CN108795502A - A kind of dry coal powder airflow bed gasification system of low pressure and method - Google Patents
A kind of dry coal powder airflow bed gasification system of low pressure and method Download PDFInfo
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- CN108795502A CN108795502A CN201810956373.4A CN201810956373A CN108795502A CN 108795502 A CN108795502 A CN 108795502A CN 201810956373 A CN201810956373 A CN 201810956373A CN 108795502 A CN108795502 A CN 108795502A
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- 238000002309 gasification Methods 0.000 title claims abstract description 157
- 239000003245 coal Substances 0.000 title claims abstract description 102
- 239000000843 powder Substances 0.000 title claims abstract description 47
- 238000000034 method Methods 0.000 title claims description 15
- 239000010881 fly ash Substances 0.000 claims abstract description 58
- 239000000428 dust Substances 0.000 claims abstract description 43
- 239000002893 slag Substances 0.000 claims abstract description 35
- 238000005201 scrubbing Methods 0.000 claims abstract description 34
- 230000005855 radiation Effects 0.000 claims abstract description 31
- 239000002699 waste material Substances 0.000 claims abstract description 31
- 238000001816 cooling Methods 0.000 claims abstract description 27
- 238000002485 combustion reaction Methods 0.000 claims abstract description 24
- 239000007789 gas Substances 0.000 claims description 147
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 38
- 239000002956 ash Substances 0.000 claims description 33
- 239000007787 solid Substances 0.000 claims description 29
- 239000002817 coal dust Substances 0.000 claims description 28
- 239000002245 particle Substances 0.000 claims description 27
- 238000009434 installation Methods 0.000 claims description 18
- 239000008187 granular material Substances 0.000 claims description 17
- 239000012535 impurity Substances 0.000 claims description 16
- 238000006243 chemical reaction Methods 0.000 claims description 15
- 239000007800 oxidant agent Substances 0.000 claims description 14
- 230000001590 oxidative effect Effects 0.000 claims description 14
- 238000006477 desulfuration reaction Methods 0.000 claims description 10
- 230000023556 desulfurization Effects 0.000 claims description 10
- 238000000926 separation method Methods 0.000 claims description 10
- 239000000567 combustion gas Substances 0.000 claims description 9
- 238000005406 washing Methods 0.000 claims description 8
- 239000010797 grey water Substances 0.000 claims description 7
- 238000002156 mixing Methods 0.000 claims description 7
- 239000000203 mixture Substances 0.000 claims description 7
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 6
- 239000003795 chemical substances by application Substances 0.000 claims description 6
- 239000001301 oxygen Substances 0.000 claims description 6
- 229910052760 oxygen Inorganic materials 0.000 claims description 6
- 230000003647 oxidation Effects 0.000 claims description 5
- 238000007254 oxidation reaction Methods 0.000 claims description 5
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims description 4
- -1 during this Substances 0.000 claims description 4
- 239000002737 fuel gas Substances 0.000 claims description 4
- 239000001257 hydrogen Substances 0.000 claims description 4
- 229910052739 hydrogen Inorganic materials 0.000 claims description 4
- 239000000463 material Substances 0.000 claims description 2
- 238000005516 engineering process Methods 0.000 abstract description 11
- 239000003034 coal gas Substances 0.000 description 14
- 238000004519 manufacturing process Methods 0.000 description 8
- 210000004027 cell Anatomy 0.000 description 7
- 230000008859 change Effects 0.000 description 4
- 238000007599 discharging Methods 0.000 description 4
- 230000008901 benefit Effects 0.000 description 3
- 239000012530 fluid Substances 0.000 description 3
- 239000000155 melt Substances 0.000 description 3
- 230000009182 swimming Effects 0.000 description 3
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 2
- 230000033228 biological regulation Effects 0.000 description 2
- 230000015572 biosynthetic process Effects 0.000 description 2
- 230000000903 blocking effect Effects 0.000 description 2
- 229910052799 carbon Inorganic materials 0.000 description 2
- 239000002360 explosive Substances 0.000 description 2
- 238000012423 maintenance Methods 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 239000011819 refractory material Substances 0.000 description 2
- 238000003786 synthesis reaction Methods 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- 235000002918 Fraxinus excelsior Nutrition 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
- CUZMQPZYCDIHQL-VCTVXEGHSA-L calcium;(2s)-1-[(2s)-3-[(2r)-2-(cyclohexanecarbonylamino)propanoyl]sulfanyl-2-methylpropanoyl]pyrrolidine-2-carboxylate Chemical group [Ca+2].N([C@H](C)C(=O)SC[C@@H](C)C(=O)N1[C@@H](CCC1)C([O-])=O)C(=O)C1CCCCC1.N([C@H](C)C(=O)SC[C@@H](C)C(=O)N1[C@@H](CCC1)C([O-])=O)C(=O)C1CCCCC1 CUZMQPZYCDIHQL-VCTVXEGHSA-L 0.000 description 1
- 239000001569 carbon dioxide Substances 0.000 description 1
- 229910002092 carbon dioxide Inorganic materials 0.000 description 1
- 239000000919 ceramic Substances 0.000 description 1
- 239000003250 coal slurry Substances 0.000 description 1
- 230000000052 comparative effect Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- JCXJVPUVTGWSNB-UHFFFAOYSA-N nitrogen dioxide Inorganic materials O=[N]=O JCXJVPUVTGWSNB-UHFFFAOYSA-N 0.000 description 1
- QJGQUHMNIGDVPM-UHFFFAOYSA-N nitrogen group Chemical group [N] QJGQUHMNIGDVPM-UHFFFAOYSA-N 0.000 description 1
- 230000000149 penetrating effect Effects 0.000 description 1
- 230000021715 photosynthesis, light harvesting Effects 0.000 description 1
- 230000008569 process Effects 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 230000006641 stabilisation Effects 0.000 description 1
- 238000011105 stabilization Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 210000000635 valve cell Anatomy 0.000 description 1
- 239000002918 waste heat Substances 0.000 description 1
- 239000002351 wastewater Substances 0.000 description 1
Classifications
-
- 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
- C10J3/48—Apparatus; Plants
- C10J3/50—Fuel charging devices
- C10J3/506—Fuel charging devices for 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
- C10J3/48—Apparatus; Plants
- C10J3/52—Ash-removing devices
- C10J3/526—Ash-removing devices for 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
- C10J3/72—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
- C10J3/74—Construction of shells or jackets
- C10J3/76—Water jackets; Steam boiler-jackets
-
- 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
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/72—Other features
- C10J3/86—Other features combined with waste-heat boilers
-
- 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
- C10J2200/00—Details of gasification apparatus
- C10J2200/15—Details of feeding means
- C10J2200/152—Nozzles or lances for introducing gas, liquids or suspensions
-
- 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
- C10J2300/16—Integration of gasification processes with another plant or parts within the plant
- C10J2300/1603—Integration of gasification processes with another plant or parts within the plant with gas treatment
- C10J2300/1615—Stripping
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
- Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
Landscapes
- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Combustion & Propulsion (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Organic Chemistry (AREA)
- Gasification And Melting Of Waste (AREA)
Abstract
The invention discloses a kind of dry coal powder airflow bed gasification systems of low pressure, it includes pulverized coal bin, dosing valve, convey mixer, gasification furnace, gasification burner tip, fly ash separator, convection current is given up pot, flying dust washer, scrubbing tower and desulfurizer, pulverized coal bin is connected by dosing valve with conveying mixer, conveying mixer is connected with gasification burner tip, gasification burner tip is mounted on top of gasification furnace, gasification furnace is by gasification combustion chamber, radiation waste pot, slag bath forms, gasification combustion chamber, the side wall of the radiation waste pot and the slag bath is made of water-cooling wall, radiation waste pot side wall is equipped with the first gas exit, first gas exit is connected with the first gas entry of fly ash separator, second gas exit of fly ash separator and the useless pot of convection current, flying dust washer, scrubbing tower and desulfurizer are sequentially connected.The present invention solves the problems, such as that high equipment cost present in existing dry coal powder airflow bed gasification technology, dry pulverized coal feed stability difference are low with integrated heat efficiency.
Description
Technical field
The present invention relates to coal gas technology fields, and in particular to a kind of dry coal powder airflow bed gasification system of low pressure and side
Method.
Background technology
Industrial combustion gas is mainly used in the burning occasion of normal pressure or low pressure, the industrial combustion gas field in China, due to natural
It gas shortage of resources and is influenced by combustion gas cost, mainly generates coal gas using coal gasification, for meeting ceramics, metallurgical, papermaking
Etc. industries demand on gas.Compared with fixed bed and the coal gasification mode of fluid bed, air-flow bed coal-gasification has efficiency of carbon con version high
The advantages that disposable with coal gasification waste water, receives more and more attention under the trend of energy-saving and emission-reduction.Air-flow bed coal-gasification point
Two ways is fed for water-coal-slurry charging and dry pulverized coal, high, oxygen consumes low advantage, dry coal with cold gas efficiency for dry pulverized coal charging
Powder airflow bed Coal Gasification Technology is suitable for coal gas burning field.
The dry coal powder airflow bed Coal Gasification Technology of industrial comparative maturity includes Shell Coal Gasification Technologies and GSP coals at present
Gasification technology is mainly used in field chemical industry synthesis (about 4MPa) of high pressure, belongs to high-pressure system, however high-pressure system no matter
Device fabrication still during operation, all haves the shortcomings that of high cost, risk is high, if being directly applied to the combustion of low pressure coal system
There will be following disadvantages in gas field：(1) pulverized coal conveying device uses normal pressure powder cabin-lock hopper-high pressure powder cabin form, gasification furnace to use
Pressure-bearing box hat and water wall structure, gasification furnace slag discharge use lock hopper structure, these settings cause apparatus structure complicated, equipment manufacturing cost
It is high；(2) for dry pulverized coal feed using material issuing tank fluidizing type feed and pneumatic conveying method, dry pulverized coal feed stability is poor, influences gas
Change the stable operation of stove；(3) coal gas of high temperature Exposure degree is incomplete, causes energy dissipation, the synthesis thermal effect that coal combustion gas utilizes
Rate is low.
Invention content
It is as follows to solve the purpose of the present invention is to provide a kind of dry coal powder airflow bed gasification system of low pressure and method
Problem：(1) the powder airflow bed coal combustion gas of high pressure dry coal is of high cost, risk is high；(2) high pressure dry coal it is powder airflow bed directly apply to it is low
Press coal combustion gas when, high equipment cost, dry pulverized coal feed stability it is poor, gasifier operation stability is poor, Exposure degree rate is low,
Integrated heat efficiency is low.
To achieve the above object, the present invention provides a kind of dry coal powder airflow bed gasification systems of low pressure comprising coal dust
Storehouse, dosing valve, conveying mixer, gasification furnace, gasification burner tip, fly ash separator and the useless pot of convection current, the pulverized coal bin are logical
It crosses the dosing valve to connect with the first coal powder entrance of the conveying mixer, the dosing valve is rotary valve, institute
State conveying mixer be venturi mixer, the gasification furnace include the gasification combustion chamber for being arranged and being sequentially communicated from top to bottom,
Radiation waste pot and slag bath, the gasification burner tip are mounted on the top of the gasification combustion chamber and connect with the gasification combustion chamber
Logical, the second coal powder entrance of the gasification burner tip is connect with the second discharge of the conveying mixer, is fired in the gasification
The side wall for burning room is externally provided with water-cooling wall a, water-cooling wall b is externally provided in the side wall of the radiation waste pot, outside the side wall of the slag bath
Equipped with water-cooling wall c, it is equipped with the first gas exit in the sidewall bottom of the radiation waste pot, the first coal gas of the radiation waste pot goes out
Mouth is connect with the first gas entry of the fly ash separator, and the second gas exit of the fly ash separator and the convection current are useless
The second gas entry connection of pot, the fly ash separator are cyclone separator.
In certain pressure differential range, rotary valve can be by the pulverized coal bin in normal pressure and described defeated in low pressure
It send mixer to keep apart, avoids gas from being leapt up into the pulverized coal bin by the conveying mixer is counter, influence coal dust feed.This
Outside, it is rotated by the steady and continuous of cell compartment in rotary valve, coal dust uniformly continuous feed may be implemented, by the rotation for adjusting cell compartment
Speed can adjust coal dust delivery rate.
In venturi mixer, conveying gas is accelerated, the conveying gas of high speed due to local constriction in flow area
It is sufficiently mixed with the pulverized coal particle for entering venturi mixer, avoids pulverized coal particle and assemble blocking pipeline in the duct.In addition,
Pressure in venturi mixer is reduced due to the raising of local gas velocity, to reduce the work pressure of the dosing valve
Difference reduces its gas blowby possibility.
Cyclone separator separates most of ash particle in coal gas, reduces dust content of gas, that is, avoids flying dust
Grain is deposited in subsequent pipeline and is blocked, and can improve the coefficient of heat transfer and waste heat recovery rate, while reducing the negative of subsequent wet dedusting
Lotus.Preferably, cyclone separator is made of the water wall structure of interior deposited wearing-proof refractory material.
Wherein, the gasification burner tip is equipped with multiple, top array of multiple gasification burner tips in the gasification combustion chamber
Distribution.Since vapor pressure is relatively low, coal gasification reaction rate is relatively low, can strengthen gas-solid by the way that multiple gasification burner tips are arranged
Contact and mixing, improve gas-solid reaction rate, reduce due to the relatively low influence to gasification reaction rate of pressure.
Wherein, the water-cooling wall of the gasification combustion chamber, the radiation waste pot and the slag bath is integral type water-cooling wall.One
Formula water-cooling wall manufactures, is easy to installation and maintenance, and one body swimming cold wall can be born between low pressure gasifying furnace interior and external environment
Pressure difference, due to eliminating the pressure-bearing box hat in high pressure coal gasification technology, to reduce integrated gasification stove manufacturing cost.
Wherein, it being exported equipped with pulp water in the bottom of the slag bath, the pulp water outlet of the slag bath is connect with deslagging water installations,
The deslagging water installations are angle valve.Angle valve can bear the gasification furnace slag bath and external pressure difference, and can continuously arrange
The pulp water in bottom of pond of slagging tap portion.By the aperture regulation gasification furnace slag discharge rate for adjusting angle valve.Due to eliminating high pressure coal gasification skill
Intermittent lock hopper system in art reduces integrated gasification stove manufacturing cost to simplify deslagging water system.
Wherein, it is equipped with ash in the bottom of the fly ash separator to export, the ash outlet of the fly ash separator and ash-valve
Connection, the ash-valve are rotary valve.Rotary valve can by low pressure the fly ash separator and external atmospheric pressure environment every
It leaves, avoids inflammable and explosive coal gas from being leaked from fly ash separator and safety accident occurs.In addition, passing through cell compartment in rotary valve
Steady and continuous rotates, and the discharge of ash particle uniformly continuous may be implemented can be adjusted by adjusting the speed of rotation of rotary valve cell compartment
Ash discharge rate.
Wherein, the dry coal powder airflow bed gasification system of the low pressure further includes flying dust washer, scrubbing tower and desulfurization dress
It sets, the flying dust washer is Venturi scrubber, third gas entry and the useless pot of the convection current of the flying dust washer
Third gas exit connects, and the 4th gas exit of the flying dust washer is connect with the 4th gas entry of the scrubbing tower,
5th gas exit of the scrubbing tower is connect with the 5th gas entry of the desulfurizer, on the side wall top of the scrubbing tower
Portion is equipped with washing water inlet, and gray water outlet is equipped in the bottom of the scrubbing tower.
The present invention also provides a kind of methods of low pressure dry coal powder airflow bed coal-gasification, use above-mentioned low pressure dry pulverized coal
Entrained-flow coal gasification system includes the following steps：
Step 1, the low pressure supply of coal dust；
Coal dust in pulverized coal bin under normal pressure state is passed through the conveying mixer under low-pressure state by dosing valve, it is fixed
Amount feed valve is continuously and uniformly fed while pulverized coal bin and conveying mixer is isolated, coal dust in conveying mixer with from defeated
The conveying gas that the conveying gas entrance of mixer enters is sent to be sent into gasification burner tip after evenly mixing；
Step 2, gasification reaction and first time Exposure degree；
Coal dust is passed through gasification furnace, the oxidation that simultaneous oxidation agent passes through gasification burner tip by the second coal powder entrance of gasification burner tip
Agent entrance is passed through gasification furnace, and gasification reaction occurs in the gasification, and combustion room on gasification furnace top and generates raw gas, during this,
Ash content in coal dust melts in an environment of high temperature becomes grey solid impurity particle, and raw gas and grey solid impurity particle carry a large amount of sensible heats and be passed through gas
Change the radiation waste pot in the middle part of stove, and carries out first time Exposure degree in radiation waste pot and make raw gas and grey solid impurity particle cooling drop
Temperature, the larger solid impurity particle of grain size fall into the slag bath of gasification furnace bottom, and the raw gas of entrainment small particle fly ash granule passes through radiation waste
First gas exit of pot sidewall bottom is passed through fly ash separator；
Step 3, gas solid separation；
Raw gas and fly ash granule carry out gas solid separation in fly ash separator, and wherein most fly ash granule passes through flying dust
The ash outlet discharge of separator, raw gas are passed through the useless pot of convection current by the second gas exit of fly ash separator；
Step 4, second of Exposure degree and washing；
Raw gas carries out second of Exposure degree in pot is given up in convection current, and the raw gas after cooling is passed through flying dust washer, slightly
Flying dust in coal gas is captured in flying dust washer, and the flying dust to get off that is captured is passed through scrubbing tower together with raw gas,
Remaining flying dust is further captured in scrubbing tower in raw gas, and raw gas is passed through after being washed thoroughly in scrubbing tower
Desulfurizer, the grey aqueous mixtures in scrubbing tower are discharged by gray water outlet；
Step 5, desulfurization；
After raw gas is by desulfurizer desulfurization, clean gas is made.
In step 1, pulverized coal flow is adjusted by adjustment quantitative feed valve, to adjust the load of coal combustion gas.
In step 2, oxidant is the mixture of oxygen and vapor, by the volume point for changing vapor in oxidant
Number can adjust hydrogen content and calorific value in fuel gas；Pulp water in slag bath is continuously discharged by deslagging water installations, is passed through
Deslagging water installations are adjusted to adjust gasification furnace slag discharge rate.
In step 3, pass through the ash-valve with ash outlet connection from the fly ash granule of the ash outlet discharge of fly ash separator
Discharge, by adjusting ash-valve to adjust ash discharge rate.
The invention has the advantages that：
(1) a kind of dry coal powder airflow bed gasification system and method for low pressure are provided, high-pressure system is not used, reduces
Cost and risk；(2) pulverized coal conveying device, gasification furnace structure and gasification furnace slag discharge system are simplified, eliminates high pressure
The lock hopper and high pressure powder cabin equipment used in dry coal powder airflow bed Coal Gasification Technology, eliminates gasification furnace pressure-bearing box hat structure, takes
Disappeared gasification furnace slag discharge lock hopper, to save equipment investment, reduces equipment manufacturing cost；(3) coal dust feed-type is optimized, is used
Dosing valve and conveying mixer mode are fed, and feed is stablized, reliability is high, easy to operate, improves the stability of gasification furnace；
(4) coal gas of high temperature sensible heat is recycled by radiation waste pot and the useless pot of convection current completely, improves Exposure degree rate, integrated heat efficiency is high.
Description of the drawings
Fig. 1 is the structural schematic diagram for the dry coal powder airflow bed gasification system of low pressure that embodiment 1 provides.
Fig. 2 is the flow chart for the dry coal powder airflow bed coal gasification method of low pressure that embodiment 2 provides.
In figure：100- pulverized coal bins, the first discharges of 110-, 200- dosing valves, 210- pan feeding valve ports, 220- dischargings
Valve port, 300- convey mixer, the first coal powder entrances of 310-, and 320- conveys gas entrance, the second discharges of 330-, 400- gasifications
Burner, the second coal powder entrances of 410-, 420- oxidant inlets, 500- gasification furnaces, 510- gasification combustion chamber, 511- water-cooling wall a,
520- radiation waste pots, the first gas exit of 521- water-cooling walls b, 522-, 530- slag baths, the outlet of 531- water-cooling walls c, 532- pulp water,
600- deslagging water installations, 610- inlets, 620- leakage fluid drams, 700- fly ash separators, the first gas entries of 710-, 720- ashes go out
Mouthful, the second gas exits of 730-, 800- ash-valves, 810- ash inlets, 820- ash discharging holes, 900- convection current gives up pot, the second coals of 910-
Gas entrance, 920- third gas exits, 1000- flying dust washers, 1010- third gas entries, the 4th gas exits of 1020-,
1100- scrubbing towers, the 4th gas entries of 1110-, the washing water inlets 1120-, 1130- gray water outlets, the 5th coal gas of 1140- go out
Mouthful, 1200- desulfurizers, the 5th gas entries of 1210-, the 6th gas exits of 1220-.
Specific implementation mode
The following examples are used to illustrate the present invention, but are not intended to limit the scope of the present invention..
Embodiment 1
As shown in Figure 1, embodiment 1 provides a kind of dry coal powder airflow bed gasification system of low pressure comprising pulverized coal bin
100, dosing valve 200, conveying mixer 300, gasification furnace 500, gasification burner tip 400, fly ash separator 700, the useless pot of convection current
900, flying dust washer 1000, scrubbing tower 1100 and desulfurizer 1200 are equipped with the first coal in the bottom of the pulverized coal bin 100
Powder outlet 110, the first discharge 110 is connect with the pan feeding valve port 210 of the dosing valve 200, dosing valve 200
Discharging valve port 220 is connect with the first coal powder entrance 310 of the conveying mixer 300, and the dosing valve 200 is rotation
Valve, the conveying mixer 300 are venturi mixer, and the gasification furnace 500 includes being arranged and being sequentially communicated from top to bottom
Gasification combustion chamber 510, radiation waste pot 520 and slag bath 530, the gasification burner tip 400 are mounted on the gasification combustion chamber 510
Top is simultaneously connected to the gasification combustion chamber 510, and the second coal powder entrance 410 of the gasification burner tip 400 is mixed with the conveying
Second discharge 330 of device 300 connects, and water-cooling wall a511 is externally provided in the side wall of the gasification combustion chamber 510, in the spoke
The side wall for penetrating useless pot 520 is externally provided with water-cooling wall b521, water-cooling wall c531 is externally provided in the side wall of the slag bath 530, in the spoke
Penetrate useless pot 520 sidewall bottom be equipped with the first gas exit 522, the first gas exit 522 of the radiation waste pot 520 with it is described
First gas entry 710 of 700 side wall upper part of fly ash separator connects, and second coal gas at 700 top of the fly ash separator goes out
Mouth 730 is connect with second gas entry 910 at useless 900 top of pot of the convection current, and the fly ash separator 700 is cyclonic separation
Device is made of the water wall structure of interior deposited wearing-proof refractory material, and the flying dust washer 1000 is Venturi scrubber, described to fly
The give up third gas exit 920 of pot 900 of the third gas entry 1010 of grey washer 1000 and the convection current is connect, the flying dust
4th gas exit 1020 of washer 1000 is connect with the 4th gas entry 1110 of 1100 sidewall bottom of the scrubbing tower, institute
The 5th gas exit 1140 for stating scrubbing tower 1100 is connect with the 5th gas entry 1210 of the desulfurizer 1200, in desulfurization
The top of device 1200 is equipped with the 6th gas exit 1220, and the 6th gas exit 1220 connects with gas pipeline (not shown)
It connects, is equipped with washing water inlet 1120 in the top side wall of the scrubbing tower 1100, ash is equipped in the bottom of the scrubbing tower 1100
Water out 1130.
In the present embodiment, conveying mixer 300 is additionally provided with conveying gas entrance 320, conveying gas entrance 320 and conveying gas
Pipeline (not shown) connects, and it is nitrogen or carbon dioxide to convey the conveying gas in feed channel.
In the present embodiment, gasification burner tip 400 is additionally provided with oxidant inlet 420, oxidant inlet 420 and oxidant conduit
(not shown) connects, and oxidant is the mixture of oxygen and vapor.
In the present embodiment, the gasification burner tip 400 is equipped with multiple, and multiple gasification burner tips 400 are fired in the gasification
The top array distribution of room 510 is burnt, since the pressure of gasification reaction is relatively low, coal gasification reaction rate is relatively low, multiple by being arranged
Gasification burner tip 400 can strengthen gas-solid contact and mixing, improve gas-solid reaction rate, reduce since pressure is relatively low to gasification reaction
The influence of rate.
In the present embodiment, the water-cooling wall of the gasification combustion chamber 510, the radiation waste pot 520 and the slag bath 530 is
One body swimming cold wall, the manufacture of one body swimming cold wall, installation and easy to maintenance, can bear the inside of low pressure gasifying stove 500 and
Pressure difference between external environment, due to eliminating the pressure-bearing box hat in high pressure coal gasification technology, to reduce integrated gasification
500 manufacturing cost of stove.
In the present embodiment, it is equipped with pulp water in the bottom of the slag bath 530 and exports 532, the pulp water outlet of the slag bath 530
532 connect with the inlet 610 of deslagging water installations 600, and leakage fluid dram 620, the deslagging are equipped in the bottom of deslagging water installations 600
Water installations 600 are angle valve, and deslagging water installations 600 can bear the slag bath 530 of 500 bottom of gasification furnace and external pressure difference, and
The pulp water of 530 bottom of slag bath can continuously be discharged, the aperture regulation by adjusting deslagging water installations 600 (angle valve) 600 gasifies
The deslagging rate of stove 500, due to eliminating the intermittent lock hopper system in high pressure coal gasification technology, to simplify deslagging water
System reduces 500 manufacturing cost of gasification furnace.
In the present embodiment, ash outlet 720, the fly ash separator 700 are equipped in the bottom of the fly ash separator 700
Ash outlet 720 connect with the ash inlet 810 of ash-valve 800, the bottom of ash-valve 800 is equipped with ash discharging hole 820, the ash-valve
800 be that rotary valve, raw gas and fly ash granule carry out gas solid separation, wherein most fly ash granule in fly ash separator 700
It by 720 discharge of ash outlet of fly ash separator 700, and is discharged by ash-valve 800, wherein ash-valve 800 can will be in
The fly ash separator 700 of low pressure and external atmospheric pressure environment are kept apart, and inflammable and explosive coal gas is avoided to be let out from fly ash separator 700
Safety accident occurs for leakage, in addition, the steady and continuous by the cell compartment in ash-valve 800 rotates, ash particle may be implemented and uniformly connect
Continuous discharge can adjust ash discharge rate by adjusting the speed of rotation of cell compartment.
When system works, the coal dust in pulverized coal bin 100 is passed through conveying mixer 300 by dosing valve 200,
In 10bar pressure differential ranges, dosing valve 200 can be by the pulverized coal bin 100 in normal pressure and the conveying mixer in low pressure
300 keep apart, and gas is avoided to be leapt up into pulverized coal bin 100 by conveying mixer 300 is counter, influence coal dust feed, in addition, by fixed
Coal dust uniformly continuous feed may be implemented in stabilization, the continuous rotation for measuring the cell compartment in feed valve 200, by the rotation for adjusting cell compartment
Rotary speed can adjust coal dust delivery rate.
In conveying mixer 300, conveying gas is due to local constriction in flow area (conveying 300 internal structure of mixer
Cause) and be accelerated, the conveying gas of high speed is sufficiently mixed with the pulverized coal particle for entering conveying mixer 300, avoids coal dust
Particle is assembled in the duct blocks pipeline, in addition, the pressure in conveying mixer 300 is reduced due to the raising of local gas velocity,
To reduce the operting differential pressure of dosing valve 200, reduce its gas blowby possibility, coal dust in conveying mixer 300 with it is defeated
It supplies gas and is sent into gasification burner tip 400 after mixing.
Coal dust and oxidant are passed through gasification furnace 500 by gasification burner tip 400, in the gasification combustion chamber 510 of gasification furnace 500
Gasification reaction occurs and generates raw gas, the ash content in coal dust melts in an environment of high temperature becomes grey solid impurity particle, wherein oxidant
In vapor volume fraction be 0~50%, by change vapor volume fraction can adjust the hydrogen content in fuel gas.
Raw gas and grey solid impurity particle are passed through in the radiation waste pot 520 of gasification furnace 500 and cool to 700~800 DEG C, in cooling procedure
In, the water-cooling wall of radiation waste pot 520 carries out first time Exposure degree, and the larger grey solid impurity particle of grain size falls into 500 bottom of gasification furnace
Slag bath 530, entrainment small particle fly ash granule raw gas flying dust is passed through by the first gas exit 522 of radiation waste pot 520
Separator 700.
Raw gas and fly ash granule carry out gas solid separation in fly ash separator 700, and the raw gas after gas solid separation passes through
Second gas exit 730 of fly ash separator 700 is passed through convection current and gives up pot 900.Fly ash separator 700 is by most of grey in coal gas
Grain separates, and reduces dust content of gas, that is, avoids fly ash granule and deposit blocking in subsequent pipeline, and can improve heat exchange system
Number and Exposure degree rate, while reducing the load of subsequent wet dedusting.
Raw gas is passed through flying dust washer 1000 after being further cooled to 200~300 DEG C during pot 900 is given up in convection current, cooling
Second of Exposure degree is carried out in the process, and the flying dust in raw gas is captured in flying dust washer 1000, is captured down
The flying dust come is passed through scrubbing tower 1100 together with raw gas, and remaining flying dust is further caught in scrubbing tower 1100 in raw gas
It catches, raw gas is passed through desulfurizer 1200 after fully washing in scrubbing tower 1100, the buck mixing in scrubbing tower 1100
Object is discharged by gray water outlet 1130, and after raw gas is by 1200 desulfurization of desulfurizer, clean gas is made.
Embodiment 2
As shown in Fig. 2, embodiment 2 provides a kind of method of low pressure dry coal powder airflow bed coal-gasification, it makes use of implementations
The dry coal powder airflow bed gasification system of low pressure in example 1 comprising following steps：
Step 1, the low pressure supply of coal dust；
Coal dust in pulverized coal bin under normal pressure state is passed through the conveying mixer under low-pressure state by dosing valve, it is fixed
Amount feed valve is continuously and uniformly fed while pulverized coal bin and conveying mixer is isolated, coal dust in conveying mixer with from defeated
The conveying gas that the conveying gas entrance of mixer enters is sent to be sent into gasification burner tip after evenly mixing；
Step 2, gasification reaction and first time Exposure degree；
Coal dust is passed through gasification furnace, the oxidation that simultaneous oxidation agent passes through gasification burner tip by the second coal powder entrance of gasification burner tip
Agent entrance is passed through gasification furnace, and gasification reaction occurs in the gasification, and combustion room on gasification furnace top and generates raw gas, during this,
Ash content in coal dust melts in an environment of high temperature becomes grey solid impurity particle, and raw gas and grey solid impurity particle carry a large amount of sensible heats and be passed through gas
Change the radiation waste pot in the middle part of stove, and carries out first time Exposure degree in radiation waste pot and make raw gas and grey solid impurity particle cooling drop
Temperature, the larger solid impurity particle of grain size fall into the slag bath of gasification furnace bottom, and the raw gas of entrainment small particle fly ash granule passes through radiation waste
First gas exit of pot sidewall bottom is passed through fly ash separator；
Step 3, gas solid separation；
Raw gas and fly ash granule carry out gas solid separation in fly ash separator, and wherein most fly ash granule passes through flying dust
The ash outlet discharge of separator, raw gas are passed through the useless pot of convection current by the second gas exit of fly ash separator；
Step 4, second of Exposure degree and washing；
Raw gas carries out second of Exposure degree in pot is given up in convection current, and the raw gas after cooling is passed through flying dust washer, slightly
Flying dust in coal gas is captured in flying dust washer, and the flying dust to get off that is captured is passed through scrubbing tower together with raw gas,
Remaining flying dust is further captured in scrubbing tower in raw gas, and raw gas is passed through after being washed thoroughly in scrubbing tower
Desulfurizer, the grey aqueous mixtures in scrubbing tower are discharged by gray water outlet；
Step 5, desulfurization；
After raw gas is by desulfurizer desulfurization, clean gas is made.
In step 1, pulverized coal flow is adjusted by adjustment quantitative feed valve, to adjust the load of coal combustion gas.
In step 2, oxidant is the mixture of oxygen and vapor, by the volume point for changing vapor in oxidant
Number can adjust hydrogen content and calorific value in fuel gas；Pulp water in slag bath is continuously discharged by deslagging water installations, is passed through
Deslagging water installations are adjusted to adjust gasification furnace slag discharge rate.
In step 2, the vapor volume fraction in oxidant is 0~50%.
In step 2, raw gas and grey solid impurity particle are passed through in the radiation waste pot of gasification furnace and cool to 700~800 DEG C.
In step 3, pass through the ash-valve with ash outlet connection from the fly ash granule of the ash outlet discharge of fly ash separator
Discharge, by adjusting ash-valve to adjust ash discharge rate.
In step 4, raw gas is cooled to 200~300 DEG C in pot is given up in convection current.
Although above having used general explanation and specific embodiment, the present invention is described in detail, at this
On the basis of invention, it can be made some modifications or improvements, 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 belong to the scope of protection of present invention.
Claims (10)
1. a kind of dry coal powder airflow bed gasification system of low pressure, which is characterized in that the low pressure dry coal powder airflow bed coal-gasification system
System include pulverized coal bin (100), dosing valve (200), convey mixer (300), gasification furnace (500), gasification burner tip (400),
Fly ash separator (700) and convection current are given up pot (900), the pulverized coal bin (100) by the dosing valve (200) with it is described
The first coal powder entrance (310) connection of mixer (300) is conveyed, the dosing valve (200) is rotary valve, and the conveying is mixed
Clutch (300) is venturi mixer, and the gasification furnace (500) includes the gasification combustion chamber for being arranged and being sequentially communicated from top to bottom
(510), radiation waste pot (520) and slag bath (530), the gasification burner tip (400) are mounted on the gasification combustion chamber (510)
Top is simultaneously connected to the gasification combustion chamber (510), the second coal powder entrance (410) of the gasification burner tip (400) with it is described defeated
It send the second discharge (330) of mixer (300) to connect, water-cooling wall a is externally provided in the side wall of the gasification combustion chamber (510)
(511), it is externally provided with water-cooling wall b (521) in the side wall of the radiation waste pot (520), is externally provided in the side wall of the slag bath (530)
Water-cooling wall c (531) is equipped with the first gas exit (522), the radiation waste pot in the sidewall bottom of the radiation waste pot (520)
(520) the first gas exit (522) is connect with the first gas entry (710) of the fly ash separator (700), the flying dust
The second gas exit (730) of separator (700) is connect with the second gas entry (910) of the useless pot (900) of the convection current, described
Fly ash separator (700) is cyclone separator.
2. the dry coal powder airflow bed gasification system of low pressure according to claim 1, which is characterized in that the gasification burner tip
(400) it is equipped with multiple, top array distribution of multiple gasification burner tips (400) in the gasification combustion chamber (510).
3. the dry coal powder airflow bed gasification system of low pressure according to claim 1, which is characterized in that the gasification combustion chamber
(510), the water-cooling wall of the radiation waste pot (520) and the slag bath (530) is integral type water-cooling wall.
4. the dry coal powder airflow bed gasification system of low pressure according to claim 1, which is characterized in that in the slag bath
(530) bottom is equipped with pulp water and exports (532), and pulp water outlet (532) and the deslagging water installations (600) of the slag bath (530) connect
It connects, the deslagging water installations (600) are angle valve.
5. the dry coal powder airflow bed gasification system of low pressure according to claim 1, which is characterized in that detached in the flying dust
The bottom of device (700) is equipped with grey outlet (720), and ash outlet (720) and the ash-valve (800) of the fly ash separator (700) connect
It connects, the ash-valve (800) is rotary valve.
6. the dry coal powder airflow bed gasification system of low pressure according to any one of claim 1-5, which is characterized in that institute
It further includes flying dust washer (1000), scrubbing tower (1100) and desulfurizer to state the dry coal powder airflow bed gasification system of low pressure
(1200), the flying dust washer (1000) is Venturi scrubber, the third gas entry of the flying dust washer (1000)
(1010) it is connect with the third gas exit (930) of the useless pot (900) of the convection current, the 4th coal of the flying dust washer (1000)
Gas outlet (1020) is connect with the 4th gas entry (1110) of the scrubbing tower (1100), and the 5th of the scrubbing tower (1100) the
Gas exit (1140) is connect with the 5th gas entry (1210) of the desulfurizer (1200), in the scrubbing tower (1100)
Top side wall be equipped with washing water inlet (1120), the bottom of the scrubbing tower (1100) be equipped with gray water outlet (1130).
7. a kind of method of low pressure dry coal powder airflow bed coal-gasification, dry using the low pressure described in any one of claim 1-6
Breeze airflow bed coal-gasification system, which is characterized in that include the following steps：
Step 1, the low pressure supply of coal dust；
Coal dust in pulverized coal bin under normal pressure state is passed through the conveying mixer under low-pressure state by dosing valve, is quantitatively given
Material valve is continuously and uniformly fed while pulverized coal bin and conveying mixer is isolated, and coal dust is mixed in conveying mixer and from conveying
The conveying gas that the conveying gas entrance of clutch enters is sent into gasification burner tip after evenly mixing；
Step 2, gasification reaction and first time Exposure degree；
Coal dust is passed through gasification furnace by the second coal powder entrance of gasification burner tip, and simultaneous oxidation agent is entered by the oxidant of gasification burner tip
Mouthful it is passed through gasification furnace, gasification reaction occurs in the gasification, and combustion room on gasification furnace top and generates raw gas, during this, coal dust
In ash content melt become grey solid impurity particle in an environment of high temperature, raw gas and grey solid impurity particle carry a large amount of sensible heats and are passed through gasification furnace
The radiation waste pot at middle part, and carry out first time Exposure degree in radiation waste pot and raw gas and grey solid impurity particle is made to cool,
The larger solid impurity particle of grain size falls into the slag bath of gasification furnace bottom, and the raw gas of entrainment small particle fly ash granule passes through radiation waste pot side
First gas exit of wall bottom is passed through fly ash separator；
Step 3, gas solid separation；
Raw gas and fly ash granule carry out gas solid separation in fly ash separator, and wherein most fly ash granule is detached by flying dust
The ash outlet discharge of device, raw gas are passed through the useless pot of convection current by the second gas exit of fly ash separator；
Step 4, second of Exposure degree and washing；
Raw gas carries out second of Exposure degree in pot is given up in convection current, and the raw gas after cooling is passed through flying dust washer, raw gas
In flying dust be captured in flying dust washer, the flying dust to get off that is captured is passed through scrubbing tower, rough coal together with raw gas
Remaining flying dust is further captured in scrubbing tower in gas, and raw gas is passed through desulfurization after being washed thoroughly in scrubbing tower
Device, the grey aqueous mixtures in scrubbing tower are discharged by gray water outlet；
Step 5, desulfurization；
After raw gas is by desulfurizer desulfurization, clean gas is made.
8. the method for low pressure dry coal powder airflow bed coal-gasification according to claim 7, which is characterized in that in step 1, lead to
Dosing valve is overregulated to adjust pulverized coal flow, to adjust the load of coal combustion gas.
9. the method for low pressure dry coal powder airflow bed coal-gasification according to claim 7, which is characterized in that in step 2, oxygen
Agent is the mixture of oxygen and vapor, and the volume fraction by changing vapor in oxidant can be adjusted in fuel gas
Hydrogen content and calorific value；Pulp water in slag bath is continuously discharged by deslagging water installations, is adjusted by adjusting deslagging water installations
Gasify furnace slag discharge rate.
10. the method for low pressure dry coal powder airflow bed coal-gasification according to claim 7, which is characterized in that in step 3,
It is discharged from the fly ash granule of the ash outlet discharge of fly ash separator by exporting the ash-valve of connection with ash, by adjusting ash-valve
To adjust ash discharge rate.
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Application publication date: 20181113 |