two grades of gasifier phases of gas unit (3) processed
Even；High-temperature dust removal unit (4) is also connected by flying dust circulating line (a) with gas unit (3) processed；The high-temperature dust removal unit (4)
In include high-temperature cyclone dust extractor；
The high-temperature fuel gas waste heat recovery unit include be linked in sequence successively air preheater (5), superheated steam unit (6),
Saturated vapor unit (7) and economizer (8)；Air preheater (5) is provided with air inlet；The air preheater (5) is also led to
Air gasification agent pipeline (b) is crossed to be connected with gas unit (3) processed；
The combustion gas dust removing units include nonaqueous dust cleaner (9)；
The combustion gas cooling unit includes indirect cooler (10)；
The gas desulfurization unit includes desulfurizer (11).
7. device according to claim 6, it is characterised in that described device also includes high-temperature ash waste heat recovery unit；
The high temperature recrement waste heat recovery unit includes lime-ash cooling unit (12)；The lime-ash cooling unit (12) is provided with cold ash
Slag is exported；
Gas unit (3) processed is connected by lime-ash cooling pipe (c) with lime-ash cooling unit (12).
8. device according to claim 7, it is characterised in that the lime-ash cooling unit (12) is provided with and softens entering for cold water
The mouth of a river；
The lime-ash cooling unit (12) also passes through steam gasification agent pipeline (d), successively via economizer (8), saturated vapor list
First (7) and superheated steam unit (6), are connected with gas unit (3) processed.
9. the method according to claim 1,2,3 or 5, it is characterised in that using described in claim 6~8 any one
Device prepares combustion gas.
10. method according to claim 4, it is characterised in that utilize claim 6~8 any one described device system
Standby combustion gas.
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| CN105462619A (en) * | 2015-12-31 | 2016-04-06 | 大连科林能源工程技术开发有限公司 | Gasification process system for urban household garbage and industrial organic solid waste |
| CN107841344A (en) * | 2017-11-14 | 2018-03-27 | 华电电力科学研究院 | A kind of power-plant flue gas produces the system and method for combustion gas with carbon-based solid fuel reaction |
| CN210595945U (en) * | 2018-11-22 | 2020-05-22 | 上海境业环保能源科技股份有限公司 | Coal gas multi-pollution-source integrated treatment system with dividing wall type cooler |
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