CN1031103A - A kind of gasification method of fluidizing power coal - Google Patents
A kind of gasification method of fluidizing power coal Download PDFInfo
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- CN1031103A CN1031103A CN 87105200 CN87105200A CN1031103A CN 1031103 A CN1031103 A CN 1031103A CN 87105200 CN87105200 CN 87105200 CN 87105200 A CN87105200 A CN 87105200A CN 1031103 A CN1031103 A CN 1031103A
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- coal
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E20/00—Combustion technologies with mitigation potential
- Y02E20/16—Combined cycle power plant [CCPP], or combined cycle gas turbine [CCGT]
- Y02E20/18—Integrated gasification combined cycle [IGCC], e.g. combined with carbon capture and storage [CCS]
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Abstract
The present invention is a kind of fluidized bed coal gasification method, it utilizes fine coal subregion fluidisation, with air and steam is fluidizing medium, equally distributed fluidized bed is divided into plural reduction and gaseous district, oxidation heat supply district and residue burning-out zone are realized the subregion gasification, the flammable composition in the enrichment coal gas, through tornado dust collector and Wen's fly-ash separator, obtain the coal gas of room temperature state after the cooling again.This method uses coal extensive, and under the condition of normal pressure, input air and steam can be satisfied the coal gas of industrial furnace heat supply requirement fully.Putting forward the high-carbon utilization ratio, boosting productivity is a kind of inexpensive coal gas and operating maintenance coal gas production method easily of producing.
Description
The present invention is a kind of fluidization gasification process of fine coal.
Rich coal resources in China, great variety of goods, so power supply is based on coal, to use after the gasification of coal, comparable direct burning improves efficiency of combustion 10-20%, simultaneously, burning coal gas can reduce pollution, be convenient to operation, control, reclaim flue gas heat, save energy is easy to realize mechanize, the automatization of production process.Therefore, this method is the technological development direction of universally acknowledged coal utilization.
In the various gasification of coal, have lot of advantages with the fluidization gasification process, about 80% the broken coal that it can use that the modern age mechanical coal mining produces also can use the higher fine coal of ash.In the production process, there is not the pollution of tar, benzene, phenol.This method gasification intensity is big, adaptability is strong, Load Regulation is good, publishes according to China Construction Industry Press, and " the gasification outline " of Lu Yongchang work introduced the Winkler evaporating method, adopt air and water vapor to make gasifying medium, can obtain calorific value is 4200-4500KJ/m
3Coal gas, if when adopting oxygen and water vapor, the coal gas calorific value can reach 10000-11000KJ/m
3Gasifying medium makes the fine coal in the vapourizing furnace be the boiling fluidized state by grid distributor.The shortcoming of Winkler evaporating method mainly is that the calorific value of coal gas is low, and the furnace gas export temperature is higher, the flammable object height of taking out of in the coal gas, and carbon content is higher in the lime-ash, and the utilization ratio of carbon is low.The Cogas evaporating method is to be constituted by gasification installation and combustion unit, is the combined process of PC-FB thermolysis and semi-coke powder fluidized-bed gasification, and whole process is made up of four major portions such as the hydrotreatment of the pre-treatment of coal, thermolysis, oil and gasifications.In burner 870 ℃ of coke grains are increased to 940 ℃, Control for Kiln Temperature can obtain 1900 ℃ flue gas at 900 ℃ with air-breathing in the gasifier, and it is the thermal source of heating cycle coke powder and the lifting gas of recycle coke powder.Because burner slag tap under high temperature and high pressure, technical difficulty is bigger, does not reach industrialness at present as yet and uses.
The objective of the invention is shortcoming at the Winkler evaporating method, employing is with the whole fluidized-bed zone that is divided three classes, reduction and gaseous district, oxidation heat supply district and residue burning-out zone, adopt preheated air and superheated vapo(u)r to effectively utilize the waste heat of coal gas and flue gas, adopt secondary cyclone dust removal and input burning-out zone to put forward the calorific value of high-carbon utilization ratio and coal gas.
The structure of fine coal fluidization gasification installation of the present invention is shown in accompanying drawing, the oxidation heat supply district (1) of fluidized-bed, reduction and gaseous district (2) and carbon residue burning-out zone (3).Import preheated air (4) below the grid distributor respectively, superheated vapour (5) and normal temperature air (6).Reduction and gaseous district's top collection chamber (7) is collected the coal gas that produces.Heating gas is through vapor superheater (8), two sections tornado dust collector (9), Wen's fly-ash separator (10) and water tank (11), can be with the coal gas cooled dehydrated to room temperature, and hot flue gas enters gravitational dust collection chamber (12), air preheater (13) and waste heat boiler (14) drain into atmosphere after reclaiming its heat.Fine coal at first enters reduction and gaseous district through coal bunker (15) and material feeder (16), travels to and fro between oxidation heat supply district and reduction and gaseous district then, enters the residue burning-out zone at last, fully reduces carbon amount in the residue, drains into outside the stove continuously through slag off apparatus (17).
Fine coal fluidization evaporating method of the present invention, in fluidization equipment, fine coal is imported reduction and gaseous district through material feeder, and the district enters the carbon residue burning-out zone through the oxidation heat supply, and preheated air is fed oxidation heat supply district, the pulverized coal friring heat release provides heat to reduction and gaseous district, superheated vapour feeds reduction and gaseous district and produces coal gas of high temperature, is collected by collector, through superheater, behind second cyclone dust extractor, Wen's fly-ash separator, the watercooler, coal gas is reduced to room temperature.Preheated air and normal temperature air enter oxidation heat supply district and the carbon residue burning-out zone produces high-temperature flue gas, after gravitational dust collection chamber, air preheater enter the waste heat boiler recovery waste heat, enters atmosphere, and residue is through the slag off apparatus venting.
Gasification reaction in the reduction and gaseous district
Major ingredient in the coal gas is CO, H
2, CH
4; Not flammable composition is CO
2, H
2O and minor N
2, the coal gas process of cooling is removed H
2O and CO
2
In the oxidation heat supply district, carry out the combustion reactions of low oxygen content:
Major ingredient is not flammable composition CO in the flue gas
2, N
2And a spot of flammable composition CO, because blending effect in the fluidized-bed, a spot of CO, H in the reduction and gaseous district
2, CH
4Flammable composition when the carbon residue burning-out zone, all transfers CO to the effect of excess oxygen
2And H
2O.
In the carbon residue burning-out zone, carry out the oxygen-excess combustion reaction
The flue gas of discharging all is not flammable composition CO
2, H
2O, N
2
The present invention selects pulverized coal particle size＜8mm for use, and fine coal at first enters the volatile matter that reduction and gaseous district removes coal, has increased the calorific value of coal gas.Make full use of fluidized state and transmit heat, travel to and fro between oxidation heat supply district and reduction and gaseous district, enter the carbon residue burning-out zone at last, the fine coal carbon content reaches more than 25%, after fully burning, carbon is reduced to below 2%, and its residue lime-ash is discharged continuously by slag-drip opening.Air preheating temperature is greater than 300 ℃, and the steam superheating temperature is imported oxidation heat supply district and reduction and gaseous district respectively greater than 300 ℃, and the air of preheating is imported the carbon residue burning-out zone, and its empty bed speed is answered 〉=1.2 times critical fluidization velocity.
According to the kind of coal, temperature is controlled at 800 °-1100 ℃ in the fluidized-bed, and the fluidized layer height of fine coal and the ratio of bed width be less than 0.5, and the grid distributor percentage of open area is less than 5%, and has the straight hole grid distributor at the pitch angle of 15 degree.The ratio of reduction and gaseous district, oxidation heat supply district and carbon residue burning-out zone changes with the kind of coal.Add annexation or catalyzer in the fine coal, but attemperation adds Wingdale in the fine coal, can adopt the higher fine coal of sulfur-bearing.
Fluidized bed coal gasification method of the present invention, when adopting the hard coal thermal value to be 25000KJ/kg, the ratio of reduction and gaseous district, oxidation heat supply district and carbon residue burning-out zone is 4: 4: 2～5: 3: 2, coal amount 500～1000kg/m
3, granularity is 1～8mm, the grid distributor percentage of open area is less than 5%, blank pipe speed 〉=1.2 times critical fluidization velocity.Carbon content 〉=25% in reduction and gaseous district and oxidation heat supply district slag, carbon content should be less than 2% in the slag of carbon residue burning-out zone, air and steam superheating temperature＞300 ℃, Control for Kiln Temperature is at 800～1100 ℃, the ratio of bed depth and bedside is less than 0.5, and in the reduction and gaseous district of fine coal input earlier, the flying dust that reclaims through second cyclone dust extractor enters oxidation heat supply district, at this moment gasification efficiency is greater than 65%, and the utilization ratio of carbon is greater than 90%.
The present invention can use hard coal, bituminous coal, even low grade coal.Under non-pressurized condition, input air also can be produced calorific value 6500～8500KJ/m
3Coal gas, coal gas does not contain compositions such as tar, benzene, phenol, vaporization rate is greater than 65%, the utilization ratio of carbon is greater than 90%.The vapourizing furnace inner structure is simple, and easy handling is easy to maintenance, and the load change scope is big, and adaptability is by force a kind of coal gas production method that is suitable for the used for industrial furnace combustion gas.
Claims (6)
1, a kind of fluidized bed coal gasification method, in fluidizer, adopt air, water vapor by grid distributor fluidisation fine coal, gas making, it is characterized in that fluidizer is divided into oxidation heat supply district, reduction and gaseous district and carbon residue burning-out zone, fine coal is imported reduction and gaseous district through coal feeder, enters the carbon residue burning-out zone through oxidation heat supply district again.Preheated air input oxidation heat supply district, provide heat with pulverized coal friring to reduction and gaseous district, superheated vapour produces coal gas of high temperature by the reaction of reduction and gaseous district, after being collected by collector, behind superheater, second cyclone dust extractor, venturi scrubber, watercooler, coal gas is reduced to room temperature.The high-temperature flue gas that oxidation heat supply district and carbon residue burning-out zone produce after gravitational dust collection chamber, air preheater input waste heat boiler reclaim heat, enters atmosphere, and residue is discharged by slag-drip opening.
2, gasification process according to claim 1 is characterized in that pulverized coal particle size＜8mm, and fine coal at first enters reduction and gaseous district, remove the volatile matter of coal, increase the calorific value of coal, utilize fluidized state to transmit heat, fine coal is after secondary cyclone dust removal, send into oxidation heat supply district, enter the carbon residue burning-out zone at last, at this moment, fine coal residue carbon content is more than 25%, through fully burning, carbon is reduced to below 2%, its lime-ash is discharged continuously by slag-drip opening again.
3, gasification process according to claim 1, it is characterized in that air preheating temperature greater than 300 ℃, steam superheat is imported oxidation heat supply district and reduction and gaseous district greater than 300 ℃ respectively with it, normal temperature air input carbon residue burning-out zone, its empty bed speed is answered 〉=1.2 times critical fluidization velocity.
4, gasification process according to claim 1 is characterized in that an interior temperature, is controlled at 800～1100 ℃ according to the kind of coal.Adopt fine coal interior interpolation annexation or catalyzer to come attemperation, when adding Wingdale in the fine coal, can select the higher fine coal of carbon containing for use.
5, according to the described gasification process of claim 1, it is characterized in that ratio＜0.5 of fine coal fluidized layer height and bed width, grid distributor percentage of open area＜5%, and have the straight hole grid distributor at the pitch angle of 15 degree.
6, according to the described gasification process of claim 1, it is characterized in that fluidized-bed comprises two above oxidation heat supply districts, reduction and gaseous district and carbon residue burning-out zones, can select trizonal ratio difference according to the kind of used coal, when anthracitic calorific value was 25000KJ/kg, trizonal ratio was 4: 4: 2～5: 3: 2.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 87105200 CN1017254B (en) | 1987-07-31 | 1987-07-31 | Gasification method of fluidizing power coal |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 87105200 CN1017254B (en) | 1987-07-31 | 1987-07-31 | Gasification method of fluidizing power coal |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1031103A true CN1031103A (en) | 1989-02-15 |
| CN1017254B CN1017254B (en) | 1992-07-01 |
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ID=4815234
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 87105200 Expired CN1017254B (en) | 1987-07-31 | 1987-07-31 | Gasification method of fluidizing power coal |
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| CN (1) | CN1017254B (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1323142C (en) * | 2005-08-24 | 2007-06-27 | 太原理工大学 | Fuild bed composite circle coal gasification method and apparatus |
| CN101838557A (en) * | 2010-02-10 | 2010-09-22 | 马鞍山科达洁能有限公司 | Coal gas producer and coal gas production method |
| CN108774549A (en) * | 2018-08-29 | 2018-11-09 | 中国石油化工股份有限公司 | Air flow bed fine coal hydrogasification stove, hydrogasification system and hydro-gasification process |
-
1987
- 1987-07-31 CN CN 87105200 patent/CN1017254B/en not_active Expired
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1323142C (en) * | 2005-08-24 | 2007-06-27 | 太原理工大学 | Fuild bed composite circle coal gasification method and apparatus |
| CN101838557A (en) * | 2010-02-10 | 2010-09-22 | 马鞍山科达洁能有限公司 | Coal gas producer and coal gas production method |
| CN101838557B (en) * | 2010-02-10 | 2011-09-21 | 马鞍山科达洁能股份有限公司 | Coal gas producer and coal gas production method |
| CN108774549A (en) * | 2018-08-29 | 2018-11-09 | 中国石油化工股份有限公司 | Air flow bed fine coal hydrogasification stove, hydrogasification system and hydro-gasification process |
| CN108774549B (en) * | 2018-08-29 | 2023-10-24 | 中国石油化工股份有限公司 | Entrained-flow pulverized coal hydro-gasification furnace, hydro-gasification system and hydro-gasification method |
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| Publication number | Publication date |
|---|---|
| CN1017254B (en) | 1992-07-01 |
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