CN2055503U - Single-stage fluidized bed powder coal gasified furnace - Google Patents
Single-stage fluidized bed powder coal gasified furnace Download PDFInfo
- Publication number
- CN2055503U CN2055503U CN89213610U CN89213610U CN2055503U CN 2055503 U CN2055503 U CN 2055503U CN 89213610 U CN89213610 U CN 89213610U CN 89213610 U CN89213610 U CN 89213610U CN 2055503 U CN2055503 U CN 2055503U
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- Prior art keywords
- furnace
- powder coal
- fluidized bed
- bed powder
- stage
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- 239000003245 coal Substances 0.000 title claims abstract description 41
- 239000000843 powder Substances 0.000 title claims description 17
- 238000002309 gasification Methods 0.000 claims abstract description 25
- 238000009826 distribution Methods 0.000 claims description 7
- 239000012530 fluid Substances 0.000 claims description 6
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 6
- 239000010881 fly ash Substances 0.000 claims description 4
- 239000000428 dust Substances 0.000 abstract description 3
- 239000003034 coal gas Substances 0.000 description 10
- 238000005516 engineering process Methods 0.000 description 7
- 238000000034 method Methods 0.000 description 4
- 238000000197 pyrolysis Methods 0.000 description 4
- 238000005243 fluidization Methods 0.000 description 3
- 229910052799 carbon Inorganic materials 0.000 description 2
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- 239000002956 ash Substances 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 238000005336 cracking Methods 0.000 description 1
- 238000000354 decomposition reaction Methods 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 238000009434 installation Methods 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 238000005065 mining Methods 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 235000020030 perry Nutrition 0.000 description 1
- 238000012552 review Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 238000012360 testing method Methods 0.000 description 1
- 238000013519 translation Methods 0.000 description 1
Classifications
-
- 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
- Solid-Fuel Combustion (AREA)
- Crucibles And Fluidized-Bed Furnaces (AREA)
Abstract
The utility model relates to a new single-stage fluidized bed powdery coal gasified furnace. As the utility model is provided with a furnace body, a grid plate, a dust remover, a two-stage self air preheater and a steam generator, and as the position of a coal auger is reasonably improved, the gas caloricity is improved. The powdery coal gasified furnace of the utility model has simple structure, reasonable structure and stable operation, having no tar. When gas produced by the utility model is used, the CH-[4] content, the gas caloricity and the gasification efficiency are respectively higher than a conventional Winkler furnace inland and abroad. The utility model can replace producer gas.
Description
Technical field is gasification process and gasification installation under the utility model.
The scheme of low calorific value coal gasification is a lot, the at present domestic fixed-bed gasification furnaces of using more, and this stove only is suitable for lump coal, and along with the development of China's mechanical coal mining technology, the coal of China 70～80% all belongs to fine coal, and lump coal is seldom.Therefore, a large amount of fine coal can not get using, and brings very big difficulty to production, thereby the fixed bed gasification technology of China's widespread use at present is subjected to very big restriction.
Close technology external now and the invention has Winkler stove and U-gas stove.These two kinds of vapourizing furnaces all make the coal fluidisation with the air distribution plate method, and its fluidizing medium is air and steam.These two kinds of vapourizing furnaces, simple in structure, easy to operate, advantages such as no tar.But it is too low that the main drawback of Winkler stove is a caloric power of gas, has only 4168～4605Kj/Nm
3(1000～1100kcal/Nm
3), the utilization ratio of carbon is low, so do not paid attention to by the people.The calorific value of U-gas stove and gasification efficiency are all higher, but because the reunion technology more complicated of its ash is difficult for grasp, it and coal relation is very big, therefore and China is a country that ature of coal is changeable, and this technology is not only grasped difficulty, and generally applies also in China and to have any problem.
The quoted passage of close technology has:
1.Perry?Nonacki，Energy?Technology?Review?NO.70：Coal?gasification?processes。
2. Wang Yang compiling: the exploitation of s-generation fluidized bed coal gasifier " coal comprehensive utilization collected translation ", 1989, No.1.
The purpose that the present utility model is created is in order to overcome the shortcoming of above-mentioned vapourizing furnace, and a kind of operation operation of innovation and creation is simple, convenient, and on calorific value the novel fluidized bed powder coal gasification furnace (see shown in Figure 1) suitable with fixed-bed gasification furnace.
Fundamental point of the present utility model is, a kind of novel fluidized bed powder coal gasification furnace (1), the position of its coal supply auger (2) is provided with height from air distribution plate (3) and is generally between 0.6～1/2H and changes, wherein H is the height of vapourizing furnace (1), in this altitude range, higher caloric power of gas will be obtained.Simultaneously in fluid bed powder coal gasification stove back-end ductwork (4), be provided with first step air and give hot gas (5), be provided with at body of heater (1) cylindrical tube top that water vapour producer (6) and second stage air give hot device (7) so that improve calorific value.In body of heater (1) cylinder bottom one reverse taper (8) is set, to solve the contradiction between fluidization quality and the carry-over loss.
Detailed structure of the present utility model is described below:
Sigle-stage AC fluid bed powder coal gasification stove, its structural representation such as Fig. 1, it has a columnar body of heater (1), in body of heater (1) bottom an air distribution plate (3) is arranged, the position of its coal supply auger (2) is provided with the height that air distribution plate (3) locates and is generally 0.6～1/2H, and wherein H is the height of vapourizing furnace (1).To obtain higher caloric power of gas in this altitude range, the difference along with height will obtain different CH
4With the content of CmHn, promptly obtain different calorific values.In fluid bed powder coal gasification stove back-end ductwork (4) lining, first step air is set gives hot device (5) (see figure 1), utilize gas exhaust duct to give heat.Water vapour producer (6) is set at body of heater (1) top utilizes the self-produced superheated vapo(u)r of method of furnace roof chuck and second stage air to give hot device (7), with the temperature of raising air, thus the calorific value of raising coal gas.The body of heater bottom is a reverse taper, thereby solves the contradiction between fluidization quality and the carry-over loss.
The present utility model is created: rationally improve coal supply auger position (2), many investigators of past are arranged on coal supply auger position near the bed surface place, here be the intensive oxidation zone, therefore a large amount of destructive distillation products is burnt or is transformed fast or cracking, methane gas seldom remains, and influences the calorific value of coal gas.The distance that auger position (2) are arranged on from air distribution plate (3) is the place of 0.6～1/2H now, because it is highly higher, promptly be in the reduction zone, so pyrolysis (destructive distillation) reaction takes place in fine coal immediately that flow into the vapourizing furnace from coal supply auger position (2), the destructive distillation gas that is produced enters coal gas with major part, produce mixed gas, CH in the coal gas like this
4And the content of CmHn is than conventional Winkler stove height (seeing Table 1).Simultaneously because we adopt two-stage self air to give thermic devices, air gives hot device (5) by the first step and utilizes gas exhaust duct to give to enter second stage air after the heat and give hot device (7), promptly utilizes the furnace roof chuck further to give heat again.Thereby the deflated sensible heat is converted into the potential chemical heat of coal gas.Equally water is flowed in the furnace roof chuck, promptly in the water vapour producer (6), just produce superheated vapo(u)r.This high temperature air and superheated vapo(u)r are mixed in the body of heater (1) from air compartment (9) end opening, because air, vapour temperature is higher, thereby the minimizing of the consumption of air, and the rate of decomposition of water vapour has also improved simultaneously, and this calorific value that all helps coal gas improves.The coal gas that generates enters fly-ash separator (10) through flue (4), and coal gas is seen off from fly-ash separator (10) top duct (11).And flying dust is sent in the body of heater (1) from fly-ash separator (10) bottom pipe (12) again, carries out flying dust recirculation, puies forward the high-carbon utilization ratio.
The single-stage fluidized bed powder coal gasification furnace of the invention, simple in structure, rationally stable, no tar, and improved the calorific value of coal gas, the data in its table 1 are interim test results of the present utility model.By table 1
As can be seen, the coal gas that adopts single-stage fluidized bed powder coal gasification furnace of the present utility model to produce, its CH content, caloric power of gas and gasification efficiency all are higher than the Winkler stove of home and abroad routine, can produce 4605～6279kj/Nm
3(1100～1500kcal/Nm
3) low-heat value gas.To have broad application prospects industrial.
Claims (4)
1, a kind of sigle-stage AC fluid bed powder coal gasification stove, it is by body of heater (1), coal supply auger (2), air distribution plate (3), flue (4), air compartment (9), fly-ash separator (10) is formed, and it is characterized in that the position of said single-stage fluidized bed powder coal gasification furnace coal supply auger (2), the height from air distribution plate (3), be generally 0.6～1/2H, wherein H is the height of vapourizing furnace (1);
2, according to the said single-stage fluidized bed powder coal gasification furnace of claim 1, it is that two-stage self air gives heat that the air that it is characterized in that said vapourizing furnace gives hot device, first step air gives hot device (5) and is arranged in the fluid bed powder coal gasification stove flue (4), second stage air gives hot device (7), for the furnace roof jacketed type gives heat.
3, according to claim 1,2 said single-stage fluidized bed powder coal gasification furnaces, it is chuck shape that the water vapour producer (6) that it is characterized in that said fluid bed powder coal gasification stove is arranged on furnace roof.
4, according to the said single-stage fluidized bed powder coal gasification furnace of claim 1, the bottom that it is characterized in that said powder coal gasification furnace is a back taper.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN89213610U CN2055503U (en) | 1989-07-08 | 1989-07-08 | Single-stage fluidized bed powder coal gasified furnace |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN89213610U CN2055503U (en) | 1989-07-08 | 1989-07-08 | Single-stage fluidized bed powder coal gasified furnace |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN2055503U true CN2055503U (en) | 1990-04-04 |
Family
ID=4869549
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN89213610U Withdrawn CN2055503U (en) | 1989-07-08 | 1989-07-08 | Single-stage fluidized bed powder coal gasified furnace |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN2055503U (en) |
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2008138167A1 (en) * | 2007-05-14 | 2008-11-20 | Foshan Keda Energy Resource Machinery Co., Ltd. | A method for producing coal gas |
| WO2008138166A1 (en) * | 2007-05-14 | 2008-11-20 | Foshan Keda Energy Resource Machinery Co., Ltd. | A coal circulating fluidized bed coal gas generating furnace system |
| CN101063053B (en) * | 2007-05-14 | 2010-05-26 | 广东科达机电股份有限公司 | Circulating fluidized bed gas generator system |
| CN102329651A (en) * | 2011-08-26 | 2012-01-25 | 北京大学深圳研究生院 | Three-stage gasification device for producing synthesis gas through biomass pyrolysis and gasification |
| CN102821840A (en) * | 2010-04-23 | 2012-12-12 | 蒂森克虏伯伍德公司 | Device and method for thermally pre-treating solid raw materials in concentrically stepped fluidized bed |
| CN104479742A (en) * | 2014-12-04 | 2015-04-01 | 广州环渝能源科技有限公司 | Biomass fuel preparation system |
| CN106323822A (en) * | 2016-08-11 | 2017-01-11 | 哈尔滨工业大学 | Experimental device and method used for research on particle flow characteristic in bubbling fluidized bed |
-
1989
- 1989-07-08 CN CN89213610U patent/CN2055503U/en not_active Withdrawn
Cited By (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2008138167A1 (en) * | 2007-05-14 | 2008-11-20 | Foshan Keda Energy Resource Machinery Co., Ltd. | A method for producing coal gas |
| WO2008138166A1 (en) * | 2007-05-14 | 2008-11-20 | Foshan Keda Energy Resource Machinery Co., Ltd. | A coal circulating fluidized bed coal gas generating furnace system |
| CN101063053B (en) * | 2007-05-14 | 2010-05-26 | 广东科达机电股份有限公司 | Circulating fluidized bed gas generator system |
| US8029581B2 (en) | 2007-05-14 | 2011-10-04 | Keda Industrial Co., Ltd. | Method for producing coal gas |
| CN102821840A (en) * | 2010-04-23 | 2012-12-12 | 蒂森克虏伯伍德公司 | Device and method for thermally pre-treating solid raw materials in concentrically stepped fluidized bed |
| CN102329651A (en) * | 2011-08-26 | 2012-01-25 | 北京大学深圳研究生院 | Three-stage gasification device for producing synthesis gas through biomass pyrolysis and gasification |
| CN102329651B (en) * | 2011-08-26 | 2014-03-26 | 北京大学深圳研究生院 | Three-stage gasification device for producing synthesis gas through biomass pyrolysis and gasification |
| CN104479742A (en) * | 2014-12-04 | 2015-04-01 | 广州环渝能源科技有限公司 | Biomass fuel preparation system |
| CN104479742B (en) * | 2014-12-04 | 2021-04-02 | 广州环渝能源科技有限公司 | Biomass gas preparation system |
| CN106323822A (en) * | 2016-08-11 | 2017-01-11 | 哈尔滨工业大学 | Experimental device and method used for research on particle flow characteristic in bubbling fluidized bed |
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|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| C19 | Lapse of patent right due to non-payment of the annual fee | ||
| CF01 | Termination of patent right due to non-payment of annual fee |