CN109797012B - High-temperature fluidized bed reaction device and method for gasifying carbon-containing material thereof - Google Patents
High-temperature fluidized bed reaction device and method for gasifying carbon-containing material thereof Download PDFInfo
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- CN109797012B CN109797012B CN201811557942.4A CN201811557942A CN109797012B CN 109797012 B CN109797012 B CN 109797012B CN 201811557942 A CN201811557942 A CN 201811557942A CN 109797012 B CN109797012 B CN 109797012B
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- 229910052799 carbon Inorganic materials 0.000 title claims abstract description 42
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 title claims abstract description 41
- 239000000463 material Substances 0.000 title claims abstract description 38
- 238000000034 method Methods 0.000 title claims abstract description 31
- 238000006243 chemical reaction Methods 0.000 title abstract description 23
- 238000002309 gasification Methods 0.000 claims abstract description 140
- 239000000843 powder Substances 0.000 claims abstract description 80
- 239000004576 sand Substances 0.000 claims abstract description 63
- 239000003575 carbonaceous material Substances 0.000 claims abstract description 39
- 239000000571 coke Substances 0.000 claims abstract description 35
- 239000002893 slag Substances 0.000 claims abstract description 25
- 238000002360 preparation method Methods 0.000 claims abstract description 3
- 239000003795 chemical substances by application Substances 0.000 claims description 49
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 44
- 229910052760 oxygen Inorganic materials 0.000 claims description 44
- 239000001301 oxygen Substances 0.000 claims description 44
- 239000003245 coal Substances 0.000 claims description 43
- 239000007789 gas Substances 0.000 claims description 31
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 29
- 238000011084 recovery Methods 0.000 claims description 13
- 239000002918 waste heat Substances 0.000 claims description 13
- 239000002283 diesel fuel Substances 0.000 claims description 12
- 239000002245 particle Substances 0.000 claims description 7
- 239000002994 raw material Substances 0.000 claims description 7
- 238000002485 combustion reaction Methods 0.000 claims description 6
- 238000000746 purification Methods 0.000 claims description 6
- 230000005855 radiation Effects 0.000 claims description 6
- 238000002386 leaching Methods 0.000 claims description 3
- 239000010453 quartz Substances 0.000 claims description 3
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N silicon dioxide Inorganic materials O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 claims description 3
- 239000002028 Biomass Substances 0.000 claims description 2
- 238000007599 discharging Methods 0.000 claims description 2
- 238000000926 separation method Methods 0.000 claims description 2
- 238000005422 blasting Methods 0.000 claims 1
- 238000009413 insulation Methods 0.000 claims 1
- 239000002910 solid waste Substances 0.000 claims 1
- 230000001131 transforming effect Effects 0.000 claims 1
- 239000003034 coal gas Substances 0.000 description 19
- 238000001035 drying Methods 0.000 description 7
- 239000002802 bituminous coal Substances 0.000 description 6
- 238000005516 engineering process Methods 0.000 description 6
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- 229920006395 saturated elastomer Polymers 0.000 description 4
- 238000005054 agglomeration Methods 0.000 description 3
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- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 description 2
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 description 2
- 229910052782 aluminium Inorganic materials 0.000 description 2
- RHZUVFJBSILHOK-UHFFFAOYSA-N anthracen-1-ylmethanolate Chemical compound C1=CC=C2C=C3C(C[O-])=CC=CC3=CC2=C1 RHZUVFJBSILHOK-UHFFFAOYSA-N 0.000 description 2
- 239000003830 anthracite Substances 0.000 description 2
- 239000011818 carbonaceous material particle Substances 0.000 description 2
- 238000013461 design Methods 0.000 description 2
- 230000003009 desulfurizing effect Effects 0.000 description 2
- 238000011161 development Methods 0.000 description 2
- 230000009970 fire resistant effect Effects 0.000 description 2
- 239000003077 lignite Substances 0.000 description 2
- 230000001105 regulatory effect Effects 0.000 description 2
- 239000007787 solid Substances 0.000 description 2
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- 239000004411 aluminium Substances 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 230000036760 body temperature Effects 0.000 description 1
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- 229910001882 dioxygen Inorganic materials 0.000 description 1
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- Fluidized-Bed Combustion And Resonant Combustion (AREA)
- Processing Of Solid Wastes (AREA)
Abstract
一种高温流化床反应装置及其含碳物料气化的方法包括高温移动床排灰单元，高温气化反应器单元，半焦细粉循环输送单元三个单元，含碳物料的气化方法是由含碳物料和砂粒的制备，供气，高温气化，排渣及细粉输送所组成。本发明具有气化反应速率快，碳转化率高，单炉处理量高的优点。
A high-temperature fluidized bed reaction device and a method for gasifying carbon-containing materials include three units: a high-temperature moving bed ash discharge unit, a high-temperature gasification reactor unit, a semi-coke fine powder circulating conveying unit, and a gasification method for carbon-containing materials. It is composed of carbonaceous material and sand preparation, gas supply, high temperature gasification, slag discharge and fine powder conveying. The invention has the advantages of fast gasification reaction rate, high carbon conversion rate and high processing capacity of a single furnace.
Description
Technical Field
The invention belongs to a high-temperature fluidized bed gasification furnace and a method for gasifying carbon-containing materials thereof.
Background
Fluidized bed gasification is an important gasification technology, and a Winkler furnace for gasifying carbon-containing material particles in a fluidized state starts a series of subsequent similar processes, including dilute phase fluidization. Such as TRIG fluidized bed gasification technology developed by Kellogg Brown & Root, USA, U-gas fluidized bed gasification technology developed by GTI, HRL fluidized bed gasification technology developed by Australia, BHEL fluidized bed gasification technology developed by Bharat Heavy electric Limited, India. Shanxi institute of coal chemistry of Chinese academy of sciences successfully developed "ash agglomeration fluidized bed gasification process and apparatus" (application number: 94106781.5), the coal type range is wide (from brown coal to anthracite), and is suitable for high ash, high sulfur, high ash fusion point coal gasification, this patent is implemented in Yunnan wenshan aluminum industry and prepared the fuel gas used for aluminium ore calcination, wherein the gasifier continuous operation duration reaches 128 days, has refreshed the operation record of domestic ash agglomeration fluidized bed gasifier, has marked the maturity and reliability that the gasification apparatus industrial application of ash agglomeration fluidized bed fine coal has obtained further promotion. Meanwhile, Shanxi institute of coal chemistry, Chinese academy of sciences, is developing a method and a device for coal gasification in a multi-stage staged conversion fluidized bed (application number: 201010291577.4), and has completed a 0.6-2.8MPa Shenmu semicoke pressurized multi-stage staged conversion fluidized bed test on a 3.0MPa multi-stage staged conversion fluidized bed coal gasification pilot plant.
In many of the developed fluidized bed gasification methods, the average operating temperature of the whole bed of the fluidized bed gasification furnace cannot be higher than the softening temperature of the carbonaceous material ash. Once the operating temperature of the whole bed is higher than the softening temperature of the ash of the carbonaceous material, the particles of the carbonaceous material are agglomerated and slag-bonded, so that the gasification furnace is fluidized and is forced to stop. The limit of the operation temperature leads the gasification rate of the carbonaceous material particles not to be further increased, so that the single-furnace treatment capacity of the fluidized bed gasification furnace is low. Along with the increase of the content of the fine powder in the modern coal mining technology, the content of the fine powder in the coal as fired of the fluidized bed gasification furnace is increased, and the fine powder is easily taken out in the gasification furnace, i.e. the retention time of the fine powder is short, so that the fine powder can not fully react. Meanwhile, a large amount of semicoke fine powder brought out from the top of the fluidized bed gasification furnace is difficult to further convert in the gasification furnace due to the limitation of the operation temperature of the fluidized bed, and the bringing out of the large amount of semicoke fine powder has great influence on the total conversion rate of carbon in a gasification system, so that the problem to be solved is already needed.
How to realize the high-temperature operation of the fluidized bed gasification furnace and prevent the generation of large agglomerates, how to safely discharge the large agglomerates once the large agglomerates are generated, how to realize the high-efficiency conversion of fine powder, and the development of a high-temperature fluidized bed reaction device is important for the development of gasification of carbon-containing materials.
Disclosure of Invention
The invention aims to design a high-temperature fluidized bed gasification furnace which has simple structure, low cost and good safety and can gasify carbonaceous materials at high temperature.
A second object of the present invention is to provide a high temperature fluidized bed gasification process which is suitable for large scale gasification of carbonaceous materials.
The invention designs a high-temperature fluidized bed gasification furnace.
The invention relates to a high-temperature fluidized bed gasification furnace, which comprises three units, namely a high-temperature moving bed ash discharge unit, a high-temperature gasification unit and a semicoke fine powder circulating and conveying unit;
the high-temperature moving bed ash discharge unit is composed of a moving bed ash discharge circular furnace body, a bottom support body, a middle rotary support body, a central pipe, a rotary ash discharge tray, an ash discharge port, an upper ash discharge hopper, a lower ash discharge hopper and a bottom gasifying agent inlet pipe, wherein the bottom support body is positioned at the bottom of the moving bed ash discharge circular furnace body, the central pipe is fixed on the bottom support body and is positioned on a vertical central line of the bottom support body, an inlet of the central pipe is connected with one end of the bottom gasifying agent inlet pipe, the middle rotary support body is fixed on the bottom support body, the rotary ash discharge tray is fixed on the upper part of the middle rotary support body, an outlet of the central pipe is positioned in the middle rotary support body, the ash discharge port is positioned at the bottom end of the moving bed ash discharge circular furnace body, the ash discharge port is, the outlet of the lower deslagging hopper is connected with a high-temperature valve;
the high-temperature gasification reactor unit consists of a circular furnace body, a middle part of the circular furnace body and an upper part of the circular furnace body, wherein the lower part of the circular furnace body is provided with a lower gasification agent inlet pipe, a carbon-containing material inlet pipe, a baking furnace diesel oil inlet pipe, a sand inlet pipe, a first-stage semicoke fine powder inlet pipe and a second-stage semicoke fine powder inlet pipe;
the circular furnace body consists of a fire-resistant wear-resistant layer, a heat-insulating layer and a furnace body from inside to outside in sequence.
The lower gasification agent inlet pipe in the lower part of the circular furnace body is positioned at the lowest part, a carbon-containing material inlet pipe and a baking furnace diesel oil inlet pipe are arranged above the lower gasification agent inlet pipe, a first-stage semicoke fine powder inlet pipe is arranged above the baking furnace diesel oil inlet pipe, a sand grain inlet pipe is arranged above the carbon-containing material inlet pipe, and a second-stage semicoke fine powder inlet pipe is arranged above the sand grain inlet pipe.
The semicoke fine powder circulating and conveying unit comprises a primary cyclone separator, a primary vertical circulating pipe, a primary semicoke fine powder circulating control high-temperature valve, a secondary cyclone separator, a secondary vertical circulating pipe, a secondary semicoke fine powder circulating control high-temperature valve, a chilling water pipe, a carbon-containing material bin and a sand grain bin, wherein the primary cyclone separator is connected with a coal gas outlet of a gasification furnace, the primary vertical circulating pipe is connected with the bottom of the primary cyclone separator, the lower end of the primary vertical circulating pipe is connected with the primary semicoke fine powder circulating control high-temperature valve, the primary semicoke fine powder circulating control high-temperature valve is connected with a primary semicoke fine powder feeding pipe, the top of the primary cyclone separator is connected with the secondary cyclone separator, the bottom of the secondary cyclone separator is connected with the secondary vertical circulating pipe, the lower end of the secondary vertical circulating pipe is connected with the secondary semicoke fine powder circulating control high-temperature valve, and the secondary.
The diameter of the circular furnace body of the high-temperature gasification reactor unit is D, and the height of the circular furnace body is H; the diameter of the moving bed ash discharge circular furnace body is D, and the height H is 0.05-0.3H.
The method for gasifying the carbonaceous material comprises the following steps:
(1) production of gasification feedstock carbonaceous material and sand
After crushing, drying and screening the carbon-containing material to ensure that the moisture content of the carbon-containing material is less than 10wt% and the granularity is less than 10mm, sending the prepared carbon-containing material into a carbon-containing material bin 30, after crushing, drying and screening the crushed sand to ensure that the granularity of the sand is less than 0.25mm, and sending the prepared sand into a sand grain bin 31;
(2) high temperature gasification
a. Firstly, baking a high-temperature fluidized bed gasification furnace, introducing air and water vapor into a bottom gasifying agent inlet pipe of a high-temperature moving bed ash discharge unit and a lower gasifying agent inlet pipe of the lower part of the circular furnace body when the temperature of the lower part of the circular furnace body is higher than 850 ℃ and the temperature of the upper part of the circular furnace body is higher than 650 ℃, continuously adding prepared carbon-containing materials from a carbon-containing material feeding pipe of the lower part of the circular furnace body according to the air-coal ratio of 2.5-6 Nm3The ratio of the coal to the steam is 0.3-0.6 Kg/Kg, so that the carbonaceous material is combusted in the gasification furnace to obtain semi-coke furnace charge, and the furnace charge in the gasification furnace is gradually built;
b. when the bed pressure drop of the semicoke material in the high-temperature fluidized bed gasification furnace reaches 3-5 KPa, the system operation is switched to oxygen/steam blast after being stable, the temperature of the high-temperature fluidized bed gasification furnace is controlled at 850-900 ℃ in the switching process, and simultaneously, prepared sand grains and sand grain feeding amount are continuously added from a sand grain feeding pipe at the lower part of the round furnace body: the weight ratio of the raw coal feeding amount is 0.0045-0.03;
c. according to the oxygen-gas-coal ratio of 0.4-0.8 Nm3The ratio of the coal to steam is 0.5-1.2 Kg/Kg, and the temperature of the lower part of the circular furnace body is stabilized at 900-;
d. after the lower part of the circular furnace body is stabilized, oxygen and steam are introduced into a middle gasification agent feeding pipe in the middle of the circular furnace body, wherein the oxygen comprises the following components in percentage by weight: the volume ratio of the steam is less than 5: 1, maintaining the temperature of the middle part of the circular furnace body at 900-1150 ℃, and introducing oxygen and steam into an upper gasification agent feeding pipe at the upper part of the circular furnace body, wherein the oxygen: the volume ratio of the steam is less than 2.5: 1, maintaining the temperature of the upper part of the circular furnace body at 900-;
(3) slag discharge of high-temperature fluidized bed gasification furnace
In the gasification process, the slag discharge amount is controlled by adjusting the rotating speed of the rotary ash discharge furnace tray, so that the semicoke furnace charge in the high-temperature fluidized bed gasification furnace keeps the bed pressure drop between 3 and 5 KPa;
(4) purification and waste heat recovery of raw gas
The coarse coal gas flowing out of the coal gas outlet is separated by a primary cyclone separator, and the collected fine semi-coke powder is sent to a primary fine semi-coke powder feeding pipe to enter the lower part of the circular furnace body for conversion at high temperature through a primary vertical circulating pipe and a primary fine semi-coke powder circulation control high-temperature valve; the separated crude gas enters a secondary cyclone separator for re-separation, and the collected semicoke fine powder passes through a secondary vertical circulating pipe and a secondary semicoke fine powder circulation control high-temperature valve and is sent to a secondary semicoke fine powder feeding pipe to enter the lower part of the circular furnace body for conversion at high temperature; the roughly separated coal gas enters a radiation boiler, heat is recovered in a heat radiation mode, semi-coke fine powder is collected at the same time, and the collected semi-coke fine powder enters a circulating fluidized bed combustion boiler for combustion through a semi-coke fine powder collecting tank and a fine powder conveyor; the separated high-temperature coal gas sequentially passes through a waste heat recovery boiler, a steam superheater and a deoxidized water preheater, the coal gas is cooled to 50-150 ℃ and enters a water-cooling leaching tower, the non-collected fine powder is washed away, and the washed coal gas is output to a coal gas purification system;
(5) high temperature fluidized bed gasifier shutdown
When the furnace is normally stopped, firstly cutting off the oxygen at the lower part, the middle part and the top of the round furnace body and the ash discharge unit of the high-temperature moving bed; stopping adding coal; stopping adding sand grains; cutting off a gas pipeline entering the rear system, emptying the gas and gradually reducing the gas to normal pressure; and then increasing the slag discharge amount of the high-temperature fluidized bed gasification furnace, simultaneously increasing the steam amount of the high-temperature fluidized bed gasification furnace, controlling the temperature in the furnace to be 900 ℃, stopping air intake after the furnace charge is discharged, and finally blowing the system once by using steam and air respectively.
The sand grains are especially sand grains rich in quartz.
The carbonaceous material is especially coal, solid garbage and biomass.
The steam used in the high temperature fluidized bed gasification furnace as described above is supplied by:
the method comprises the steps that deoxygenated water enters a deoxygenated water preheater to be preheated and then enters boiler bubbles, the heat recovered by a waste heat recovery boiler in the boiler bubbles is heated to be changed into saturated steam, and the saturated steam enters a steam superheater and is heated to be changed into superheated steam from high-temperature coal gas discharged from the waste heat recovery boiler and then is supplied to a high-temperature fluidized bed gasification furnace to be gasified.
The invention has the following advantages:
(1) the average operating temperature of the whole bed of the high-temperature fluidized bed gasification furnace is close to the softening temperature of the carbonaceous material ash, so that the operation of the gasification furnace close to the ash melting point is realized, the gasification reaction rate is high, the carbon conversion rate is high, and the single-furnace treatment capacity is high.
(2) The high-efficiency conversion of a large amount of semi-coke fine powder brought out from the top of the high-temperature fluidized bed gasification furnace is realized, the semi-coke fine powder is further converted in the high-temperature gasification furnace, the common problem of the fluidized bed gasification furnace is solved, and the carbon conversion rate is 90-96%.
(3) The gasification is carried out by adopting air, oxygen enrichment or pure oxygen, and the gasification furnace is suitable for different occasions;
(4) through the ash discharge of the high-temperature moving bed, the continuous discharge reactor of the ash of the gasification furnace can be realized, and large slag blocks in the reactor can be discharged, so that the large slag blocks are prevented from being further increased, and the ash discharge device plays a vital role in the safe and stable production of the high-temperature fluidized bed gasification furnace.
Drawings
FIG. 1 is a schematic view of a high-temperature fluidized-bed reactor.
FIG. 2 is a flow chart of a process for gasifying carbonaceous materials in a high-temperature fluidized bed.
The figure illustrates that 1 is a moving bed ash discharge circular furnace body, 2 is a circular furnace body lower part, 3 is a circular furnace body middle part, 4 is a circular furnace body upper part, 5 is a bottom support body, 6 is a middle rotary support body, 7 is a central pipe, 8 is a rotary ash discharge furnace disc, 9 is an ash discharge port, 10 is an upper slag discharge hopper, 11 is a lower slag discharge hopper, 12 is a bottom gasifying agent inlet pipe, 13 is a lower gasifying agent inlet pipe, 14 is a carbon-containing material inlet pipe, 15 is a baking furnace diesel oil inlet pipe, 16 is a sand inlet pipe, 17 is a first-stage semicoke fine powder inlet pipe, 18 is a second-stage semicoke fine powder inlet pipe, 19 is a middle gasifying agent inlet pipe, 20 is an upper gasifying agent inlet pipe, 21 is a desulfurizing agent inlet pipe, 22 is a coal gas outlet, 23 is a first-stage cyclone separator, 24 is a first-stage vertical circulating pipe, 25 is a first-stage, 27 is a two-stage vertical circulation pipe, 28 is a two-stage semicoke fine powder circulation control high-temperature valve, 29 is a chilling water pipe, 30 is a carbonaceous material bin, 31 is a sand bin, 32 is a carbonaceous material belt conveyor, 33 is a carbonaceous material linear vibrating screen, 34 is a carbonaceous material crusher, 35 is a carbonaceous material drier, 36 is a sand belt conveyor, 37 is a sand linear vibrating screen, 38 is a sand crusher, 39 is a sand storage bin, 40 is a sand conveyor, 41 is a dried carbonaceous material belt conveyor (1), 42 is a dried carbonaceous material elevator (1), 43 is a dried carbonaceous material storage bin, 44 is a dried carbonaceous material belt conveyor (2), 45 is a dried carbonaceous material elevator (2), 46 is a feed hopper, 47 is a rotary feeder, 48 is a radiation boiler, 49 is a semicoke fine powder collection tank, 50 is a fine powder conveyor, 51 is a waste heat recovery boiler, 52 is a boiler bubble, 53 is a steam superheater, 54 is a deoxidized water preheater, 55 is a venturi scrubber, 56 is a water-cooled leaching tower, 57 is a flash tower, 58 is a gas-water separator, 59 is a desulfurizing tower, 60 is a gas pressure regulating valve, 61 is an air cylinder, 62 is a superheated steam cylinder, and 63 is an oxygen cylinder.
Detailed Description
In an embodiment, a method for gasifying carbonaceous materials on a high temperature fluidized bed reactor consisting of three units, a high temperature moving bed ash discharge unit, a high temperature gasification reactor unit, and a semicoke fines recycle conveyor unit, is provided: the high-temperature gasification reaction unit can be operated at high temperature to realize the high-efficiency conversion of the carbon-containing materials, and the ash slag and the sand grains are fully mixed in the moving bed ash discharge unit at high temperature, so that the probability of the high-temperature ash being bonded into massive slag is reduced; meanwhile, partial gasifying agent is introduced into the moving bed, so that the high-temperature ash and slag are converted again, the gas-solid contact efficiency is increased, and the higher carbon conversion rate of the high-temperature fluidized bed is ensured.
The method for gasifying the carbonaceous material and the special equipment thereof are described as follows by combining the attached drawings:
example 1:
the high-temperature fluidized bed gasification furnace comprises a high-temperature moving bed ash discharge unit, a high-temperature gasification reactor unit and a semicoke fine powder circulating and conveying unit;
the high-temperature moving bed ash discharge unit comprises a moving bed ash discharge circular furnace body 1, a bottom support body 5, a middle rotary support body 6, a central pipe 7, a rotary ash discharge furnace disc 8, an ash discharge port 9, an upper ash discharge hopper 10, a lower ash discharge hopper 11 and a gasifying agent air inlet pipe 12, wherein the bottom support body 5 is positioned at the bottom of the moving bed ash discharge circular furnace body 1, the central pipe 7 is fixed on the bottom support body 5, the central pipe 7 is positioned on a vertical central line of the bottom support body 5, an inlet of the central pipe 7 is connected with one end of the bottom gasifying agent air inlet pipe 12, the middle rotary support body 6 is fixed on the bottom support body 5, the rotary ash discharge disc 8 is fixed on the upper part of the middle rotary support body 6, an outlet of the central pipe 7 is positioned in the middle rotary support body 6, the ash discharge port 9 is positioned at the bottom, the outlet of the upper deslagging hopper 10 is connected with the inlet of the lower deslagging hopper 11 through a high-temperature valve, and the outlet of the lower deslagging hopper 11 is connected with the high-temperature valve;
the high-temperature gasification reactor unit comprises a circular furnace body consisting of a circular furnace body lower part 2, a circular furnace body middle part 3 and a circular furnace body upper part 4, wherein the circular furnace body lower part 2 is provided with a lower gasification agent inlet pipe 13, a carbon-containing material inlet pipe 14, a baking furnace diesel oil inlet pipe 15, a sand grain inlet pipe 16, a first-stage semicoke fine powder inlet pipe 17 and a second-stage semicoke fine powder inlet pipe 18, the circular furnace body middle part 3 is provided with a middle gasification agent inlet pipe 19, the circular furnace body upper part 4 is provided with an upper gasification agent inlet pipe 20 and a desulfurizer inlet pipe 21, and the top of the circular furnace body upper part 4 is provided;
the circular furnace body consists of a fire-resistant wear-resistant layer, a heat-insulating layer and a furnace body from inside to outside in sequence.
A gasifying agent inlet pipe 13 in the lower part 2 of the circular furnace body is positioned at the lowest part, a carbon-containing material inlet pipe 14 and a drying furnace diesel oil inlet pipe 15 are arranged above the gasifying agent inlet pipe 13, a first-stage semicoke fine powder inlet pipe 17 is arranged above the drying furnace diesel oil inlet pipe 15, a sand grain inlet pipe 16 is arranged above the carbon-containing material inlet pipe 14, and a second-stage semicoke fine powder inlet pipe 18 is arranged above the sand grain inlet pipe 16.
The semicoke fine powder circulating and conveying unit comprises a primary cyclone separator 23, a primary vertical circulating pipe 24, a primary semicoke fine powder circulating control high-temperature valve 25, a secondary cyclone separator 26, a secondary vertical circulating pipe 27 and a secondary semicoke fine powder circulating control high-temperature valve 28, wherein the primary cyclone separator 23 is connected with a gasification furnace gas outlet 22, the bottom of the primary cyclone separator 23 is connected with the primary vertical circulating pipe 24, the lower end of the primary vertical circulating pipe 24 is connected with the primary semicoke fine powder circulating control high-temperature valve 25, the primary semicoke fine powder circulating control high-temperature valve 25 is connected with a primary semicoke fine powder feeding pipe 17, the top of the primary cyclone separator 23 is connected with the secondary cyclone separator 26, the bottom of the secondary cyclone separator 26 is connected with the secondary vertical circulating pipe 27, the lower end of the secondary vertical circulating pipe 27 is connected with the secondary semicoke fine powder circulating control high-temperature valve 28, the second-stage semicoke fine powder circulation control high-temperature valve 28 is connected with the second-stage semicoke fine powder feeding pipe 18.
The diameter of a circular furnace body of the high-temperature gasification reactor unit is D, and the height of the circular furnace body is H; the moving bed ash discharge round furnace body 1 has the diameter D and the height H of 0.05H.
The invention discloses a method for gasifying Shaanxi Shenmu bituminous coal, which comprises the following steps:
(1) preparation of gasification raw material Shaanxi Shenmu soft coal and sand grains
The method comprises the steps of crushing the Shaanxi Shenmu bituminous coal, drying and screening to enable the moisture of a carbon-containing material to be 8 wt% and enable the particle size to be smaller than 10mm, sending the prepared Shaanxi Shenmu bituminous coal into a carbon-containing material bin 30, conveying the crushed Shaanxi Shenmu bituminous coal to a carbon-containing material linear vibrating screen 33 through a carbon-containing material belt conveyor 32, crushing the bituminous coal with the particle size larger than 10mm to be crushed coal with the particle size smaller than 10mm through a carbon-containing material crusher 34, sending the crushed coal and crushed coal under the carbon-containing material linear vibrating screen 33 into a carbon-containing material dryer 35, sending the dried bituminous coal into a dried carbon-containing material belt conveyor 41 and a dried carbon-containing material lifter 42. After being crushed, sand grains (the content of quartz is more than 95wt percent) are dried and screened, and the prepared sand grains are sent into a sand grain bin 31; the sand grains are conveyed to a sand grain linear vibrating screen 37 by a sand grain belt conveyor 36, the sand grains with the grain size larger than 0.25mm are crushed by a sand grain crusher 38 to be crushed sand grains with the grain size smaller than 0.25mm, and the crushed sand grains and undersize crushed sand grains of the sand grain linear vibrating screen 37 are conveyed to a sand grain storage bin 39 for standby.
(2) High temperature gasification
a. Firstly, the gasifier is dried, the air for drying the gasifier comes from the air sub-cylinder 61, the diesel oil enters the gasifier through the diesel oil inlet pipe 15 for drying the gasifier, and the air respectively enters the gasifier through the gasifying agent inlet pipe 12 and the lower gasifying agent inlet pipe 13. When the temperature of the lower part 2 of the circular furnace body is 860 ℃, the temperature of the upper part 4 of the circular furnace body is 650 ℃, air and water vapor are introduced into a bottom gasifying agent inlet pipe 12 of the high-temperature moving bed ash discharge unit and a lower gasifying agent inlet pipe 13 of the lower part 2 of the circular furnace body, and the air is 4500Nm3At 500Kg/h steam (steam from superheated steam cylinder 62), the rotary feeder 47 was started to continuously feed crushed coal from the carbonaceous material feed pipe 14 in a constant amount, keeping the feed rate at 1500Kg/h, and keeping the feed rate at 4500Nm3/h and 500 Kg/h. And according to the air-coal ratio of 3Nm3The ratio of coal to steam is 0.33KgPerforming operation on/Kg to enable the carbon-containing materials to be combusted in the gasification furnace, obtaining semi-coke furnace burden, and gradually establishing the furnace burden in the gasification furnace;
b. when the bed pressure drop of the semicoke material in the high-temperature fluidized bed gasification furnace reaches 4KPa, the system operation is switched to oxygen/steam blast after being stable, the oxygen comes from an oxygen gas distributing cylinder 63, and the oxygen inlet amount is 750Nm3The steam amount is 1500Kg/h, the furnace body temperature of the high-temperature fluidized bed gasification furnace is controlled at 850 ℃ in the switching process, and simultaneously, prepared sand grains are continuously added from a sand grain feeding pipe 16 at the lower part 2 of the circular furnace body, and the sand grain feeding amount is as follows: the weight ratio of the raw coal feeding amount is 0.0045;
c. then slowly adjusting the flow of oxygen and steam, gradually adjusting the pressure of the gasification system to 0.6MPa, simultaneously adjusting the coal feeding amount to 2000Kg/h and the oxygen amount to 1200Nm3The steam amount is 2200Kg/h, the operation is carried out according to the oxygen-coal ratio of 0.6Nm3/Kg and the steam-coal ratio of 1.1Kg/Kg, and the temperature of the lower part 2 of the circular furnace body is stabilized at 1100 ℃;
d. after the lower part 2 of the circular furnace body is stabilized, oxygen and steam are introduced into the middle gasification agent feeding pipe 19 in the middle part 3 of the circular furnace body, wherein the oxygen: the volume ratio of steam is 2.5: 1, oxygen amount 120Nm3The steam amount is 39Kg/h, the temperature of the middle part 3 of the circular furnace body is maintained at 1100 ℃, oxygen and steam are introduced into an upper gasifying agent inlet pipe 20 of the circular furnace body, and the oxygen: the volume ratio of steam is 1.5: 1, oxygen amount 60Nm3The steam amount is 32Kg/h, and the temperature of the upper part 4 of the circular furnace body is kept at 1000 ℃. A laser cooling water pipe 29 is arranged on the top of the circular furnace body to lead water in, so that the temperature of the coal gas outlet 22 is controlled at 1000 ℃, and the operating pressure of the high-temperature fluidized bed gasification furnace is controlled at 0.6 MPa;
(3) slag discharge of high-temperature fluidized bed gasification furnace
In the gasification process, ash in the moving bed ash discharge circular furnace body 1 is discharged into an upper ash discharge hopper 10 through a rotary ash discharge furnace disc 8, then enters a lower ash discharge hopper 11, and the ash is discharged from the lower ash discharge hopper 11 periodically. The slag discharge amount is controlled by adjusting the rotating speed of the rotary ash discharge furnace plate 8, so that the pressure drop of a bed layer of semi-coke furnace charge in the high-temperature fluidized bed gasification furnace is kept between 4 KPa;
(4) purification and waste heat recovery of raw gas
In the operation process, the temperature of the coal gas at the outlet of the gasification furnace is ensured to be 1000 ℃ by adjusting the flow rate of the chilling water in the chilling water pipe 29 at the top of the furnace. The crude gas is separated by a first-stage cyclone separator 23, the collected fine semi-coke powder is sent into a gasification furnace through a first-stage fine semi-coke powder feeding pipe 17 under the action of steam blowing by a first-stage vertical circulating pipe 24 and a first-stage fine semi-coke powder circulation control high-temperature valve 25 to participate in reaction again; the crude gas at the top outlet of the primary cyclone separator 23 is separated by a secondary cyclone separator 26, the collected fine semi-coke powder passes through a secondary vertical circulating pipe 27 and a secondary fine semi-coke powder circulation control high-temperature valve 28, and is fed into the gasification furnace through a secondary fine semi-coke powder feeding pipe 18 under the action of steam blowing to participate in reaction again; the roughly separated coal gas enters a radiation boiler 48 to recover heat in a heat radiation mode and capture semicoke fine powder, and the captured semicoke fine powder enters a circulating fluidized bed combustion boiler for combustion through a semicoke fine powder collecting tank 49 and a fine powder conveyor 50; the separated high-temperature coal gas sequentially passes through a waste heat recovery boiler 51, a steam superheater 53 and a deoxidized water preheater 54, the temperature of the coal gas is reduced to 100 ℃, and the reduced-temperature coal gas sequentially passes through a Venturi scrubber 55, a tower plate type water washing tower 56, a flash tower 57 and a gas-water separator 58, is further reduced in temperature and dedusted, and is then conveyed to a coal gas purification second-stage section through a coal gas pressure regulating valve 60.
(5) High temperature fluidized bed gasifier shutdown
When the furnace is normally stopped, firstly cutting off oxygen of the lower part 2, the middle part 3 and the top part 4 of the circular furnace body and the ash discharge unit of the high-temperature moving bed; stopping the rotary feeder 47 and stopping the coal feeding; stopping adding sand grains; cutting off a gas pipeline entering the rear system, emptying the gas, adjusting a gas pressure adjusting valve 60, and gradually reducing the pressure to normal pressure; then, the rotating speed of the rotary ash discharging furnace plate 8 is increased, the slag discharge amount of the high-temperature fluidized bed gasification furnace is increased, the steam amount of the high-temperature fluidized bed gasification furnace is increased, the temperature in the furnace is controlled to be 900 ℃, after the furnace burden is discharged, air inlet is stopped, and finally the system is respectively swept by steam and air.
The water vapor used by the high-temperature fluidized bed gasification furnace is provided by the following modes:
the deoxidized water enters a deoxidized water preheater 54 to be preheated and then enters a boiler bubble 52, the heat recovered by a waste heat recovery boiler 51 in the boiler bubble 52 is heated to become saturated steam, and the saturated steam enters a steam superheater 53 to be heated to become superheated steam by high-temperature coal gas coming out of the waste heat recovery boiler 51 and then is supplied to a high-temperature fluidized bed gasification furnace for gasification.
Example 2:
the diameter of a circular furnace body of the high-temperature gasification reactor unit is D, and the height of the circular furnace body is H; the moving bed ash discharge round furnace body 1 has the diameter D and the height of 0.05H.
The gasification raw material is Yunnan wenshan brown coal, the coal feeding amount is 2600Kg/h, and the oxygen feeding amount is 1600Nm3The steam inlet amount is 2500Kg/h, the sand inlet amount is 24Kg/h, the pressure of the gasification furnace is controlled at 1.0MPa, the temperature of the lower part 2 of the circular furnace body is stabilized at 950 ℃, the oxygen amount is 155Nm3/h and the steam amount is 50Kg/h are introduced into the middle gasification agent inlet pipe 19 of the circular furnace body, the temperature of the middle part 3 of the circular furnace body is maintained at 980 ℃, and the oxygen amount is 77Nm introduced into the upper gasification agent inlet pipe 20 of the circular furnace body3The temperature of the upper part (4) of the circular furnace body is maintained at 950 ℃ with a steam amount of 41Kg/h, and the rest is the same as that of the embodiment 1.
Example 3:
the diameter of a circular furnace body of the high-temperature gasification reactor unit is D, and the height of the circular furnace body is H; the moving bed ash discharge round furnace body 1 has the diameter D and the height of 0.15H.
The gasification raw material is Jincheng anthracite, the coal feeding amount is 3000Kg/h, and the oxygen feeding amount is 2100Nm33500Kg/h of steam and 38Kg/h of sand, 1.5MPa of pressure of gasification furnace, 1200 deg.C of lower part 2 of circular furnace, 190Nm of oxygen introduced into middle gasification agent inlet pipe 19 of circular furnace3The steam amount is 61Kg/h, the temperature of the middle part 3 of the circular furnace body is kept at 1125 ℃, and the oxygen amount introduced into the upper gasification agent inlet pipe 20 of the circular furnace body is 95Nm3The temperature of the upper part 4 of the circular furnace body is maintained at 1050 ℃ with the steam amount of 51Kg/h, and the rest is the same as that in the embodiment 1.
Example 4:
the diameter of a circular furnace body of the high-temperature gasification reactor unit is D, and the height of the circular furnace body is H; the moving bed ash discharge round furnace body 1 has the diameter D and the height of 0.05H.
The gasification raw material is Shanxi Shenmu soft coalThe coal amount is 3700Kg/h, the oxygen intake is 2250Nm3The steam inflow is 4000Kg/h, the sand inflow is 55Kg/h, the pressure of the gasification furnace is controlled to be 2.0MPa, and the oxygen amount of the middle gasification agent inlet pipe (19) of the circular furnace body is 219Nm3The amount of the oxygen and the steam are 70Kg/h, and the amount of the oxygen introduced into an upper gasifying agent inlet pipe (20) of the circular furnace body is 110Nm3The rest of the procedure was as in example 1, except that the amounts of steam were 59 Kg/h.
Example 5:
the diameter of a circular furnace body of the high-temperature gasification reactor unit is D, and the height of the circular furnace body is H; the moving bed ash discharge round furnace body 1 has the diameter D and the height of 0.15H.
The gasification raw material is Shanxi Shenmu soft coal, the coal feeding amount is 4100Kg/h, and the oxygen feeding amount is 2500Nm3The steam inlet amount is 4500Kg/h, the sand inlet amount is 74Kg/h, the pressure of the gasification furnace is controlled at 2.5MPa, and the oxygen amount is 245Nm in the middle gasification agent inlet pipe 19 of the circular furnace body3The amount of the steam and the amount of the steam are 79Kg/h, and the amount of the oxygen introduced into the upper gasification agent inlet pipe 20 of the circular furnace body is 122Nm3The rest of the procedure was as in example 1, except that the amounts of steam were 66 Kg/h.
Example 6:
the diameter of a circular furnace body of the high-temperature gasification reactor unit is D, and the height of the circular furnace body is H; the moving bed ash discharge round furnace body 1 has the diameter D and the height of 0.3H.
The gasification raw material is the Shanxi Shenmu soft coal, the coal feeding amount is 4500Kg/h, the oxygen feeding amount is 2700Nm3The steam inflow is 5000Kg/h, the sand inflow is 134Kg/h, the pressure of the gasification furnace is controlled at 3.0MPa, and the oxygen amount introduced into the middle gasification agent inlet pipe 19 of the circular furnace body is 268Nm3The amount of the steam and the amount of the steam are 86Kg/h, and the amount of the oxygen introduced into the upper gasification agent inlet pipe 20 of the circular furnace body is 134Nm3The rest of the procedure was as in example 1, with a steam content of 72 Kg/h.
The composition of the synthesis gas produced by high temperature fluidized bed gasification of crushed coal as carried out under the conditions of examples 1-6 is shown in Table 1.
TABLE 1 composition of gas produced by high-temperature fluidized bed gasification of crushed coal under different conditions
| Example 1 | Example 2 | Example 3 | Example 4 | Example 5 | Example 6 | |
| Gasification pressure, MPa | 0.6 | 1.0 | 1.5 | 2.0 | 2.5 | 3.0 |
| Gasification temperature of | 1100 | 950 | 1200 | 1105 | 1095 | 1100 |
| Coal input in kg/h | 2000 | 2600 | 3000 | 3700 | 4100 | 4500 |
| Total oxygen intake, Nm3/h | 1380 | 1832 | 2385 | 2579 | 2867 | 3102 |
| Total steam amount of Kg/h | 2271 | 2591 | 3612 | 4129 | 4645 | 5158 |
| Dry gas composition Vol% | ||||||
| H2 | 32.5 | 33.2 | 31.7 | 33.5 | 33.9 | 34.2 |
| N2 | 8.6 | 5.5 | 5.8 | 6.1 | 5.5 | 5.8 |
| CO | 30.4 | 28.6 | 35.4 | 32.8 | 34.1 | 33.5 |
| CH4 | 2.6 | 4.2 | 0.5 | 3.3 | 3.5 | 3.8 |
| CO2 | 25.9 | 28.5 | 26.6 | 24.3 | 23 | 22.7 |
| Gas production rate Nm3/Kg | 2.04 | 1.92 | 2.03 | 2.02 | 2.01 | 2.01 |
| Carbon conversion% | 91.5 | 94.1 | 90.0 | 91.2 | 90.8 | 90.6 |
。
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