CN106635095A - System and method for treating pulverized coal and calcium-based raw material - Google Patents
System and method for treating pulverized coal and calcium-based raw material Download PDFInfo
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- CN106635095A CN106635095A CN201611111153.9A CN201611111153A CN106635095A CN 106635095 A CN106635095 A CN 106635095A CN 201611111153 A CN201611111153 A CN 201611111153A CN 106635095 A CN106635095 A CN 106635095A
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- 239000003245 coal Substances 0.000 title claims abstract description 81
- 238000000034 method Methods 0.000 title claims abstract description 30
- 239000002994 raw material Substances 0.000 title claims abstract description 30
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 title claims abstract description 29
- 239000011575 calcium Substances 0.000 title claims abstract description 29
- 229910052791 calcium Inorganic materials 0.000 title claims abstract description 29
- 239000007789 gas Substances 0.000 claims abstract description 134
- 238000000197 pyrolysis Methods 0.000 claims abstract description 79
- 239000005997 Calcium carbide Substances 0.000 claims abstract description 49
- CLZWAWBPWVRRGI-UHFFFAOYSA-N tert-butyl 2-[2-[2-[2-[bis[2-[(2-methylpropan-2-yl)oxy]-2-oxoethyl]amino]-5-bromophenoxy]ethoxy]-4-methyl-n-[2-[(2-methylpropan-2-yl)oxy]-2-oxoethyl]anilino]acetate Chemical compound CC1=CC=C(N(CC(=O)OC(C)(C)C)CC(=O)OC(C)(C)C)C(OCCOC=2C(=CC=C(Br)C=2)N(CC(=O)OC(C)(C)C)CC(=O)OC(C)(C)C)=C1 CLZWAWBPWVRRGI-UHFFFAOYSA-N 0.000 claims abstract description 49
- 239000011812 mixed powder Substances 0.000 claims abstract description 37
- 238000000746 purification Methods 0.000 claims abstract description 34
- 239000000571 coke Substances 0.000 claims abstract description 33
- 239000000463 material Substances 0.000 claims abstract description 22
- 238000003723 Smelting Methods 0.000 claims abstract description 20
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims abstract description 9
- 239000001301 oxygen Substances 0.000 claims abstract description 9
- 229910052760 oxygen Inorganic materials 0.000 claims abstract description 9
- 238000002309 gasification Methods 0.000 claims description 52
- 239000000843 powder Substances 0.000 claims description 42
- 238000006243 chemical reaction Methods 0.000 claims description 26
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims description 20
- 239000001257 hydrogen Substances 0.000 claims description 20
- 229910052739 hydrogen Inorganic materials 0.000 claims description 20
- 238000004523 catalytic cracking Methods 0.000 claims description 18
- 239000003034 coal gas Substances 0.000 claims description 18
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims description 18
- 239000003054 catalyst Substances 0.000 claims description 17
- 238000004321 preservation Methods 0.000 claims description 15
- 238000004519 manufacturing process Methods 0.000 claims description 12
- 239000000919 ceramic Substances 0.000 claims description 7
- 239000000428 dust Substances 0.000 claims description 5
- 239000007788 liquid Substances 0.000 claims description 3
- 238000001914 filtration Methods 0.000 claims description 2
- 239000002245 particle Substances 0.000 claims description 2
- 239000007787 solid Substances 0.000 abstract description 6
- 239000007921 spray Substances 0.000 abstract description 5
- 230000001172 regenerating effect Effects 0.000 abstract 1
- 230000003197 catalytic effect Effects 0.000 description 16
- ODINCKMPIJJUCX-UHFFFAOYSA-N Calcium oxide Chemical compound [Ca]=O ODINCKMPIJJUCX-UHFFFAOYSA-N 0.000 description 12
- 238000005984 hydrogenation reaction Methods 0.000 description 11
- 235000012255 calcium oxide Nutrition 0.000 description 6
- 239000000292 calcium oxide Substances 0.000 description 6
- 238000005265 energy consumption Methods 0.000 description 5
- 238000010438 heat treatment Methods 0.000 description 5
- 230000005484 gravity Effects 0.000 description 4
- 239000000969 carrier Substances 0.000 description 3
- 230000008878 coupling Effects 0.000 description 3
- 238000010168 coupling process Methods 0.000 description 3
- 238000005859 coupling reaction Methods 0.000 description 3
- 239000000203 mixture Substances 0.000 description 3
- 239000008188 pellet Substances 0.000 description 2
- 239000012495 reaction gas Substances 0.000 description 2
- 235000008733 Citrus aurantifolia Nutrition 0.000 description 1
- 235000019738 Limestone Nutrition 0.000 description 1
- 235000011941 Tilia x europaea Nutrition 0.000 description 1
- 230000001174 ascending effect Effects 0.000 description 1
- 239000002817 coal dust Substances 0.000 description 1
- 239000000498 cooling water Substances 0.000 description 1
- 238000005336 cracking Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005338 heat storage Methods 0.000 description 1
- 230000002779 inactivation Effects 0.000 description 1
- 239000011810 insulating material Substances 0.000 description 1
- 239000004571 lime Substances 0.000 description 1
- 239000006028 limestone Substances 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 238000005453 pelletization Methods 0.000 description 1
- 239000002893 slag Substances 0.000 description 1
- 239000000779 smoke Substances 0.000 description 1
- 239000008247 solid mixture Substances 0.000 description 1
- 239000002910 solid waste Substances 0.000 description 1
- 238000003860 storage Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 239000002351 wastewater 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
- C10B27/00—Arrangements for withdrawal of the distillation gases
-
- 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
- C10B37/00—Mechanical treatments of coal charges in the oven
-
- 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
- C10B43/00—Preventing or removing incrustations
-
- 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
-
- 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
- C10B57/18—Modifying the properties of the distillation gases in the oven
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
- C10G1/002—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal in combination with oil conversion- or refining processes
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
- C10K1/00—Purifying combustible gases containing carbon monoxide
- C10K1/02—Dust removal
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
- C10K3/00—Modifying the chemical composition of combustible gases containing carbon monoxide to produce an improved fuel, e.g. one of different calorific value, which may be free from carbon monoxide
- C10K3/02—Modifying the chemical composition of combustible gases containing carbon monoxide to produce an improved fuel, e.g. one of different calorific value, which may be free from carbon monoxide by catalytic treatment
- C10K3/023—Reducing the tar content
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
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- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Organic Chemistry (AREA)
- Materials Engineering (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Combustion & Propulsion (AREA)
- Life Sciences & Earth Sciences (AREA)
- Wood Science & Technology (AREA)
- Catalysts (AREA)
Abstract
The invention discloses a system and a method for treating pulverized coal and a calcium-based raw material. The system comprises a pyrolysis unit, a gas purification unit, a hydrogasification unit and a calcium carbide smelting unit, wherein the pyrolysis unit comprises a pulverized coal and calcium-based raw material mixed material inlet, a raw coke oven gas outlet and a high-temperature mixed powder outlet; a device used by the pyrolysis unit is a heat-free carrier regenerative downer reactor; the gas purification unit comprises a raw coke oven gas inlet and a purified coke oven gas outlet; the hydrogasification unit comprises a pulverized coal spray nozzle, a purified coke oven gas spray nozzle, a coke residue outlet and an oil gas outlet; the purified coke oven gas spray nozzle is connected with the purified coke oven gas outlet; the calcium carbide smelting unit comprises a high-temperature mixed powder inlet, an oxygen spray nozzle, a calcium carbide furnace gas outlet and a calcium carbide outlet. According to the system and the method disclosed by the invention, oil gas products and pyrolysis solids which are generated by pyrolyzing the pulverized coal and the calcium-based raw material in a fast pyrolysis furnace are effectively utilized at high temperature, and quality-divided gradient utilization of the pulverized coal is really realized while the heat efficiency of the system is improved.
Description
Technical Field
The invention belongs to the technical field of chemical industry, and particularly relates to a system and a method for treating pulverized coal and calcium-based raw materials.
Background
Coal hydro-gasification refers to a process of reacting raw coal powder with a hydrogen-containing reaction gas at high temperature and high pressure (800-1000 ℃, 3-8 MPa) to generate a methane-rich gas and a light oil product. Compared with the traditional coal gasification, the coal hydro-gasification has the characteristics of simple process, high thermal efficiency and little pollution, thereby being widely concerned and applied. However, hydrogen is expensive and finding alternative atmospheres for hydrogen has become a concern for many researchers.
The prior art reports that high-temperature active pellets can be obtained by mixing and pelletizing powdery medium-low-rank coal and powdery quicklime and then pyrolyzing the mixture by a rotating bed, and the high-temperature active pellets are directly and thermally fed into a calcium carbide furnace for calcium carbide production, so that the raw material cost can be greatly reduced, the thermal efficiency of a system can be improved, and the production energy consumption can be reduced. In the process, the pyrolysis of the coal in the rotating bed belongs to the pyrolysis without a heat carrier, and the obtained pyrolysis gas has high quality, particularly the hydrogen content is high and reaches more than 50 v%; the obtained tar basically belongs to heavy tar, and if the tar is reused, the tar must be subjected to pretreatment and then hydrofining, but the process is complex, the requirements on a catalyst and pressure are high, and the tar cannot be efficiently utilized.
Meanwhile, coal hydro-gasification refers to a process of reacting raw coal powder with a hydrogen-containing reaction gas under high temperature and high pressure conditions (800-1000 ℃, 3-8 MPa) to generate a methane-rich gas and a light oil product. Compared with the traditional coal gasification, the coal hydro-gasification has the characteristics of simple process, high thermal efficiency and little pollution, thereby being widely concerned and applied. However, hydrogen is expensive and finding alternative atmospheres for hydrogen is a concern for many researchers; meanwhile, the existing hydrogenation gasification furnace generally adopts cooling water for chilling, so that a large amount of waste water is generated.
Disclosure of Invention
The invention aims to mix coal powder and calcium-based raw materials, co-pyrolyze the mixture in a coal powder fast pyrolysis furnace, spray the raw coke oven gas generated by pyrolysis into a coal powder gasification furnace at high temperature after dedusting and tar catalytic cracking of a high-temperature catalytic purification unit, and uniformly mix the raw coke oven gas with the coal powder to generate hydro-gasification reaction; the powdery solid mixture generated by pyrolysis is directly sent into a calcium carbide reactor through a high-temperature closed conveying device, and calcium carbide is synthesized by an oxidation method, so that the quality-based graded utilization of medium-low-rank coal is realized.
In order to achieve the purpose, the invention provides a system for treating pulverized coal and calcium-based raw materials, which comprises a pyrolysis unit, a gas purification unit, a hydro-gasification unit and a calcium carbide smelting unit; wherein,
the pyrolysis unit comprises a mixed material inlet of pulverized coal and calcium-based raw materials, a raw gas outlet and a high-temperature mixed powder outlet, and is used for high-temperature pyrolysis of the pulverized coal and the calcium-based raw materials; the device used by the pyrolysis unit is a heat-carrier-free heat accumulating type descending bed, and a multilayer heat accumulating type radiant tube is arranged in the heat-carrier-free heat accumulating type descending bed;
the gas purification unit comprises a raw gas inlet and a purified gas outlet, the raw gas inlet is connected with the raw gas outlet, and the gas purification unit is used for processing the raw gas to obtain purified gas;
the hydro-gasification unit comprises a pulverized coal nozzle, a clean gas nozzle, a coke residue outlet and an oil gas outlet, the clean gas nozzle is connected with the clean gas outlet, and the clean gas is used as a hydrogen source to perform hydro-gasification reaction with coal in the hydro-gasification unit;
the calcium carbide smelting unit comprises a high-temperature mixed powder inlet, an oxygen nozzle, a calcium carbide furnace gas outlet and a calcium carbide outlet, the high-temperature mixed powder inlet is connected with the high-temperature mixed powder outlet, and the calcium carbide smelting unit is used for smelting high-temperature mixed powder generated by pyrolysis.
Specifically, the device used by the gas purification unit is a purification reactor. The device used by the hydro-gasification unit is a gasification furnace. The device used by the calcium carbide smelting unit is an entrained flow bed.
Furthermore, the number of the clean coal gas nozzles is even, and the clean coal gas nozzles are symmetrically arranged around the coal powder nozzles.
Each layer of heat accumulating type radiant tubes are parallel and uniformly distributed around the periphery of the descending bed, and each heat accumulating type radiant tube is parallel to each heat accumulating type radiant tube in the adjacent upper and lower layers of heat accumulating type radiant tubes and is distributed in a staggered mode along the height direction of the body of the descending bed.
Furthermore, the purification reactor is internally provided with a gas distributor arranged at the lowest layer, and a filter layer and a tar catalytic cracking catalyst layer which are sequentially arranged from bottom to top.
The filter layer is a ceramic filter plate and is used for removing dust in the raw coke oven gas and storing heat.
The tar catalytic cracking catalyst layer is CaO and is used for sufficiently catalyzing tar in the raw coke oven gas to obtain pyrolysis gas and light tar.
Furthermore, the system also comprises a heat-preservation conveying device, the high-temperature mixed powder inlet is connected with the high-temperature mixed powder outlet through the heat-preservation conveying device, and the high-temperature conveying device is a heat-preservation barrel or a heat-preservation chain plate.
The invention also provides a method for treating the coal powder and the calcium-based raw materials, which is characterized by comprising the following steps:
A. pyrolysis: feeding the coal powder and the calcium-based raw material into the pyrolysis unit for high-temperature pyrolysis to obtain coal pyrolysis product raw coke oven gas and high-temperature mixed powder;
B. gas purification: feeding the raw gas into the gas purification unit, and filtering and performing tar catalytic cracking to obtain purified gas;
C. hydro-gasification: in the hydro-gasification unit, the clean coal gas is used as a hydrogen source to perform hydro-gasification reaction with coal, so as to obtain methane-rich gas and light tar;
D. calcium carbide production: and smelting the high-temperature mixed powder generated by pyrolysis in the calcium carbide smelting unit to obtain liquid calcium carbide and calcium carbide furnace gas.
Further, the pyrolysis temperature of the pyrolysis unit is controlled at 550-800 ℃, and the pyrolysis time, namely the time for the material to fall from the top to the bottom of the furnace is 6-10 s.
Specifically, the temperature of the tar catalytic cracking catalyst layer is controlled at 700-900 ℃.
As a preferred embodiment, the particle sizes of the pulverized coal and the calcium-based raw material are both controlled to be less than or equal to 1 mm.
Specifically, the reaction temperature of the hydro-gasification unit is controlled to be 800-1000 ℃, and the gasification time is less than 2 s.
As a preferred embodiment, the reaction temperature of the calcium carbide smelting unit is 1800-2200 ℃.
According to the invention, through process coupling, oil gas products and pyrolysis solids generated by pyrolyzing the coal powder and the calcium-based raw materials in the fast pyrolysis furnace are effectively utilized at high temperature, so that the quality-based gradient utilization of coal is really realized while the thermal efficiency of the system is improved.
On one hand, the advantages of high quality and high hydrogen content of pyrolysis gas obtained by co-pyrolysis of coal and calcium-based raw materials in a rapid pyrolysis furnace are utilized, and the pyrolysis gas is directly used as a hydrogen source for coal hydro-gasification after high-temperature catalytic purification, so that the cost of a hydrogen source for coal powder gasification is reduced, and the sensible heat of high-temperature clean coal gas is fully utilized; on the other hand, solid powder generated by pyrolysis can be directly thermally fed into the entrained flow bed, and the calcium carbide is synthesized by adopting an oxygen thermal method, so that the energy consumption for producing the calcium carbide is reduced.
By adopting the system and the method of the invention, the following effects are achieved:
(1) the coal powder and the calcium-based raw materials are pyrolyzed by adopting the heat-carrier-free heat accumulating type downer, so that the heat utilization rate can be improved, the quality of pyrolysis gas can be improved, especially the hydrogen content in the pyrolysis gas is improved, and the pyrolysis gas is favorably used as a hydrogen source for the hydropyrolysis reaction;
(2) the running direction of the coal powder and the calcium-based raw materials in the downer is opposite to that of the raw coke oven gas, and the raw coke oven gas is contacted with the mixed material in the ascending process, so that the mixed material can be preheated, and the raw coke oven gas can be partially purified and dedusted, thereby reducing the dust content in the raw coke oven gas;
(3) raw coke oven gas generated by co-pyrolysis of coal powder and calcium-based raw materials is directly input into a high-temperature catalytic purification unit for dust removal and purification, and part of sensible heat of the raw coke oven gas is utilized to catalytically crack tar under the action of a catalyst to generate pyrolysis gas and light tar, so that the added value of products is improved, the product is sent into a hydrogenation gasification furnace at high temperature again, and the sensible heat of the raw coke oven gas is fully utilized;
(4) the tar catalytic cracking catalyst bed (CaO bed) of the high-temperature catalytic purification unit can be directly recycled after purifying the gas, and can be used as a raw material for calcium carbide production, so that the problems of high cost and solid waste caused by catalyst inactivation are avoided, and the tar attached to the tar is cracked again in the reaction process;
(5) raw coke oven gas generated by pyrolysis is directly used as a hydrogen source of the hydropyrolysis unit after being purified at high temperature, so that the cost of the hydrogen source is reduced, the preheating energy consumption of hydrogen can be reduced, and the reaction energy consumption of the hydrogenation unit is reduced;
(6) the high-temperature mixed powder produced by pyrolysis directly enters a calcium carbide production device through a closed heat-preservation conveying device, so that the sensible heat of the pyrolysis solid can be fully utilized, and the energy consumption of calcium carbide production is further reduced.
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 flow chart of the production process of the present invention;
FIG. 2 is a schematic view of a production system of 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 method for coupling coal powder pyrolysis, hydro-gasification and calcium carbide production, as shown in figure 1, comprising the following steps:
the first step is as follows: co-pyrolysis of coal dust and calcium-based raw materials: sending the mixed material of the coal powder and the calcium-based raw material into a rapid pyrolysis furnace through a belt conveyor, and carrying out high-temperature pyrolysis to obtain raw coke oven gas and high-temperature mixed powder; wherein, the fast pyrolysis furnace is a heat accumulating type heat carrier-free downer; the granularity of the coal powder and the calcium-based raw material is less than or equal to 1 mm; the pyrolysis temperature is 550-;
the second step is that: high-temperature catalytic purification of raw gas: raw gas generated by pyrolysis enters a high-temperature catalytic purification unit, is uniformly distributed in a high-temperature catalytic purifier under the action of a gas distributor, and is further filtered by a solid bed layer and subjected to tar catalytic cracking to obtain clean gas; the tar cracking catalyst is CaO; the temperature of catalytic cracking of the tar is 700-900 ℃;
the third step: coal powder hydro-gasification: the purified gas sent by the purification unit is used as a hydrogen source and is subjected to hydro-gasification reaction with the pulverized coal to obtain methane-rich gas and light tar. The reactor for hydro-gasification is a gasification furnace; the gasification temperature is 800-1000 ℃; the gasification time is less than 2 s;
the fourth step: calcium carbide production: and (3) sending the high-temperature mixed powder generated by pyrolysis of the preheating furnace into a calcium carbide reaction device through a heat-preservation closed conveying device, heating to 1800 plus 2200 ℃ in the calcium carbide reaction device, and smelting to obtain liquid calcium carbide and calcium carbide furnace gas.
The invention also provides a system for coupling coal powder pyrolysis, hydro-gasification and calcium carbide production, which is shown in figure 2:
the system described in the invention is composed of a mixed powder fast pyrolysis unit 1, a high-temperature catalytic purification unit 2, a hydro-gasification unit 3, a high-temperature heat delivery unit 4 and a calcium carbide smelting unit 5.
The device of the mixed powder fast pyrolysis unit 1 can be a heat-carrier-free heat accumulating type downer, and comprises a mixed material inlet 11 of pulverized coal and calcium-based raw materials, a raw coke oven gas outlet 12 and a high-temperature mixed powder outlet 13; the mixed material inlet of the pulverized coal and the quicklime is connected with a powerful mixer through a belt conveyer (not shown); the powerful mixer is respectively connected with storage bins (not shown) of the pulverized coal and the calcium-based raw materials through a belt conveyer.
The heat-carrier-free heat accumulating type descending bed is internally provided with a plurality of layers of heat accumulating type radiant tubes, each layer of heat accumulating type radiant tubes are parallel and uniformly distributed around the periphery of the descending bed, and each heat accumulating type radiant tube is parallel to each heat accumulating type radiant tube in the adjacent upper and lower layers of heat accumulating type radiant tubes and is distributed in a staggered mode along the height direction of the descending bed body.
The device of the high-temperature catalytic purification unit 2 can be a high-temperature catalytic reactor and is provided with a raw gas inlet 21 and a clean gas outlet 25; the raw gas inlet 21 is connected with the raw gas outlet 12 of the mixed powder fast pyrolysis unit 1; the high-temperature catalytic purification reactor is internally provided with a gas distributor 22, and a filter layer 23 and a tar catalytic cracking catalyst layer 24 which are sequentially arranged from bottom to top; the filter layer is a ceramic filter plate and aims to remove smoke dust in the raw coke oven gas and play a role in heat storage; the tar catalytic cracking catalyst layer aims to fully catalyze tar in the raw coke oven gas to obtain pyrolysis gas and light tar.
The device of the hydro-gasification unit 3 can be a gasification furnace and is provided with a coal powder nozzle 31, a clean gas nozzle 32, a coke residue outlet 33 and an oil gas outlet 34; the clean gas nozzle 32 is connected with the clean gas outlet 25 of the high-temperature catalytic purification unit 2; the number of the clean coal gas nozzles 32 is even, and the clean coal gas nozzles are symmetrically arranged around the pulverized coal nozzle 31, so that the clean coal gas and the pulverized coal can be fully mixed;
the device of the high-temperature solid conveying unit 4 is a closed heat-preserving tank or a closed heat-preserving conveying chain plate. The temperature resistant temperature of the heat insulating material is above 900 ℃.
The device of the calcium carbide smelting unit 5 can be an entrained flow bed and is provided with a high-temperature mixed powder inlet 51, an oxygen nozzle 52, a calcium carbide furnace gas outlet 53 and a calcium carbide outlet 54; the high-temperature mixed powder inlet 51 is connected with the outlet of the closed heat-preservation conveying device 4.
The invention will now be described with reference to specific examples, which are intended to be illustrative only and not to be limiting in any way.
Example 1
By utilizing the system, the powdery medium-low-rank coal powder with the granularity of less than 1mm and the lime are conveyed into the heat accumulating type downer without heat carriers by the belt conveyor. The mixed powder material runs downwards from the top inlet of the downer under the action of gravity and is pyrolyzed under the heating of a heat accumulating type radiant tube in the descending process, and the pyrolysis temperature is 700 ℃, so that raw coke oven gas and high-temperature mixed powder material are obtained; directly conveying the discharged raw gas into a high-temperature catalytic purification reactor at high temperature, uniformly distributing the discharged raw gas into the reactor through a gas distributor, sequentially passing through a ceramic filter and a tar catalytic cracking catalyst bed layer, keeping the temperature of the reactor at 800 ℃, and obtaining clean gas and light tar; then, clean coal gas enters a hydrogenation gasification furnace through a clean coal gas nozzle, is fully mixed with coal powder sprayed by a coal powder nozzle, and is subjected to hydrogenation gasification reaction at 850 ℃ to obtain methane-rich gas and light tar; high-temperature pyrolysis powder generated by pyrolysis of the mixed material in the downer is added into the entrained flow bed through closed heat-preservation conveying equipment, and reacts at high temperature generated by reaction of oxygen and part of pulverized coal, wherein calcium carbide is generated at the reaction temperature of 1850 ℃.
Example 2
This example is the same as the system used in example 1 above, but with different process conditions, as described below. Feeding the powdery medium and low-rank coal powder with the granularity of less than 1mm and the carbide slag into a heat accumulating type downward bed without heat carriers by using a belt conveyor. The mixed powder material runs downwards from the top inlet of the downer under the action of gravity, and is pyrolyzed under the heating of a heat accumulating type radiant tube in the descending process, wherein the pyrolysis temperature is 800 ℃, so that raw coke oven gas and high-temperature mixed powder material are obtained; directly conveying the discharged raw gas into a high-temperature catalytic purification reactor at high temperature, uniformly distributing the discharged raw gas into the reactor through a gas distributor, sequentially passing through a ceramic filter and a tar catalytic cracking catalyst bed layer, keeping the temperature of the reactor at 900 ℃, and obtaining clean gas and light tar; then, clean coal gas enters a hydrogenation gasification furnace through a clean coal gas nozzle, is fully mixed with coal powder sprayed by a coal powder nozzle, and is subjected to hydrogenation gasification reaction at 1000 ℃ to obtain methane-rich gas and light tar; high-temperature pyrolysis powder generated by pyrolysis of the mixed material in the downer is added into the entrained flow bed through closed heat-preservation conveying equipment, and reacts at high temperature generated by reaction of oxygen and part of coal powder, wherein calcium carbide is generated at the reaction temperature of 1800 ℃.
Example 3
This example is the same as the system used in example 1 above, but with different process conditions, as described below. Feeding the powdery medium and low-rank coal powder with the granularity of less than 1mm and the quick lime into a heat accumulating type downer without a heat carrier by a belt conveyor. The mixed powder material runs downwards from the top inlet of the downer under the action of gravity, and is pyrolyzed under the heating of a heat accumulating type radiant tube in the descending process, wherein the pyrolysis temperature is 550 ℃, so that raw coke oven gas and high-temperature mixed powder material are obtained; directly conveying the discharged raw gas into a high-temperature catalytic purification reactor at high temperature, uniformly distributing the discharged raw gas into the reactor through a gas distributor, sequentially passing through a ceramic filter and a tar catalytic cracking catalyst bed layer, keeping the temperature of the reactor at 800 ℃, and obtaining clean gas and light tar; then, clean coal gas enters a hydrogenation gasification furnace through a clean coal gas nozzle, is fully mixed with coal powder sprayed by a coal powder nozzle, and is subjected to hydrogenation gasification reaction at 800 ℃ to obtain methane-rich gas and light tar; high-temperature pyrolysis powder generated by pyrolysis of the mixed material in the downer is added into the entrained flow bed through closed heat-preservation conveying equipment, and reacts at high temperature generated by reaction of oxygen and part of coal powder, wherein calcium carbide is generated at the reaction temperature of 2100 ℃.
Example 4
This example is the same as the system used in example 1 above, but with different process conditions, as described below. Feeding the powdery medium-low-order coal powder with the granularity of less than 1mm and limestone into a heat accumulating type downer without heat carriers by a belt conveyor. The mixed powder material runs downwards from the top inlet of the downer under the action of gravity and is pyrolyzed under the heating of a heat accumulating type radiant tube in the descending process, and the pyrolysis temperature is 600 ℃, so that raw coke oven gas and high-temperature mixed powder material are obtained; directly conveying the discharged raw gas into a high-temperature catalytic purification reactor at high temperature, uniformly distributing the discharged raw gas into the reactor through a gas distributor, sequentially passing through a ceramic filter and a tar catalytic cracking catalyst bed layer, keeping the temperature of the reactor at 700 ℃, and obtaining clean gas and light tar; then, clean coal gas enters a hydrogenation gasification furnace through a clean coal gas nozzle, is fully mixed with coal powder sprayed by a coal powder nozzle, and is subjected to hydrogenation gasification reaction at 900 ℃ to obtain methane-rich gas and light tar; high-temperature pyrolysis powder generated by pyrolysis of the mixed material in the downer is added into the entrained flow bed through closed heat-preservation conveying equipment, and reacts at high temperature generated by reaction of oxygen and part of coal powder, wherein calcium carbide is generated at the reaction temperature of 2200 ℃.
Claims (10)
1. A system for treating pulverized coal and calcium-based raw materials comprises a pyrolysis unit, a gas purification unit, a hydro-gasification unit and a calcium carbide smelting unit; wherein,
the pyrolysis unit comprises a mixed material inlet of pulverized coal and calcium-based raw materials, a raw gas outlet and a high-temperature mixed powder outlet, and is used for high-temperature pyrolysis of the pulverized coal and the calcium-based raw materials; the device used by the pyrolysis unit is a heat-carrier-free heat accumulating type descending bed, and a multilayer heat accumulating type radiant tube is arranged in the heat-carrier-free heat accumulating type descending bed;
the gas purification unit comprises a raw gas inlet and a purified gas outlet, the raw gas inlet is connected with the raw gas outlet, and the gas purification unit is used for processing the raw gas to obtain purified gas;
the hydro-gasification unit comprises a pulverized coal nozzle, a clean gas nozzle, a coke residue outlet and an oil gas outlet, the clean gas nozzle is connected with the clean gas outlet, and the clean gas is used as a hydrogen source to perform hydro-gasification reaction with coal in the hydro-gasification unit;
the calcium carbide smelting unit comprises a high-temperature mixed powder inlet, an oxygen nozzle, a calcium carbide furnace gas outlet and a calcium carbide outlet, the high-temperature mixed powder inlet is connected with the high-temperature mixed powder outlet, and the calcium carbide smelting unit is used for smelting high-temperature mixed powder generated by pyrolysis.
2. The system of claim 1,
the device used by the gas purification unit is a purification reactor;
the device used by the hydro-gasification unit is a gasification furnace;
the device used by the calcium carbide smelting unit is an entrained flow bed.
3. The system according to claim 1 or 2,
the number of the clean coal gas nozzles is even, and the clean coal gas nozzles are symmetrically arranged around the pulverized coal nozzle;
each layer of heat accumulating type radiant tubes are parallel and uniformly distributed around the periphery of the descending bed, and each heat accumulating type radiant tube is parallel to each heat accumulating type radiant tube in the adjacent upper and lower layers of heat accumulating type radiant tubes and is distributed in a staggered mode along the height direction of the body of the descending bed.
4. The system of claim 2,
the purification reactor is internally provided with a gas distributor arranged at the lowest layer, and a filter layer and a tar catalytic cracking catalyst layer which are sequentially arranged from bottom to top;
the filter layer is a ceramic filter plate and is used for removing dust in the raw gas and storing heat;
the tar catalytic cracking catalyst layer is CaO and is used for sufficiently catalyzing tar in the raw coke oven gas to obtain pyrolysis gas and light tar.
5. The system of claim 1,
the system also comprises a heat-preservation conveying device, the high-temperature mixed powder inlet is connected with the high-temperature mixed powder outlet through the heat-preservation conveying device, and the high-temperature conveying device is a heat-preservation barrel or a heat-preservation chain plate.
6. A method for treating coal fines and calcium based feedstock using the system of any one of claims 1-5, comprising the steps of:
A. pyrolysis: feeding the coal powder and the calcium-based raw material into the pyrolysis unit for high-temperature pyrolysis to obtain coal pyrolysis product raw coke oven gas and high-temperature mixed powder;
B. gas purification: feeding the raw gas into the gas purification unit, and filtering and performing tar catalytic cracking to obtain purified gas;
C. hydro-gasification: in the hydro-gasification unit, the clean coal gas is used as a hydrogen source to perform hydro-gasification reaction with coal, so as to obtain methane-rich gas and light tar;
D. calcium carbide production: and smelting the high-temperature mixed powder generated by pyrolysis in the calcium carbide smelting unit to obtain liquid calcium carbide and calcium carbide furnace gas.
7. The method as claimed in claim 6, wherein the pyrolysis temperature of the pyrolysis unit is controlled to be 550-800 ℃, and the pyrolysis time, i.e. the time for the material to fall from the top to the bottom of the furnace, is 6-10 s.
8. The method as claimed in claim 6, wherein the temperature of the tar catalytic cracking catalyst layer is controlled to 700-900 ℃.
9. The method according to claim 6, wherein the particle sizes of both the pulverized coal and the calcium-based raw material are controlled to be 1mm or less.
10. The method as claimed in claim 6, wherein the reaction temperature of the hydro-gasification unit is controlled to be 800-.
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN103708455A (en) * | 2013-12-25 | 2014-04-09 | 北京神雾环境能源科技集团股份有限公司 | Method for preparing calcium carbide |
| CN104498107A (en) * | 2014-12-23 | 2015-04-08 | 东北大学 | Device and method for processing tar in coke oven crude gas |
| CN105925287A (en) * | 2016-06-16 | 2016-09-07 | 北京神雾环境能源科技集团股份有限公司 | Quick coal pyrolysis reactor |
| CN106006554A (en) * | 2016-07-25 | 2016-10-12 | 神雾环保技术股份有限公司 | System and method for preparing hydrogen-rich gas and calcium carbide by calcium carbide residue |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN103708455A (en) * | 2013-12-25 | 2014-04-09 | 北京神雾环境能源科技集团股份有限公司 | Method for preparing calcium carbide |
| CN104498107A (en) * | 2014-12-23 | 2015-04-08 | 东北大学 | Device and method for processing tar in coke oven crude gas |
| CN105925287A (en) * | 2016-06-16 | 2016-09-07 | 北京神雾环境能源科技集团股份有限公司 | Quick coal pyrolysis reactor |
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