CN100577774C - Differential bed catalytic coal gasifaction stove and catalysis gasification method - Google Patents
Differential bed catalytic coal gasifaction stove and catalysis gasification method Download PDFInfo
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- CN100577774C CN100577774C CN200610088402A CN200610088402A CN100577774C CN 100577774 C CN100577774 C CN 100577774C CN 200610088402 A CN200610088402 A CN 200610088402A CN 200610088402 A CN200610088402 A CN 200610088402A CN 100577774 C CN100577774 C CN 100577774C
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- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
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Abstract
Differential bed catalytic coal gasifaction stove and catalysis gasification method are a kind of extensive China's reserves abundant high ash, high-sulfur, high ash melting point gasification of coal and vapourizing furnaces handled that be fit to, burner hearth (12) is arranged in the pressure vessel (6), burner hearth is divided into lower hearth (1) and upper furnace (2) from bottom to top, lower hearth (1) is a chamber with a wide bed diameter, adopts low flow velocity and low temperature mode to move; Be respectively equipped with the import of air, coal dust, Wingdale, water vapour, catalyzer in lower hearth (1) bottom and side; Shrink the upper furnace (2) that forms by lower hearth (1) top, upper furnace (2) adopts high flow rate and high temperature mode to move; The internal diameter of upper furnace (2) is less than lower hearth (1), and the height of upper furnace (2) is greater than lower hearth (1); The outlet of upper furnace (2) connects cyclonic separator (3), and cyclonic separator (3) bottom is connected to downtake (4), and the bottom of downtake (4) is connected with horizontally disposed " L " valve (5), the lower side of another termination lower hearth (1) of " L " valve (5).
Description
Technical field
The present invention relates to a kind of catalytic coal gasifaction method and apparatus, especially a kind of employing differential bed carries out the catalytic coal gasifaction method and apparatus, belongs to the technical field of gasification.
Background technology
Clean efficient utilization of coal is current China great technical task in energy and environment field, is one of key factor that is related to the Chinese national economy Sustainable development.Coal Gasification Technology is the core of modern many clear energy sources technology, as coal-based Poly-generation, integrated gasification combined cycle for power generation (IGCC), gelatin liquefaction etc.In at present numerous vapourizing furnaces, mainly contain two types of air flow bed and fluidized-bed gasification furnaces.
Texaco's (Texaco) vapourizing furnace and Xie Er (Shell) vapourizing furnace are two kinds of main entrained flow gasification type of furnaces, they all adopt purity is that oxygen and the water vapor of 85-99% is vaporized chemical, the former is a coal water slurry feed mode, the latter is a dry powder feed mode, and its main advantage is that efficiency of carbon conversion height, amplifying power are strong.But shortcoming also is tangible: as the requirement strictness (ash content, ash fusion point and sludge forming performance etc.) of Texaco vapourizing furnace to ature of coal, have only minority coals such as Shenhua, Datong District, Huating and Yima to select for use, and the available rate of vapourizing furnace has only 80%-85%; The main drawback of Shell vapourizing furnace is: the drying of dry powder, preparation system complexity need be 99.9% N with purity
2Gas is carried, and the operating pressure of vapourizing furnace generally should not surpass 4～4.5MPa; Furnace binding and Controlling System are complicated, the investment cost height.Compare with entrained flow gasification, fluidized-bed gasification has can directly utilize the flour coal, little to the susceptibility of the ash content of coal, is suitable for the utilization of high grey low grade coal, can add sulphur-fixing agent in bed, realizes direct desulfurization in the stove, and coal tar content is low in the coal gas.But fluidized-bed gasification furnace has very high gasification temperature like that not as airflow bed gasification furnace, can guarantee that gasification reaction carries out fast, thereby on coal, require to use the coal of greater activity and than the coal of high ash melting point, simultaneously because the semicoke gasification reaction carries out thoroughly inadequately, discharge lime-ash and the unburned carbon in flue dust height of taking out of with coal gas with regard to having brought, lose big problem, in addition, the amplifying power of fluidized-bed gasification furnace is relatively poor, commercial in the world operation maximum-norm fluidized-bed gasification furnace day is handled the coal amount about 1000t, far below the level of air flow bed 2000t/d at present.
Summary of the invention
Technical problem: in view of the defective of above two kinds of type of furnaces, the present invention proposes the differential bed catalytic coal gasifaction stove and the catalysis gasification method of synthetic gas stream bed and fluidization characteristics, purpose is to provide a kind of extensive China's reserves abundant high ash, high-sulfur, high ash melting point gasification of coal and vapourizing furnace handled that be fit to.
Technical scheme: differential bed gasification furnace system mainly is made up of turbulent bed, upcast, downtake and L valve etc.Burner hearth is arranged in the pressure vessel, and burner hearth is divided into lower hearth and upper furnace from bottom to top, and lower hearth is a chamber with a wide bed diameter, adopts low flow velocity and low temperature mode to move; Be respectively equipped with the import of coal dust, water vapour, catalyzer, air or oxygen in lower hearth bottom and side; Shrink the upper furnace that forms by lower hearth top, upper furnace adopts high flow rate and high temperature mode to move; The internal diameter of upper furnace is less than lower hearth, and the height of upper furnace is greater than lower hearth; The outlet of upper furnace connects cyclonic separator, and the cyclonic separator bottom is connected to downtake, and the bottom of downtake is connected with horizontally disposed " L " valve, the lower side of another termination lower hearth of " L " valve.The outer wall of cyclonic separator, downtake, " L " valve adopts the structure formation of water wall.In described low flow velocity and the low temperature mode, low flow velocity is the 3-4 meter per second, and low temperature is 850-950 ℃; In high flow rate and the high temperature mode, high flow rate is the 8-10 meter per second, and high temperature is 1100-1200 ℃.
The differential catalysis gasification method of differential bed catalytic coal gasifaction stove is: adopt the method that changes the bed diameter that the gas flow rate of different zones in the bed is changed in burner hearth, it is differential, thereby change gas-solid flow state and reaction conditions, reach by the component of different activities in the coal and carry out the classification conversion, concrete mode is: with coal, the air or oxygen of vaporized chemical and steam, Wingdale and catalyzer join in the lower hearth, coal provides the gasification reaction heat with air or oxygen generation combustion reactions in bed, the active low semicoke of highly active component generation water-gas reaction formation reaction in steam and the coal then, lower hearth is in gentle gasification reaction state promptly: the turbulent bed operation scheme, flow velocity 3-4m/s, temperature 850-950 ℃; The semicoke of low reaction activity and catalyzer are carried by air-flow and enter upper furnace, this district has higher temperature of reaction and good gas-solid efficient, help the gasification of low activity semicoke, semicoke and catalyzer carry out degree of depth gasification in this zone, the upper furnace working conditions is air conveying operation scheme, flow velocity 8-10m/s, temperature 1100-1200 ℃; Add catalyzer at lower hearth, these catalyzer can be basic metal, alkaline earth salt or Ni-based compound, and these catalyzer form complex compound with coal in burner hearth, reduce reaction activity, have improved gasification reaction speed and efficiency of carbon conversion.Coal, vaporized chemical (oxygen/air and water vapor), Wingdale join in the turbulent bed, carry out the gasification of coal devolatilization and part of coke under lower temperature and low flow velocity, and this part is the higher part of reactive behavior in the coal, requires relatively low to reaction conditions; Semicoke behind the partial gasification is the active minimum and part of difficult gasification in the coal, this partial gasification share will determine efficiency of carbon conversion and the gasification efficiency that vapourizing furnace is final, tradition fluidized-bed gasification furnace efficiency of carbon conversion major cause on the low side is because lower reaction in furnace temperature and gasification speed of reaction cause active low semicoke fully not gasify.Based on this, add partial oxygen/air and catalyzer on the top of turbulent bed, improve temperature of reaction, flow velocity also is increased to 8-10m/s.Semicoke and water vapor carry out catalytic coal gasification in pipe, the raising of temperature and the dual function of catalyzer will have been accelerated the gasification reaction process of semicoke, have improved an efficiency of carbon conversion of coal.Circulate through downtake and L valve loopback turbulent bed by the isolating particle of separator (containing unreacted carbon and catalyzer etc.), when improving efficiency of carbon conversion, also make catalyzer be able to recycle.
Beneficial effect: compared with prior art, the present invention has following characteristics:
Change the reaction conditions of turbulent bed and upcast, the component of different activities in the coal is carried out classification transform; Have very strong coal adaptability, be specially adapted to high ash melting point, high ash content, high sulfur content coal; The main reaction region temperature is higher, between air flow bed and fluidized-bed, has avoided the shortcoming of air flow bed to coal adaptability difference and fluidized-bed low reaction speed; Adopting particle diameter is the coal grain of 0.5-1.0mm, also reduces because of grinding the cost that coal dust increases when improving gasification reaction speed; Adopt the turbulent bed in wide cross section, prolonged the residence time of particle, help the raising of efficiency of carbon conversion and pollutant removing efficient in the vapourizing furnace class; Adopt the upcast of high gas speed, reduce the probability of particle collision, avoid the appearance of high-temperature coke; Adopt appropriate catalyst, can improve the speed of reaction and the efficiency of carbon conversion of gasification, can control the generation of pollutent and the distribution in product thereof again.
Description of drawings
Fig. 1 is a differential bed coal-gasification furnace structure synoptic diagram of the present invention.
Fig. 2 implements the coal gasifying process schema for adopting device of the present invention.
Have among the above figure: lower hearth 1, upper furnace 2, cyclonic separator 3, downtake 4, " L " valve 5, pressure vessel 6, gas cooler 7, fly-ash separator 8, compressor 9, preheater 10, vapor superheater 11, burner hearth 12, coal dust A, water vapor B, catalyzer C, air or oxygen D, slag E, water F.
Embodiment
Referring to accompanying drawing 1, this vapourizing furnace burner hearth is divided into 2 two sections of lower hearth 1 and upper furnaces.Lower hearth 1 is a chamber with a wide bed diameter, gas is at this flow velocity lower (3-4m/s), the gas-solid way of contact is a turbulent bed, under this operation scheme, the gas-solid contact is good and do not have air pocket to generate, around the bed and the bottom arrange coal, Wingdale, catalyzer and vaporized chemical (air/oxygen and steam) inlet and slag-drip opening, operating temperature lower (850-950 ℃) in the bed helps the carrying out that coal partial gasification and limestone desulfurization react.Top at lower hearth 1, to inwardly shrink around the bed and form the less reaction tubes formation upper furnace 2 of an area, after area shrinks, gas flow rate increases, below upper furnace 2, bubbling air or oxygen, burn part coal gas temperature of reaction is risen to 1100-1200 ℃, be intended to improve gasification reaction speed, upper furnace 2 gas flow rates are controlled at 8-10m/s, and under this flow velocity, the gas-solid flow flowing mode is air conveying, the probability that collides between particle reduces, and has avoided the coking that particle causes because of collision under the high temperature.Catalyzer adds from lower hearth 1 top, and most of catalyzer will be brought into upper furnace 2 by air-flow, with vaporized chemical and semicoke effect, reduces active low semicoke gasification reaction activation energy, improves efficiency of carbon conversion.The inabundant semicoke that reacts of coal gas, catalyzer and part that comes out from upper furnace 2 will enter cyclonic separator 3, coal gas is separated with solid particulate (semicoke and catalyzer), catalyzer after the separation and semicoke are by downtake 4, " L " valve 5 is transmitted back to lower hearth 1, realize the circulating reaction of catalyzer and semicoke, cyclonic separator 3, downtake 4 and " L " valve 5 adopt water wall structure, and coal gas of high temperature and solid particulate are cooled off.Sequence number 1 is a lower hearth among Fig. 1, and 2 is upper furnace, and 3 is cyclonic separator, and 4 is downtake, and 5 is " L " valve.
Concrete structure is: burner hearth 12 is arranged in the pressure vessel 6, and burner hearth is divided into lower hearth 1 and upper furnace 2 from bottom to top, and lower hearth 1 is a chamber with a wide bed diameter, adopts low flow velocity and low temperature mode to move; Be respectively equipped with the import of coal dust A, water vapour B, catalyzer C, air or oxygen D in lower hearth 1 bottom and side; Shrink the upper furnace 2 that forms by lower hearth 1 top, upper furnace 2 adopts high flow rate and high temperature mode to move; The internal diameter of upper furnace 2 is less than lower hearth 1, and the height of upper furnace 2 is greater than lower hearth 1; The outlet of upper furnace 2 connects cyclonic separator 3, and cyclonic separator 3 bottoms are connected to downtake 4, and the bottom of downtake 4 is connected with horizontally disposed " L " valve 5, the lower side of another termination lower hearth 1 of " L " valve 5.The outer wall of cyclonic separator 3, downtake 4, " L " valve 5 adopts the structure formation of water wall.In low flow velocity and the low temperature mode, low flow velocity is the 3-4 meter per second, and low temperature is 850-950 ℃; In high flow rate and the high temperature mode, high flow rate is the 8-10 meter per second, and high temperature is 1100-1200 ℃.
The gasifying process flow process of implementing according to the present invention is as shown in Figure 2: coal, vaporized chemical (air/oxygen and steam), catalyzer directly join in the stove from the bottom and the side of lower hearth 1, coal adopts the following fine powder of 1mm, the catalyst particle size scope is also suitable with the coal grain, to improve the diffusional resistance of upper furnace 2 air conveying abilities and minimizing gasification reaction.10 compressions of the compressed machine 9 of air or oxygen and preheater and heating back make grain fluidized in the lower hearth 1 as fluidized gas, simultaneously and coal, catalyzer carry out catalytic gasification and react.Air temperature and current speed in the lower hearth 1 is controlled respectively between 850-950 ℃ and the 3-4m/s, therefore the gas velocity lower hearth 1 in is lower than fast bed and carries bed but be higher than the bubbling bed, when prolonging gas-solid duration of contact, avoided because the phenomenon that the gas-solid contact that the generation of air pocket produces worsens, reactor moves at a lower temperature simultaneously, and the desulfuration in furnace reaction of favourable Wingdale and the heavy metal contaminants in the coal are cured in the lime-ash discharges.Ingress at upper furnace 2 adds little air/oxygen, improve temperature of reaction, help the gasification of the semicoke that reactive behavior is minimum in the coal, air temperature and current speed in the upper furnace 2 is controlled respectively between 1100-1200 ℃ and the 8-10m/s, this temperature is in the middle of fluidized-bed gasification furnace (1000 ℃) and the airflow bed gasification furnace (1400 ℃), and gas velocity and air flow bed are suitable, under this reaction conditions, gas-solid is flowed and to be characterized as air conveyingly in the upper furnace 2, and this helps having strengthened mass transfer between gas-solid, heat transfer and reaction.Catalyzer (being generally basic metal, alkaline earth salt or Ni-based compound) adds from lower hearth 1 top, most of catalyzer will together be brought into upper furnace 2 by air-flow and unreacted semicoke, in this and vaporized chemical and semicoke effect, realize the catalytic gasification of semicoke, improve efficiency of carbon conversion.Burner hearth (comprising lower hearth 1 and upper furnace 2) is placed in the pressure vessel 6, to realize that coal gasifies under pressure, improves gasification intensity, helps the extensive processing of coal.The outlet of upper furnace 2 is connecting cyclonic separator 3, the effect of this separator is that most particle in the coal gas (comprising catalyzer and unburnt semicoke) is separated with coal gas, particle under separating enters the downtake 4 of cyclonic separator 3 bottoms, the downtake flow pattern is a moving-bed type, the particle translational speed is 0.5-1.0m/s, particle is sent in the bed circulating reaction again back to by level " L " valve 5 that links to each other with downtake bottom then, to improve the service efficiency and the efficiency of carbon conversion of catalyzer, " L " valve adopts superheated vapour as carrying wind.The shell of cyclonic separator 3, downtake 4, " L " valve 5 all adopts the water wall structure form, has both cooled off particle and has avoided high-temperature coking between particle, has produced steam again as vaporized chemical.Coal gas through just purifying enters gas cooler 7, and the steam of generation is sent into lower hearth 1 as vaporized chemical after vapor superheater 11 is overheated, and cooled coal gas enters fly-ash separator 8 and further purifies, and purification coal gas enters the gas burner combustion power generation at last.
Claims (3)
1. differential bed catalytic coal gasifaction stove, it is characterized in that: burner hearth (12) is arranged in the pressure vessel (6), and burner hearth is divided into lower hearth (1) and upper furnace (2) from bottom to top, and lower hearth (1) is a chamber with a wide bed diameter, adopts low flow velocity and low temperature mode to move; Be provided with the import of coal dust (A) in lower hearth (1) bottom, be respectively equipped with the import of water vapour (B), catalyzer (C), air or oxygen (D) in the side of lower hearth (1); Shrink the upper furnace (2) that forms by lower hearth (1) top, upper furnace (2) adopts high flow rate and high temperature mode to move; The internal diameter of upper furnace (2) is less than lower hearth (1), and the height of upper furnace (2) is greater than lower hearth (1); The outlet of upper furnace (2) connects cyclonic separator (3), and cyclonic separator (3) bottom is connected to downtake (4), and the bottom of downtake (4) is connected with horizontally disposed " L " valve (5), the lower side of another termination lower hearth (1) of " L " valve (5); In described low flow velocity and the low temperature mode, low flow velocity is the 3-4 meter per second, and low temperature is 850-950 ℃; In high flow rate and the high temperature mode, high flow rate is the 8-10 meter per second, and high temperature is 1100-1200 ℃.
2. differential bed catalytic coal gasifaction stove according to claim 1, the outer wall that it is characterized in that cyclonic separator (3), downtake (4), " L " valve (5) adopts the structure formation of water wall.
3. differential catalysis gasification method that utilizes the described differential bed of claim 1 catalytic coal gasifaction stove, it is characterized in that: in burner hearth (12), adopt the method that changes the bed diameter that the gas flow rate of different zones in the bed is changed, it is differential, thereby change gas-solid flow state and reaction conditions, reach by the component of different activities in the coal and carry out the classification conversion, concrete mode is: be the coal of 0.5-1.0mm with particle diameter, the air of vaporized chemical or the oxygen of vaporized chemical and steam, Wingdale and catalyzer join in the lower hearth (1), coal provides the gasification reaction heat with air or oxygen generation combustion reactions in bed, the active low semicoke of highly active component generation water-gas reaction formation reaction in steam and the coal then, lower hearth (1) is in gentle gasification reaction state promptly: the turbulent bed operation scheme, flow velocity 3-4m/s, temperature 850-950 ℃; The semicoke of low reaction activity and catalyzer are carried by air-flow and enter upper furnace (2), this district has higher temperature of reaction, help the gasification of low activity semicoke, semicoke and catalyzer carry out degree of depth gasification in this zone, upper furnace (2) working conditions is air conveying operation scheme, flow velocity 8-10m/s, temperature 1100-1200 ℃; Add catalyzer at lower hearth (1), these catalyzer are basic metal, alkaline earth salt or Ni-based compound, and these catalyzer form complex compound with coal in burner hearth (12), reduce reaction activity, have improved gasification reaction speed and efficiency of carbon conversion.
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| CN100577774C true CN100577774C (en) | 2010-01-06 |
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Families Citing this family (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CA2713656C (en) | 2007-12-28 | 2014-07-08 | Greatpoint Energy, Inc. | Steam generating slurry gasifier for the catalytic gasification of a carbonaceous feedstock |
| CN102076829B (en) * | 2008-06-27 | 2013-08-28 | 格雷特波因特能源公司 | Four-train catalytic gasification systems |
| CN105441135A (en) * | 2014-06-25 | 2016-03-30 | 通用电气公司 | Coal gasification method |
| CN105154141B (en) * | 2015-09-18 | 2018-01-12 | 北京华石联合能源科技发展有限公司 | A kind of coal gasification reaction device and reaction system and technique based on the device |
| CN107746726B (en) * | 2017-11-25 | 2020-01-10 | 太原理工大学 | Integrated CO2Process and device for preparing synthesis gas by capturing and gasifying coal |
| CN112824501B (en) * | 2019-11-21 | 2022-02-08 | 中国科学院工程热物理研究所 | Circulating fluidized bed partial gasification device and circulating fluidized bed partial gasification method |
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2006
- 2006-08-22 CN CN200610088402A patent/CN100577774C/en not_active Expired - Fee Related
Non-Patent Citations (2)
| Title |
|---|
| 差速循环流化床的数学模型研究. 钊丽，徐向东.清华大学学报（自然科学版），第38卷第4期. 1998 |
| 差速循环流化床的数学模型研究. 钊丽，徐向东.清华大学学报（自然科学版），第38卷第4期. 1998 * |
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