CN107880918A - A kind of pyrolysis of coal and the system and method for fluidizing gas coupling processed - Google Patents
A kind of pyrolysis of coal and the system and method for fluidizing gas coupling processed Download PDFInfo
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- CN107880918A CN107880918A CN201711217143.8A CN201711217143A CN107880918A CN 107880918 A CN107880918 A CN 107880918A CN 201711217143 A CN201711217143 A CN 201711217143A CN 107880918 A CN107880918 A CN 107880918A
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- 238000000197 pyrolysis Methods 0.000 title claims abstract description 82
- 239000003245 coal Substances 0.000 title claims abstract description 64
- 230000008878 coupling Effects 0.000 title claims abstract description 12
- 238000010168 coupling process Methods 0.000 title claims abstract description 12
- 238000005859 coupling reaction Methods 0.000 title claims abstract description 12
- 238000000034 method Methods 0.000 title claims description 27
- 239000007789 gas Substances 0.000 claims abstract description 94
- 239000012071 phase Substances 0.000 claims abstract description 61
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims abstract description 45
- 239000000571 coke Substances 0.000 claims abstract description 31
- 239000002737 fuel gas Substances 0.000 claims abstract description 26
- 238000002485 combustion reaction Methods 0.000 claims abstract description 19
- 239000007790 solid phase Substances 0.000 claims abstract description 13
- 239000000428 dust Substances 0.000 claims abstract description 8
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 54
- 239000003546 flue gas Substances 0.000 claims description 54
- 238000001035 drying Methods 0.000 claims description 22
- 239000011280 coal tar Substances 0.000 claims description 20
- 238000005243 fluidization Methods 0.000 claims description 13
- 239000002245 particle Substances 0.000 claims description 13
- 238000000926 separation method Methods 0.000 claims description 13
- 238000000746 purification Methods 0.000 claims description 10
- 239000000843 powder Substances 0.000 claims description 9
- 239000000446 fuel Substances 0.000 claims description 5
- 239000007787 solid Substances 0.000 claims description 5
- 238000005507 spraying Methods 0.000 claims description 5
- 239000007921 spray Substances 0.000 claims description 4
- 238000007599 discharging Methods 0.000 claims description 3
- 239000011286 gas tar Substances 0.000 claims description 3
- 238000010438 heat treatment Methods 0.000 claims description 3
- 239000000779 smoke Substances 0.000 abstract description 3
- 239000012530 fluid Substances 0.000 abstract 6
- 239000000839 emulsion Substances 0.000 abstract 1
- 239000007792 gaseous phase Substances 0.000 abstract 1
- 238000004519 manufacturing process Methods 0.000 description 14
- 239000000463 material Substances 0.000 description 10
- 230000008569 process Effects 0.000 description 9
- 239000000126 substance Substances 0.000 description 6
- 230000005540 biological transmission Effects 0.000 description 3
- 238000006243 chemical reaction Methods 0.000 description 3
- 238000007789 sealing Methods 0.000 description 3
- 239000007788 liquid Substances 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 230000009471 action Effects 0.000 description 1
- 230000003139 buffering effect Effects 0.000 description 1
- 239000013064 chemical raw material Substances 0.000 description 1
- 239000002817 coal dust Substances 0.000 description 1
- 238000007796 conventional method Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000009826 distribution Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 230000005611 electricity Effects 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 238000004880 explosion Methods 0.000 description 1
- 239000002360 explosive Substances 0.000 description 1
- 239000010419 fine particle Substances 0.000 description 1
- 230000005484 gravity Effects 0.000 description 1
- 239000011261 inert gas Substances 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 239000003921 oil Substances 0.000 description 1
- 150000002978 peroxides Chemical class 0.000 description 1
- 238000010248 power generation Methods 0.000 description 1
- 238000011112 process operation Methods 0.000 description 1
- 230000002035 prolonged effect Effects 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 231100000331 toxic Toxicity 0.000 description 1
- 230000002588 toxic effect Effects 0.000 description 1
- 239000013585 weight reducing agent Substances 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B53/00—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form
- C10B53/04—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form of powdered coal
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B57/00—Other carbonising or coking processes; Features of destructive distillation processes in general
- C10B57/08—Non-mechanical pretreatment of the charge, e.g. desulfurization
- C10B57/10—Drying
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/46—Gasification of granular or pulverulent flues in suspension
- C10J3/54—Gasification of granular or pulverulent fuels by the Winkler technique, i.e. by fluidisation
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/72—Other features
- C10J3/82—Gas withdrawal means
- C10J3/84—Gas withdrawal means with means for removing dust or tar from the gas
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0913—Carbonaceous raw material
- C10J2300/0943—Coke
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/16—Integration of gasification processes with another plant or parts within the plant
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/16—Integration of gasification processes with another plant or parts within the plant
- C10J2300/1603—Integration of gasification processes with another plant or parts within the plant with gas treatment
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/16—Integration of gasification processes with another plant or parts within the plant
- C10J2300/1603—Integration of gasification processes with another plant or parts within the plant with gas treatment
- C10J2300/1615—Stripping
Landscapes
- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Organic Chemistry (AREA)
- Combustion & Propulsion (AREA)
- Materials Engineering (AREA)
- Fluidized-Bed Combustion And Resonant Combustion (AREA)
Abstract
The present invention proposes a kind of pyrolysis of coal and the system for fluidizing gas coupling processed, including pyrolysis reactor, Pneumatic conveyer, stokehold cyclone separator and fluid bed producer；Pyrolysis reactor includes fuel gas entrance, pyrolysis gas outlet, exhanst gas outlet, multitubular bundles distributing device and Re Jiao outlets；Pneumatic conveyer includes pressurization smoke inlet and Re Jiao feed-lines；Stokehold cyclone separator includes gaseous phase outlet, solid-phase outlet；Fluid bed producer includes cyclone separator after fluid bed and stove, and fluid bed is divided into dilute-phase zone and emulsion zone；Cyclone separator includes coke powder smoke inlet, feed back outlet, after-flame dust export and fuel gas outlet after stove.Scheme proposed by the present invention make it that the conveying of high-temperature semi-coke is safer, and the cyclone separator of stokehold solves the interference problem of conveying gaseous exchange fluidized bed combustion, protects the safety and stability of fluid bed producer, improves the service life of fluid bed.
Description
Technical Field
The invention relates to the technical field of coal stepped and stepped utilization, in particular to a system and a method for coupling coal pyrolysis and fluidization gas production.
Background
In China's coal resources, annual light coal with high volatile content accounts for a large proportion, annual light coal with a drying base volatile content of more than 28% accounts for about 3/4 of national coal reserves, and annual light coal with a drying base volatile content of more than 35% accounts for about 50 of national coal reserves. The coal directly burned in China accounts for about 80% of the total coal amount, more than half of the coal directly burned is used for power generation, the chemical energy in the light coal is completely converted into heat energy for many years, and potential oil, gas and chemicals with high added values in the light coal are wasted.
If the heterogeneity of the coal molecular structure composition and the difference of the conversion characteristics of different components can be fully considered to further implement the grading conversion, the method has great significance for improving the comprehensive utilization rate of the young coal in China. Based on the above, Guo Musun academy of Chinese academy of sciences proposes a coal topping process for oil, gas, heat, electricity and the like co-production based on pyrolysis of young coal, namely, before the young coal is utilized, the young coal is treated by a simple process with mild conditions to obtain liquid and gas products, the liquid and gas products are used as chemical raw materials, and the remaining solid residue semi-coke is sent to be combusted or gasified, so that the comprehensive utilization rate of the young coal is greatly improved, and simultaneously, the gas products and the chemical products which are urgently needed by society are obtained.
The prior art discloses a coal pyrolysis process for conveying a high-temperature semicoke buried scraper, as shown in figure 1, the process flow is as follows: and conveying the 800 ℃ high-temperature semicoke discharged from the pyrolysis furnace 1 to the inlet of the closed high-temperature buried scraper 3 through the rotary feeder 2. The material is conveyed to a material inlet of a fluidized bed boiler through a high-temperature embedded scraper 3, and an outlet of the high-temperature embedded scraper enters an inlet 4 of a fluidization area of the boiler. Simultaneously, primary air enters from a primary air inlet 51 and is conveyed to the fluidized zone 5 of the boiler through a boiler fan 8, and the primary air enables the semi-coke particles to enter a fluidized state and be combusted. The small particles and gases such as CO flow upwards through the bed layer and enter the combustion zone 6. Secondary air enters from a secondary air inlet 61 and is mixed with the secondary air to be further combusted as fuel gas of the combustion zone 6, and then coke powder and flue gas enter a boiler cyclone separator 9 to be subjected to gas-solid separation. The unburned coke powder returns to the fluidized zone through a material returning port to be continuously combusted. The burnt-off dust is discharged out of the boiler with the flue gas and heated by the steam generator 10.
However, the above-mentioned techniques have the following drawbacks: (1) in the pyrolysis furnace, pyrolysis gas is generated along with the generation of high-temperature semicoke, and the pyrolysis gas contains CO with the proportion of more than 20 percent and belongs to toxic, combustible and explosive gas; (2) the high-temperature embedded scraper is adopted to convey high-temperature semicoke, pyrolysis gas can enter the high-temperature embedded scraper together with the high-temperature semicoke, but the high-temperature embedded scraper is difficult to completely seal the driving end and the tail wheel part due to the structural characteristics, particularly, the temperature is greatly changed in a production state, so that each sealing surface is more difficult to realize, and the environmental pollution can be caused; (3) the inside of the high-temperature buried scraper and the feeding area of the boiler are difficult to completely separate, open fire in the boiler easily enters the inside of the buried scraper to cause pyrolysis gas explosion, and the method is also a potential safety hazard.
Disclosure of Invention
In order to solve the technical problems, the invention aims to provide a system and a method for pyrolysis gas making combined chemical industry aiming at medium-low-order pulverized coal, and aims to achieve the purposes of improving the energy utilization efficiency and ensuring the safety of the system by adopting a mode of coupling pyrolysis furnace, fluidized bed gas making furnace, high-temperature semicoke pneumatic transmission and cyclone separation.
In order to achieve the aim, the invention provides a system for coupling coal pyrolysis and fluidized gas production, which is characterized by comprising a pyrolysis reactor, a pneumatic conveying device, a stokehole cyclone separator and a fluidized bed gas production furnace; wherein,
the pyrolysis reactor comprises a fuel gas inlet, a pyrolysis gas outlet, a flue gas outlet, a multi-tube-bundle distributor arranged at the top and a hot coke outlet at the bottom;
the pneumatic conveying device comprises a pressurized flue gas inlet and a hot coke conveying pipeline; one end of the hot coke conveying pipeline is connected with the pressurized flue gas inlet and the hot coke outlet, and the other end of the hot coke conveying pipeline is connected with the stokehole cyclone separator; further, the pressurized flue gas inlet is connected with a flue gas pressurizing device;
the stokehole cyclone separator comprises a gas phase outlet arranged at the top and a solid phase outlet arranged at the bottom;
the fluidized bed gas making furnace comprises a fluidized bed and a cyclone separator arranged at the rear of the furnace,
the fluidized bed is divided into a dilute phase area and a dense phase area; the dilute phase zone is provided with a gas phase inlet, a secondary air inlet and a coke powder flue gas outlet, the secondary air inlet is preferably higher than the gas phase inlet, and the gas phase inlet is connected with the gas phase outlet; the dense-phase area is provided with a solid phase inlet, a pulverized coal inlet, a primary air inlet, a feed back inlet and a burner, and the solid phase inlet is connected with the solid phase outlet through an inclined pipe; further, the upper two-thirds height part of the fluidized bed is the dilute phase zone, and the lower one-third height part of the fluidized bed is the dense phase zone;
the furnace rear cyclone separator comprises a coke powder flue gas inlet, a return material outlet, a burnt dust outlet and a fuel gas outlet, wherein the coke powder flue gas inlet is connected with the coke powder flue gas outlet, and the return material outlet is connected with the return material inlet; further, the burnt dust outlet is connected with a heat exchange device.
Preferably, the elevation of said stokehole cyclone is located between said overfire air inlet and said dense phase zone.
Further, the system also comprises a purification device and a spraying device which are connected with each other; purifier includes the pyrolysis gas entry, spray set includes purification gas export and coal tar export, the pyrolysis gas entry with the pyrolysis gas export links to each other.
Specifically, the coal tar outlet is divided into a first coal tar outlet and a second coal tar outlet; wherein the second coal tar outlet is connected with a burner of the fluidized bed.
Further, the pyrolysis reactor comprises radiant tube heaters, and a plurality of the radiant tube heaters are arranged in heating zones in the pyrolysis reactor from top to bottom;
the pyrolysis gas outlet, the flue gas outlet and the fuel gas inlet are all provided with a plurality of gas inlets and are arranged on the side wall of the pyrolysis reactor from top to bottom.
Preferably, the fuel gas inlet is connected to the fuel gas outlet.
Further, the system comprises a screw conveyor, a drying lifting pipe and a hopper; wherein,
the spiral conveyor is connected with the multi-tube bundle distributor;
the lower part of the drying lifting pipe is provided with a coal powder feeding hole and a drying gas inlet, and the upper part of the drying lifting pipe is provided with a coal powder discharging hole;
the hopper is connected with the pulverized coal discharge port, and the lower part of the hopper is connected with the screw conveyer.
Preferably, the drying gas inlet is connected with the flue gas outlet.
The invention also provides a method for coupling coal pyrolysis and fluidization gas production, which is characterized by comprising the following steps:
A. coal pyrolysis: drying the pulverized coal, adding the dried pulverized coal into a pyrolysis reactor from the top, and pyrolyzing to obtain hot coke, flue gas and pyrolysis gas; the particle size of the pulverized coal is preferably less than 10 mm;
B. pneumatic conveying and stokehole separation: conveying the hot coke to a cyclone separator in front of a furnace by using a pneumatic conveying device for gas-solid separation, conveying the obtained flue gas and fine coke powder to a dilute phase region of a fluidized bed, and allowing the coarse coke powder to flow into a dense phase region of the fluidized bed through an inclined pipe; the ratio of the conveying capacity of the flue gas and the fine coke powder entering the dilute phase zone to the conveying capacity of the coarse coke powder entering the dense phase zone is preferably 1: 5-10;
C. fluidizing and gas making: in the fluidized bed, the coarse coke powder is partially combusted in the dense-phase zone and then enters the dilute-phase zone by utilizing the combustion supporting and fluidization of primary air, and then the coarse coke powder and the flue gas and the fine coke powder in the dilute-phase zone are further combusted by utilizing the combustion supporting of secondary air to obtain coke powder flue gas;
D. and (3) recovering crude coke: and the coke powder flue gas enters a cyclone separator behind the furnace for separation, the obtained coke particles which are not burnt out enter the dense phase zone again through a feed back inlet, and the obtained fuel gas is discharged from a fuel gas outlet.
Further, the method also comprises the step of enabling the pyrolysis gas obtained in the step A to sequentially pass through a purification device and a spraying device to obtain purified gas and coal tar; preferably, a portion of the coal tar is delivered to the fluidized bed as a gas making fuel.
Specifically, the method further comprises: and D, conveying the fuel gas obtained in the step D to the pyrolysis reactor as pyrolysis fuel.
Further, the method further comprises: and B, drying the pulverized coal by using the flue gas obtained in the step A.
The technical scheme of the invention has the main advantages that:
(1) the sealing problem and the safety problem of semicoke sealing are solved by utilizing pneumatic transmission; in the pneumatic conveying process, the related semicoke conveying pipelines are statically sealed, the leakage problem of pyrolysis gas in the conveying process is avoided, and meanwhile, the conveying safety can be ensured by using inert gas for conveying.
(2) The cyclone separator in front of the furnace solves the problem of interference of conveying gas on the combustion of the fluidized bed; the semicoke of pneumatic transmission gets into the cyclone before the fluidized bed furnace at first, through cyclone, coarse grain semicoke and conveying gas separation, and the coarse grain semicoke gets into dense phase district through blanking pipe (pipe chute), has guaranteed stable feed on the one hand, and on the other hand, the conveying gas of avoiding is to the interference in dilute phase district, and conveying gas and fine particle coke powder are through getting into upper portion combustor along with the overgrate air, and the burning effect of coke powder along with the overgrate air burning, assurance.
(3) The temperature of the semicoke is reduced by utilizing the flue gas air of the pyrolysis furnace, and the safety of the system is ensured by controlling the solid-gas ratio;
(4) the low-grade gas generated by the fluidized bed gas making furnace is used as fuel gas of the pyrolysis reactor, so that the comprehensive utilization rate of energy is improved.
Additional aspects and advantages of the invention will be set forth in part in the description which follows and, in part, will be obvious from the description, or may be learned by practice of the invention.
Drawings
FIG. 1 is a schematic view of the conveying process of a high-temperature semicoke buried scraper of the invention;
FIG. 2 is a schematic diagram of a system for coupling coal pyrolysis and fluidized gas production according to the present invention.
Detailed Description
The following detailed description of the present invention, taken in conjunction with the accompanying drawings and examples, is provided to enable the invention and its various aspects and advantages to be better understood. However, the specific embodiments and examples described below are for illustrative purposes only and are not limiting of the invention.
The invention provides a system for coupling coal pyrolysis and fluidized gas production, as shown in figure 2, which is characterized by comprising a pyrolysis reaction 1, a pneumatic conveying device 2, a stokehole cyclone separator 3 and a fluidized bed gas production furnace 4; wherein,
the pyrolysis reactor 1 comprises a fuel gas inlet 11, a pyrolysis gas outlet 12, a flue gas outlet 13, a multi-tube bundle distributor 14 arranged at the top and a hot coke outlet 15 arranged at the bottom;
the pneumatic conveying device 2 comprises a pressurized flue gas inlet 21 and a hot coke conveying pipeline 22; one end of the hot coke conveying pipeline 22 is connected with the pressurized flue gas inlet 21 and the hot coke outlet 15, and the other end of the hot coke conveying pipeline is connected with the stokehole cyclone separator 3; further, the pressurized flue gas inlet 21 is connected with a flue gas pressurizing device (not shown);
the stokehole cyclone separator 3 comprises a gas phase outlet 31 arranged at the top and a solid phase outlet 32 arranged at the bottom;
the fluidized-bed gas-making furnace 4 includes a fluidized bed 41 and a post-furnace cyclone 42, wherein,
the fluidized bed 41 is divided into a dilute phase zone 411 and a dense phase zone 412; the dilute phase zone 411 is provided with a gas phase inlet 4111, a secondary air inlet (not shown) and a coke powder flue gas outlet 4112, the secondary air inlet is preferably higher than the gas phase inlet 4111, and the gas phase inlet 4111 is connected with the gas phase outlet 31; the dense phase zone 412 is provided with a solid phase inlet 4121 (fluidization port), a pulverized coal inlet 4122, a primary air inlet (not shown) at the bottom, a return material inlet 4123 and a burner 4124, wherein the solid phase inlet 4121 and the solid phase outlet 32 are preferably connected through an inclined pipe 5;
furthermore, the part of the height of the lower third of the fluidized bed 41 (the part from the fluidization port to the one third of the height of the combustion chamber of the fluidized bed boiler) is the dense phase zone 412, which is mainly the combustion and fluidization of the granular coal, and is anaerobic low temperature combustion, after the granular coal is combusted to a certain extent, because of the weight reduction, part of the raw coal (semi-coke) particles are pulverized during the combustion process, and the related small particles and part of pulverized coal enter the upper dilute phase combustion zone along with the gas flow; the upper two-thirds height part (from one-third height of the boiler combustion chamber to the coke powder smoke outlet) is the dilute phase zone 411, and the combustion property is high-temperature peroxide combustion.
The cyclone separator 42 comprises a coke powder flue gas inlet 421, a return material outlet 422, a burnt dust outlet 423 and a fuel gas outlet 424, wherein the coke powder flue gas inlet 421 is connected with the coke powder flue gas outlet 4112, and the return material outlet 422 is connected with the return material inlet 4123; further, the burnt dust outlet 423 is connected with a heat exchange device.
Preferably, the elevation of the stokehold cyclone 3 is between the overfire air inlet and the dense phase zone 412.
Further, the system also comprises a purification device 6 and a spraying device 7 which are connected with each other; purification device 6 includes pyrolysis gas entry 61, spray set 7 includes purification gas export 71 and coal tar export, pyrolysis gas entry 61 with pyrolysis gas export 12 links to each other.
Specifically, the coal tar outlet is divided into a first coal tar outlet 72 and a second coal tar outlet 73; wherein the second coal tar outlet 722 is connected with the burner 4124 of the fluidized bed 41.
Further, the pyrolysis reactor 1 includes radiant tube heaters 16, and a plurality of the radiant tube heaters 16 are arranged in heating zones within the pyrolysis reactor from top to bottom;
the pyrolysis gas outlet 12, the flue gas outlet 13 and the fuel gas inlet 11 are all provided with a plurality of inlets and arranged on the side wall of the pyrolysis reactor 1 from top to bottom.
Preferably, the fuel gas inlet 11 is connected to the fuel gas outlet 424.
Further, the system comprises a screw conveyor 8, a drying lifting pipe 9 and a hopper 10; wherein,
the spiral conveyor 8 is connected with the multi-tube bundle distributor 14;
the lower part of the drying lifting pipe 9 is provided with a coal powder feeding hole 91 and a drying gas inlet 92, and the upper part is provided with a coal powder discharging hole 93;
the hopper 10 is connected with the pulverized coal discharge port 93, and the lower part of the hopper 10 is connected with the screw conveyor 8.
Preferably, the drying gas inlet 92 is connected to the flue gas outlet 13.
The invention also provides a method for coupling coal pyrolysis and fluidization gas production, which is characterized by comprising the following steps:
A. coal pyrolysis: coal powder is dried in a drying lifting pipe and then is added into a pyrolysis reactor from the top to be pyrolyzed, so that hot coke, flue gas (at the temperature of 150-; the particle size of the pulverized coal is preferably less than 10 mm;
B. pneumatic conveying and stokehole separation: in a pneumatic conveying device, the hot coke is conveyed to a cyclone separator in front of a furnace for gas-solid separation under the action of compressed air of a U-shaped valve, the obtained flue gas and fine coke powder are conveyed to a dilute phase region of a fluidized bed, and coarse coke powder flows into a dense phase region of the fluidized bed through an inclined pipe; the ratio of the conveying capacity of the flue gas and the fine coke powder entering the dilute phase zone to the conveying capacity of the coarse coke powder entering the dense phase zone is preferably 1: 5-10; the cyclone separator can separate the air conveying and semicoke particles, reduces the interference of the air conveying to the fluidized bed, and simultaneously, the cyclone separator also serves as buffering to ensure that the semicoke particles enter the fluidized bed gas making furnace more uniformly and stably;
C. fluidizing and gas making: in the fluidized bed, the coarse coke powder is partially combusted in the dense-phase zone and then enters the dilute-phase zone by utilizing the combustion supporting and fluidization of primary air, and then the coarse coke powder and the flue gas and the fine coke powder in the dilute-phase zone are further combusted by utilizing the combustion supporting of secondary air to obtain coke powder flue gas;
D. and (3) recovering crude coke: and the coke powder flue gas enters a cyclone separator behind the furnace for separation, the obtained coke particles which are not burnt out enter the dense phase zone again through a feed back inlet, and the obtained fuel gas is discharged from a fuel gas outlet.
The pyrolysis gas obtained in the step A sequentially passes through a purification device to remove fine dust carried in pyrolysis steam, and then enters a spraying device to obtain purified gas and coal tar, wherein the purified gas enters a chemical system to serve as a chemical raw material; preferably, a portion of the coal tar is delivered to the fluidized bed as a gas making fuel.
Specifically, the method further comprises: and D, conveying the fuel gas obtained in the step D to the pyrolysis reactor as pyrolysis fuel.
Further, the method further comprises: and B, drying the coal powder by using the flue gas obtained in the step A, and drying and lifting the coal powder to a hopper. The pulverized coal in the hopper is distributed by a multi-tube bundle distributor at the top of the pyrolysis reactor, uniformly enters the pyrolysis reactor, falls freely, and is heated and pyrolyzed by a plurality of layers of radiant tubes of the reactor.
The coal pyrolysis and fluidized gas production coupled process of the present invention will be described in further detail with reference to specific examples, but the embodiments of the present invention are not limited thereto, and may be performed with reference to conventional techniques for process parameters not particularly noted.
Example 1
The system of the invention is used for coal dust high-temperature pyrolysis and fluidization gas production, wherein the production capacity of the high-temperature semicoke of the pyrolysis furnace is 5t/h, and other process operation parameters are shown in tables 1-3.
Alternative pneumatic transport parameters are shown in table 1.
Table 1: pneumatic transport parameters
Table 2: high temperature semicoke characteristics after pyrolysis
Table 3: particle size distribution of high-temperature semicoke after pyrolysis
| Particle size (mm) | 0～0.074 | 0.074～1 | 1～2 | 2～3 | 3～10 |
| Weight ratio (%) | 5～15 | 5～40 | 5～10 | 5～20 | 5～20 |
When the conveying parameter of number 4 in Table 1 is selected, after cyclone separation, the obtained flue gas and fine coke powder (about 4.5T/H) are conveyed to the dense phase zone of the fluidized bed, and the coarse coke powder (about 0.5T/H) flows into the dilute phase zone of the fluidized bed by gravity through an inclined tube. By using the scheme, the transportation of the high-temperature semicoke is safer, the cyclone separator in front of the furnace solves the problem of interference of the transported gas on the combustion of the fluidized bed, the safety and the stability of the fluidized bed gas making furnace are protected, and the service life of the fluidized bed is prolonged.
Finally, it should be noted that: it should be understood that the above examples are only for clearly illustrating the present invention and are not intended to limit the embodiments. Other variations and modifications will be apparent to persons skilled in the art in light of the above description. And are neither required nor exhaustive of all embodiments. And obvious variations or modifications of the invention may be made without departing from the scope of the invention.
Claims (10)
1. A system for coupling coal pyrolysis and fluidization gas making is characterized by comprising a pyrolysis reactor, a pneumatic conveying device, a furnace-front cyclone separator and a fluidized bed gas making furnace; wherein,
the pyrolysis reactor comprises a fuel gas inlet, a pyrolysis gas outlet, a flue gas outlet, a multi-tube-bundle distributor arranged at the top and a hot coke outlet at the bottom;
the pneumatic conveying device comprises a pressurized flue gas inlet and a hot coke conveying pipeline; one end of the hot coke conveying pipeline is connected with the pressurized flue gas inlet and the hot coke outlet, and the other end of the hot coke conveying pipeline is connected with the stokehole cyclone separator;
the stokehole cyclone separator comprises a gas phase outlet arranged at the top and a solid phase outlet arranged at the bottom;
the fluidized bed gas making furnace comprises a fluidized bed and a cyclone separator arranged at the rear of the furnace,
the fluidized bed is divided into a dilute phase area and a dense phase area; the dilute phase zone is provided with a gas phase inlet, a secondary air inlet and a coke powder flue gas outlet, and the gas phase inlet is connected with the gas phase outlet; the dense-phase area is provided with a solid phase inlet, a pulverized coal inlet, a primary air inlet, a feed back inlet and a burner, and the solid phase inlet is connected with the solid phase outlet through an inclined pipe;
the cyclone separator behind the furnace comprises a coke powder flue gas inlet, a feed back outlet, a burnt dust outlet and a fuel gas outlet, wherein the coke powder flue gas inlet is connected with the coke powder flue gas outlet, and the feed back outlet is connected with the feed back inlet.
2. The system of claim 1, wherein the stokehole cyclone is located at a height position between the overfire air inlet and the dense phase zone.
3. The system of claim 1, further comprising a purification device and a spray device connected to each other; purifier includes the pyrolysis gas entry, spray set includes purification gas export and coal tar export, the pyrolysis gas entry with the pyrolysis gas export links to each other.
4. The system of claim 3, wherein the coal tar outlet is divided into a first coal tar outlet and a second coal tar outlet; wherein the second coal tar outlet is connected with a burner of the fluidized bed.
5. The system of claim 1, wherein the pyrolysis reactor comprises radiant tube heaters arranged from top to bottom in heating zones within the pyrolysis reactor;
the pyrolysis gas outlet, the flue gas outlet and the fuel gas inlet are all provided with a plurality of gas inlets and are arranged on the side wall of the pyrolysis reactor from top to bottom.
6. The system of claim 1, comprising a screw conveyor, a drying riser, and a hopper; wherein,
the spiral conveyor is connected with the multi-tube bundle distributor;
the lower part of the drying lifting pipe is provided with a coal powder feeding hole and a drying gas inlet, and the upper part of the drying lifting pipe is provided with a coal powder discharging hole;
the hopper is connected with the pulverized coal discharge port, and the lower part of the hopper is connected with the screw conveyer.
7. A method for coupling coal pyrolysis and fluidized gas generation using the system of any of claims 1-6, comprising:
A. coal pyrolysis: drying the pulverized coal, adding the dried pulverized coal into a pyrolysis reactor from the top, and pyrolyzing to obtain hot coke, flue gas and pyrolysis gas;
B. pneumatic conveying and stokehole separation: conveying the hot coke to a cyclone separator in front of a furnace by using a pneumatic conveying device for gas-solid separation, conveying the obtained flue gas and fine coke powder to a dilute phase region of a fluidized bed, and allowing the coarse coke powder to flow into a dense phase region of the fluidized bed through an inclined pipe;
C. fluidizing and gas making: in the fluidized bed, the coarse coke powder is partially combusted in the dense-phase zone and then enters the dilute-phase zone by utilizing the combustion supporting and fluidization of primary air, and then the coarse coke powder and the flue gas and the fine coke powder in the dilute-phase zone are further combusted by utilizing the combustion supporting of secondary air to obtain coke powder flue gas;
D. and (3) recovering crude coke: and the coke powder flue gas enters a cyclone separator behind the furnace for separation, the obtained coke particles which are not burnt out enter the dense phase zone again through a feed back inlet, and the obtained fuel gas is discharged from a fuel gas outlet.
8. The method according to claim 7, further comprising passing the pyrolysis gas obtained in step A through a purification device and a spraying device in sequence to obtain a purified gas and coal tar.
9. The method of claim 7, further comprising: and D, conveying the fuel gas obtained in the step D to the pyrolysis reactor as pyrolysis fuel.
10. The method of claim 7, further comprising: and B, drying the pulverized coal by using the flue gas obtained in the step A.
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