CN106479547A - The system and method that a kind of coal is classified dual treatment - Google Patents
The system and method that a kind of coal is classified dual treatment Download PDFInfo
- Publication number
- CN106479547A CN106479547A CN201611111577.5A CN201611111577A CN106479547A CN 106479547 A CN106479547 A CN 106479547A CN 201611111577 A CN201611111577 A CN 201611111577A CN 106479547 A CN106479547 A CN 106479547A
- Authority
- CN
- China
- Prior art keywords
- gas
- coal
- calcium
- pyrolysis
- outlet
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
- 239000003245 coal Substances 0.000 title claims abstract description 132
- 238000000034 method Methods 0.000 title claims abstract description 22
- 230000009977 dual effect Effects 0.000 title abstract 2
- 239000007789 gas Substances 0.000 claims abstract description 130
- 238000000197 pyrolysis Methods 0.000 claims abstract description 95
- 238000002309 gasification Methods 0.000 claims abstract description 72
- 239000002994 raw material Substances 0.000 claims abstract description 58
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 claims abstract description 56
- 239000011575 calcium Substances 0.000 claims abstract description 56
- 229910052791 calcium Inorganic materials 0.000 claims abstract description 56
- 239000005997 Calcium carbide Substances 0.000 claims abstract description 53
- 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 53
- 239000007787 solid Substances 0.000 claims abstract description 45
- 238000000926 separation method Methods 0.000 claims abstract description 30
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims abstract description 21
- 239000001257 hydrogen Substances 0.000 claims abstract description 21
- 229910052739 hydrogen Inorganic materials 0.000 claims abstract description 21
- 239000000571 coke Substances 0.000 claims abstract description 19
- 239000003034 coal gas Substances 0.000 claims abstract description 16
- 239000000498 cooling water Substances 0.000 claims abstract description 15
- 239000011269 tar Substances 0.000 claims description 72
- 239000008188 pellet Substances 0.000 claims description 51
- 239000000843 powder Substances 0.000 claims description 51
- 238000006243 chemical reaction Methods 0.000 claims description 35
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims description 32
- 238000000746 purification Methods 0.000 claims description 27
- 238000003723 Smelting Methods 0.000 claims description 26
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 17
- 239000011230 binding agent Substances 0.000 claims description 14
- 238000004519 manufacturing process Methods 0.000 claims description 12
- 238000005507 spraying Methods 0.000 claims description 12
- 239000003795 chemical substances by application Substances 0.000 claims description 11
- 239000000463 material Substances 0.000 claims description 10
- 238000004321 preservation Methods 0.000 claims description 10
- 238000001816 cooling Methods 0.000 claims description 8
- 238000002156 mixing Methods 0.000 claims description 8
- 239000007788 liquid Substances 0.000 claims description 6
- 238000012216 screening Methods 0.000 claims description 6
- 239000002641 tar oil Substances 0.000 claims description 6
- 238000000748 compression moulding Methods 0.000 claims description 5
- 230000015572 biosynthetic process Effects 0.000 claims description 3
- 239000002826 coolant Substances 0.000 claims description 3
- 238000005336 cracking Methods 0.000 claims description 3
- 239000002245 particle Substances 0.000 claims description 3
- 238000003786 synthesis reaction Methods 0.000 claims description 3
- 238000005984 hydrogenation reaction Methods 0.000 abstract description 12
- 238000005453 pelletization Methods 0.000 abstract description 5
- 241001417490 Sillaginidae Species 0.000 abstract 1
- 241001062472 Stokellia anisodon Species 0.000 abstract 1
- 239000003818 cinder Substances 0.000 abstract 1
- 239000002817 coal dust Substances 0.000 abstract 1
- ODINCKMPIJJUCX-UHFFFAOYSA-N Calcium oxide Chemical compound [Ca]=O ODINCKMPIJJUCX-UHFFFAOYSA-N 0.000 description 12
- 239000000047 product Substances 0.000 description 8
- 239000002893 slag Substances 0.000 description 7
- 235000008733 Citrus aurantifolia Nutrition 0.000 description 6
- 235000019738 Limestone Nutrition 0.000 description 6
- 235000011941 Tilia x europaea Nutrition 0.000 description 6
- 239000000292 calcium oxide Substances 0.000 description 6
- 235000012255 calcium oxide Nutrition 0.000 description 6
- 239000004571 lime Substances 0.000 description 6
- 239000006028 limestone Substances 0.000 description 6
- 238000004517 catalytic hydrocracking Methods 0.000 description 5
- 239000000428 dust Substances 0.000 description 5
- 239000007921 spray Substances 0.000 description 5
- 238000007599 discharging Methods 0.000 description 4
- 238000001754 furnace pyrolysis Methods 0.000 description 4
- 238000000465 moulding Methods 0.000 description 4
- 238000005265 energy consumption Methods 0.000 description 3
- 239000007795 chemical reaction product Substances 0.000 description 2
- 238000010438 heat treatment Methods 0.000 description 2
- 238000003825 pressing Methods 0.000 description 2
- 239000002351 wastewater Substances 0.000 description 2
- 239000003054 catalyst Substances 0.000 description 1
- 230000003197 catalytic effect Effects 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 230000002349 favourable effect Effects 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 239000003921 oil Substances 0.000 description 1
- 238000007781 pre-processing Methods 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 238000010791 quenching Methods 0.000 description 1
- 239000012495 reaction gas Substances 0.000 description 1
- 230000001172 regenerating effect Effects 0.000 description 1
- 239000012265 solid product Substances 0.000 description 1
- 239000000126 substance 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
- 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
- C10G1/06—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal by destructive hydrogenation
Landscapes
- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Organic Chemistry (AREA)
- Life Sciences & Earth Sciences (AREA)
- Wood Science & Technology (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Materials Engineering (AREA)
- Carbon And Carbon Compounds (AREA)
Abstract
The invention discloses the system and method that a kind of coal is classified dual treatment.The system includes that pyrolysis unit, Oil-gas Separation clean unit, hydrogasification unit and calcium carbide smelt unit；Pyrolysis unit includes coal dust with calcium based raw material mixed type ball entrance, raw coke oven gas outlet and the pelletizing outlet of pyrolysis solid；Oil-gas Separation clean unit is provided with raw coke oven gas entrance, circulating cooling water inlet, circulating cooling water out, light oil outlet, purified gas outlet and heavy tar outlet；Hydrogasification unit includes coal nozzle, clean coal gas jets, tar nozzle, cinder outlet and oil gas vent, and tar nozzle is connected with heavy tar outlet；Calcium carbide smelts unit includes high-temp solid pelletizing entrance, calcium carbide furnace gas outlet and calcium carbide outlet, and high-temp solid pelletizing entrance is connected with the pelletizing outlet of pyrolysis solid.The present invention reduces the cost of hydrogen source, it is achieved that the efficient utilization of pyrolysis product using coal with calcium based raw material pyrolysis gained pyrolysis gas as the hydrogen source of coal hydrogenation gasification.
Description
Technical Field
The invention belongs to the technical field of chemical industry, and particularly relates to a system and a method for coal grading and quality grading treatment.
Background
Coal pyrolysis is a process of heating coal at a certain temperature and in an anaerobic environment so as to decompose volatile matters in the coal and generate pyrolysis solid, pyrolysis gas and tar, and is a key step for realizing quality-based gradient utilization of the coal. 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 couple coal and calcium-based raw material mixed pellet pyrolysis with coal hydro-gasification and calcium carbide production processes, wherein pyrolysis gas generated by mixed pellet pyrolysis is used as a hydrogen source of coal hydro-gasification, pyrolysis tar is used as a chilling agent of coal hydro-gasification, and secondary cracking is carried out to obtain light tar while cooling gasification synthesis gas; the pyrolysis solid is directly heated at high temperature and is sent to a calcium carbide furnace to generate calcium carbide, so that oil, gas and solid products generated by pyrolysis of medium and low-rank coal are efficiently utilized, the system efficiency is improved, and the quality-based graded utilization of the medium and low-rank coal is realized.
In order to achieve the purpose, the invention provides a system for coal grading and quality-grading treatment, which comprises a pyrolysis unit, an oil-gas separation and purification unit, a hydro-gasification unit and a calcium carbide smelting unit; wherein,
the pyrolysis unit comprises a pulverized coal and calcium-based raw material mixed ball inlet, a raw coke oven gas outlet and a pyrolysis solid pellet outlet, and is used for high-temperature pyrolysis of the pulverized coal and calcium-based raw material mixed ball;
the oil-gas separation and purification unit is provided with a raw gas inlet, a circulating cooling water outlet, a light oil outlet, a clean gas outlet and a heavy tar oil outlet, the raw gas inlet is connected with the raw gas outlet, and the oil-gas separation and purification unit is used for treating the raw gas to obtain clean gas, heavy tar oil and light tar oil;
the hydro-gasification unit comprises a coal powder nozzle, a clean gas nozzle, a tar nozzle, a coke residue outlet and an oil gas outlet, wherein the clean gas nozzle is connected with the clean gas outlet, and the tar nozzle is connected with the heavy tar outlet; in the hydro-gasification unit, the heavy tar is used as a coolant, and the clean coal gas is used as a hydrogen source to perform hydro-gasification reaction with coal;
the calcium carbide smelting unit comprises a high-temperature solid pellet inlet, a calcium carbide furnace gas outlet and a calcium carbide outlet, the high-temperature solid pellet inlet is connected with the pyrolysis solid pellet outlet, and the calcium carbide smelting unit is used for smelting high-temperature solid pellets generated by pyrolysis.
The system further comprises a coal powder and calcium-based raw material pretreatment unit, the coal powder and calcium-based raw material pretreatment unit comprises a coal powder and calcium-based raw material inlet and a coal powder and calcium-based raw material mixed ball outlet, the coal powder and calcium-based raw material mixed ball outlet and the coal powder and calcium-based raw material mixed ball inlet are connected, and the coal powder and calcium-based raw material pretreatment unit is used for treating the coal powder and calcium-based raw material to obtain the coal powder and calcium-based raw material mixed ball.
Further, the device used by the pyrolysis unit is a heat-carrier-free regenerative preheating furnace.
The heat-carrier-free heat accumulating type preheating furnace is provided with an upper heat accumulating type radiant tube layer and a lower heat accumulating type radiant tube layer which are uniformly distributed above and below the material layer in parallel, and the adjacent upper layer radiant tube and the lower layer radiant tube are distributed in a staggered mode.
The device used by the hydro-gasification unit is a gasification furnace.
The device used by the calcium carbide smelting unit is a calcium carbide furnace.
Specifically, the device used by the oil-gas separation and purification unit is a water spraying device. The water spraying device is characterized in that a plurality of nozzles are arranged on a cooling water inlet pipe in the water spraying device, the nozzles are arranged in a staggered mode, a baffle is arranged in the vertical direction of the cooling water inlet pipe, and the lower end of the baffle is located below the purified gas outlet.
Preferably, the number of the clean coal gas nozzles is even, and the clean coal gas nozzles are symmetrically arranged around the pulverized coal nozzles.
Further, the system also comprises a heat-preservation conveying device, and the high-temperature solid pellet inlet is connected with the pyrolysis solid pellet outlet through the heat-preservation conveying device; the high-temperature conveying device is a heat-insulating barrel or a heat-insulating chain plate.
The invention also provides a method for carrying out classification and quality classification treatment on coal, which is characterized by comprising the following steps:
A. pyrolysis: feeding the mixed balls of the coal powder and the calcium-based raw materials into the pyrolysis unit for high-temperature pyrolysis to obtain raw coke oven gas and high-temperature solid pellets which are coal pyrolysis products;
B. oil-gas separation and purification: sending the raw coke oven gas into the oil-gas separation and purification unit for water spraying, cooling and dedusting treatment, conveying the obtained purified gas serving as a hydrogen source to the hydro-gasification unit, and spraying the heavy tar obtained after oil-water separation of the obtained liquid serving as a chilling agent into the gasification furnace;
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; the heavy tar is used as a chilling agent for coal hydro-gasification, and secondary cracking is carried out while the gasification synthesis gas is cooled;
D. calcium carbide production: and smelting the high-temperature solid pellets generated by pyrolysis in the calcium carbide smelting unit to obtain liquid calcium carbide and calcium carbide furnace gas.
Further, the method further comprises preprocessing: and crushing and screening the pulverized coal and the calcium-based raw material in the pulverized coal and calcium-based raw material pretreatment unit, mixing the pulverized coal and the calcium-based raw material with a binder, and performing compression molding to obtain the pulverized coal and calcium-based raw material mixed pellet.
Specifically, the pyrolysis temperature of the pyrolysis unit is controlled at 750-950 ℃. The pyrolysis time is 20-60 min.
As a preferred embodiment, the crushed particle size of the pulverized coal in the pulverized coal and calcium-based raw material mixed type pellet is controlled to be <1 mm. The crushing granularity of the calcium-based raw material is controlled to be less than 3 mm. The addition amount of the binder is 1.0-10.0 wt% of the mixed material. The mass ratio of the calcium-based raw material to the pulverized coal is 0.8-1.2: 1.
Specifically, the reaction temperature of the hydro-gasification unit is controlled to be 800-1000 ℃. The gasification time is less than 2 s.
As a preferred embodiment, the reaction temperature of the calcium carbide smelting unit is 1800-2200 ℃.
The method utilizes the advantages of high quality and high hydrogen content of pyrolysis gas obtained by co-pyrolysis of the mixed pellets of the coal and the calcium-based raw materials in the preheating furnace, and takes the pyrolysis gas as a hydrogen source for coal hydro-gasification, thereby reducing the cost of the hydrogen source; the solid pellets generated by pyrolysis can be directly and thermally fed into a calcium carbide furnace, so that the energy consumption for calcium carbide production is reduced; meanwhile, tar produced by pyrolysis is directly used as a chilling agent of the hydrogenation gasification furnace, so that heavy tar is cracked again to obtain light tar while the generation of waste water is reduced. The high-efficiency utilization of pyrolysis products is realized.
By adopting the system and the method of the invention, the following effects are achieved:
(1) the calcium-based raw material and the pulverized coal mixed pellet are used as raw materials, so that the contact area of the raw materials can be greatly increased and the reaction rate can be increased when the pyrolyzed solid pellet is subjected to calcium production; meanwhile, due to the catalytic action of the calcium-based raw material, the content of hydrogen in the pyrolysis gas can be obviously improved, and the calcium-based raw material is favorable for being used as a hydrogen source for the hydropyrolysis reaction;
(2) the calcium-based raw material and the pulverized coal mixed pellets are pyrolyzed by adopting a heat-carrier-free heat accumulating type preheating furnace, so that the heat utilization rate can be improved, and the quality of pyrolysis gas can be improved;
(3) raw coke oven gas generated by pyrolysis is purified and then used as a hydrogen source of a hydro-pyrolysis unit, so that the cost of the hydrogen source in the hydro-gasification reaction can be obviously reduced;
(4) cooling the tar generated by pyrolysis, directly spraying the cooled tar as a coolant into a hydro-gasification reaction furnace without pretreatment, reducing the temperature of a gasification reaction product, simultaneously performing a hydrocracking reaction, fully utilizing the sensible heat of the hydro-gasification reaction product, and improving the added value of the tar;
(5) the high-temperature solid pellets generated by pyrolysis are directly conveyed into the carbide furnace through the closed heat-preservation conveying device, so that the sensible heat of the pyrolyzed solids can be fully utilized, and the energy consumption of the 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 realizing graded utilization of coal according to quality, which comprises the following steps of:
the first step is as follows: and (3) pyrolyzing the mixed pellets of the coal powder and the calcium-based raw materials: conveying the mixed pellets of the coal powder and the calcium-based raw materials into a preheating furnace through a belt conveyor, and performing high-temperature pyrolysis to obtain raw coke oven gas and high-temperature solid pellets which are coal pyrolysis products; wherein, the pyrolysis reactor is a heat accumulating type preheating furnace; the pyrolysis temperature is 550-;
the preparation method of the mixed ball of the coal powder and the calcium-based raw material comprises the following steps: firstly, crushing and screening the medium-low rank coal and the calcium-based raw material, and crushing the medium-low rank coal to be less than 1 mm; crushing the calcium-based raw material to be less than 3 mm; then mixing the coal powder, the calcium-based raw material and the binder, and pressing and molding; the addition amount of the binder is 1.0-10.0 wt% of the mixed material; the adding mass ratio of the calcium-based raw material to the coal powder is 0.8-1.2: 1;
the second step is that: oil-gas separation and purification: raw gas generated by pyrolysis enters a gas purification unit, and gas subjected to water spraying, temperature reduction and dust removal is conveyed and sprayed into a hydro-gasification furnace to be mixed with coal powder for reaction; after the sprayed liquid is subjected to oil-water separation, the heavy tar is sprayed into the gasification furnace as a chilling agent, and water can be recycled;
the third step: coal 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 solid pellets generated by pyrolysis of the preheating furnace into the calcium carbide furnace through a heat-insulating closed conveying device, heating to 1800 plus 2200 ℃ in the calcium carbide furnace, and smelting to obtain liquid calcium carbide and calcium carbide furnace gas.
The invention provides a system for realizing coal quality-based gradient utilization, which is shown in a figure 2:
the calcium carbide production system described by the invention is composed of a preheating furnace pyrolysis unit 1, an oil-gas separation and purification unit 2, a coal hydrogenation gasification unit 3 and a calcium carbide smelting unit 4.
The device of the preheating furnace pyrolysis unit 1 can be a heat-carrier-free heat accumulating type preheating furnace and comprises a pulverized coal and calcium-based raw material mixed ball inlet 11, a crude gas outlet 12 and a pyrolysis solid ball outlet 13; the mixed ball inlet of the pulverized coal and calcium-based raw material is connected with a ball conveyor belt; the molding ball conveying belt is connected with an outlet of the molding machine.
An upper layer of heat accumulating type radiant tubes and a lower layer of heat accumulating type radiant tubes are arranged in the preheating furnace and are distributed above and below the material layer; each layer of the heat accumulating type radiant tube comprises a plurality of heat accumulating type radiant tubes which are parallel and evenly distributed.
The device of the oil-gas separation and purification unit 2 can be a water spraying device and is provided with a raw gas inlet 21, a circulating cooling water inlet 22, a circulating cooling water outlet 23, a light oil outlet 25, a clean gas outlet 26 and a heavy tar outlet 27;
the raw gas inlet 21 is connected with the raw gas outlet 12 of the preheating furnace pyrolysis unit 1; a plurality of nozzles 24 are arranged on the cooling water inlet pipe; the direction of the nozzles is staggered to ensure that the cooling water is fully contacted with the raw coke oven gas; a baffle is arranged in the spray tower and is vertical to the cooling water inlet pipe, and the lower end of the baffle is positioned below the clean gas outlet 26, so that the cooling water is further ensured to be fully contacted with the raw coke oven gas;
the device of the coal hydro-gasification unit 3 may be a gasification furnace comprising a reaction chamber 3-1 and a quench chamber 3-2. Is provided with a coal powder nozzle 31, a clean gas nozzle 32, a tar nozzle 33, an oil gas outlet 34 and a coke residue outlet 35; the clean gas nozzle 32 is connected with the clean gas outlet 26 of the oil-gas separation and purification unit 2; the tar nozzle 33 is connected with the heavy tar outlet 27 of the oil-gas separation and 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 number of the tar nozzles 33 is even, and the tar nozzles are symmetrically arranged around the gasification furnace;
the device of the calcium carbide smelting unit 4 can be a closed calcium carbide furnace, and is provided with a high-temperature solid pellet inlet 41, a calcium carbide furnace gas outlet 42 and a calcium carbide outlet 43; the high-temperature solid pellet inlet 41 is connected with a pyrolysis pellet outlet 13 of the preheating furnace pyrolysis unit 1 through a heat preservation conveying device; the high-temperature conveying device can be one of a heat-insulating barrel or a heat-insulating chain plate.
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 medium and low-rank coal and limestone are crushed and sieved to be less than 1 mm; limestone is crushed to <2 mm; then mixing the coal powder, limestone and a binder, and pressing and molding to obtain a coal powder and limestone mixed ball; wherein the addition amount of the binder is 1.0 wt% of the mixed material, and the addition mass ratio of the limestone to the coal powder is 0.8: 1.
And then conveying the pulverized coal and limestone mixed balls into a pyrolysis unit of a preheating furnace by using a belt conveyor. Pyrolyzing the mixed pellets in a preheating furnace at 950 ℃ for 30min to obtain raw coke oven gas and high-temperature solid pellets; the discharged raw gas is subjected to dust removal, purification and separation in a water spray tower to obtain clean gas, light tar and heavy tar; wherein, the purified coal gas is sprayed into the hydrogenation gasification furnace through a nozzle, is fully mixed with the coal powder sprayed by the coal powder nozzle, and is subjected to hydrogenation gasification reaction at 1000 ℃ to obtain methane-rich gas and light tar, and the methane-rich gas and the light tar are further utilized after purification and separation; the heavy tar is sprayed into the gasification furnace through a nozzle to serve as a chilling agent for the hydro-gasification reaction, the methane-rich gas and the semicoke generated by the reaction are cooled, the temperature after cooling is about 500 ℃ and 650 ℃, meanwhile, the heavy tar is subjected to a hydrocracking reaction to generate pyrolysis gas and light tar, and the pyrolysis gas and the light tar are mixed with an oil gas product of the hydro-pyrolysis reaction; directly purifying and storing the light tar after being output; and (3) sending the high-temperature solid pellets obtained by the pyrolysis unit of the preheating furnace into a calcium carbide smelting device through closed heat-preservation conveying equipment (the heat sending temperature is the pyrolysis solid discharging temperature), and smelting at 2200 ℃ to obtain calcium carbide.
Example 2
This example is the same as the system used in example 1 above, but with different process conditions, as described below. Crushing and screening the medium and low rank coal and quicklime, and crushing the medium and low rank coal to be less than 1 mm; crushing the carbide slag to be less than 3 mm; then mixing the coal powder, the quicklime and the binder, and performing compression molding to obtain a coal powder and quicklime mixed ball; wherein the addition amount of the binder is 10.0 wt% of the mixed material, and the addition mass ratio of the quicklime to the coal powder is 1.2: 1.
And then conveying the mixed balls of the pulverized coal and the quicklime into a pyrolysis unit of a preheating furnace by using a belt conveyor. Pyrolyzing the mixed pellets in a preheating furnace at 750 ℃ for 60min to obtain raw coke oven gas and high-temperature solid pellets; the discharged raw gas is subjected to dust removal, purification and separation in a water spray tower to obtain clean gas, light tar and heavy tar; wherein, the clean coal gas is sprayed into the hydrogenation gasification furnace through a nozzle, is fully mixed with the coal powder sprayed by the coal powder nozzle, and is subjected to hydrogenation gasification reaction at 900 ℃ to obtain methane-rich gas and light tar, and the methane-rich gas and the light tar are further utilized after purification and separation; the heavy tar is sprayed into the gasification furnace through a nozzle to serve as a chilling agent for the hydro-gasification reaction, the methane-rich gas and the semicoke generated by the reaction are cooled, the temperature after cooling is about 500 ℃ and 650 ℃, meanwhile, the heavy tar is subjected to a hydrocracking reaction to generate pyrolysis gas and light tar, and the pyrolysis gas and the light tar are mixed with an oil gas product of the hydro-pyrolysis reaction; directly purifying and storing the light tar after being output; and (3) sending the high-temperature solid pellets obtained by the pyrolysis unit of the preheating furnace into a calcium carbide smelting device through closed heat-preservation conveying equipment (the heat sending temperature is the pyrolysis solid discharging temperature), and smelting at 2100 ℃ to obtain the calcium carbide.
Example 3
This example is the same as the system used in example 1 above, but with different process conditions, as described below. Crushing and screening the medium and low-rank coal and the carbide slag, and crushing the medium and low-rank coal to be less than 1 mm; crushing the carbide slag to be less than 3 mm; then mixing the coal powder, the carbide slag and the binder, and performing compression molding to obtain a coal powder and carbide slag mixed ball; wherein the addition amount of the binder is 4.0 wt% of the mixed material, and the addition mass ratio of the carbide slag to the coal powder is 1: 1.
And then conveying the mixed balls of the coal powder and the carbide slag into a pyrolysis unit of a preheating furnace by using a belt conveyor. Pyrolyzing the mixed pellets in a preheating furnace at 850 ℃ for 40min to obtain raw coke oven gas and high-temperature solid pellets; the discharged raw gas is subjected to dust removal, purification and separation in a water spray tower to obtain clean gas, light tar and heavy tar; wherein, the purified coal gas is sprayed into the hydrogenation gasification furnace through a nozzle, is fully mixed with the coal powder sprayed by the coal powder nozzle, and is subjected to hydrogenation gasification reaction at 850 ℃ to obtain methane-rich gas and light tar, and the methane-rich gas and the light tar are further utilized after purification and separation; the heavy tar is sprayed into the gasification furnace through a nozzle to serve as a chilling agent for the hydro-gasification reaction, the methane-rich gas and the semicoke generated by the reaction are cooled, the temperature after cooling is about 500 ℃ and 650 ℃, meanwhile, the heavy tar is subjected to a hydrocracking reaction to generate pyrolysis gas and light tar, and the pyrolysis gas and the light tar are mixed with an oil gas product of the hydro-pyrolysis reaction; directly purifying and storing the light tar after being output; and (3) sending the high-temperature solid pellets obtained by the pyrolysis unit of the preheating furnace into a calcium carbide smelting device through closed heat-preservation conveying equipment (the heat sending temperature is the pyrolysis solid discharging temperature), and smelting at 2000 ℃ to obtain calcium carbide.
Example 4
This example is the same as the system used in example 1 above, but with different process conditions, as described below. Crushing and screening the medium and low rank coal and lime, and crushing the medium and low rank coal to be less than 1 mm; lime is crushed to be less than 3 mm; then mixing the coal powder, lime and a binder, and performing compression molding to obtain a coal powder and lime mixed ball; wherein the addition amount of the binder is 8.0 wt% of the mixed material, and the addition mass ratio of the lime to the coal powder is 1.2: 1.
And then conveying the pulverized coal and lime mixed balls into a pyrolysis unit of a preheating furnace by using a belt conveyor. Pyrolyzing the mixed pellets in a preheating furnace at 800 ℃ for 45min to obtain raw coke oven gas and high-temperature solid pellets; the discharged raw gas is subjected to dust removal, purification and separation in a water spray tower to obtain clean gas, light tar and heavy tar; wherein, the purified coal gas is sprayed into the hydrogenation gasification furnace through a nozzle, is fully mixed with the coal powder sprayed by the coal powder nozzle, and is subjected to hydrogenation gasification reaction at 800 ℃ to obtain methane-rich gas and light tar, and the methane-rich gas and the light tar are further utilized after purification and separation; the heavy tar is sprayed into the gasification furnace through a nozzle to serve as a chilling agent for the hydro-gasification reaction, the methane-rich gas and the semicoke generated by the reaction are cooled, the temperature after cooling is about 500 ℃ and 650 ℃, meanwhile, the heavy tar is subjected to a hydrocracking reaction to generate pyrolysis gas and light tar, and the pyrolysis gas and the light tar are mixed with an oil gas product of the hydro-pyrolysis reaction; directly purifying and storing the light tar after being output; and (3) sending the high-temperature solid pellets obtained by the pyrolysis unit of the preheating furnace into a calcium carbide smelting device through closed heat-preservation conveying equipment (the heat sending temperature is the pyrolysis solid discharging temperature), and smelting at 1800 ℃ to obtain the calcium carbide.
Claims (10)
1. A system for coal grading and quality-grading treatment comprises a pyrolysis unit, an oil-gas separation and purification unit, a hydro-gasification unit and a calcium carbide smelting unit; wherein,
the pyrolysis unit comprises a pulverized coal and calcium-based raw material mixed ball inlet, a raw coke oven gas outlet and a pyrolysis solid pellet outlet, and is used for high-temperature pyrolysis of the pulverized coal and calcium-based raw material mixed ball;
the oil-gas separation and purification unit is provided with a raw gas inlet, a circulating cooling water outlet, a light oil outlet, a clean gas outlet and a heavy tar oil outlet, the raw gas inlet is connected with the raw gas outlet, and the oil-gas separation and purification unit is used for treating the raw gas to obtain clean gas, heavy tar oil and light tar oil;
the hydro-gasification unit comprises a coal powder nozzle, a clean gas nozzle, a tar nozzle, a coke residue outlet and an oil gas outlet, wherein the clean gas nozzle is connected with the clean gas outlet, and the tar nozzle is connected with the heavy tar outlet; in the hydro-gasification unit, the heavy tar is used as a coolant, and the clean coal gas is used as a hydrogen source to perform hydro-gasification reaction with coal;
the calcium carbide smelting unit comprises a high-temperature solid pellet inlet, a calcium carbide furnace gas outlet and a calcium carbide outlet, the high-temperature solid pellet inlet is connected with the pyrolysis solid pellet outlet, and the calcium carbide smelting unit is used for smelting high-temperature solid pellets generated by pyrolysis.
2. The system of claim 1,
the system further comprises a coal powder and calcium-based raw material pretreatment unit, the coal powder and calcium-based raw material pretreatment unit comprises a coal powder and calcium-based raw material inlet and a coal powder and calcium-based raw material mixed ball outlet, the coal powder and calcium-based raw material mixed ball outlet is connected with the coal powder and calcium-based raw material mixed ball inlet, and the coal powder and calcium-based raw material pretreatment unit is used for treating the coal powder and calcium-based raw materials to obtain the coal powder and calcium-based raw material mixed balls.
3. The system according to claim 1 or 2,
the device used by the pyrolysis unit is a heat-carrier-free heat accumulating type preheating furnace, an upper layer of heat accumulating type radiant tubes and a lower layer of heat accumulating type radiant tubes are arranged in the heat-carrier-free heat accumulating type preheating furnace and are uniformly distributed above and below the material layer in parallel, and the adjacent upper layer radiant tubes and the lower layer radiant tubes are distributed in a staggered manner;
the device used by the hydro-gasification unit is a gasification furnace;
the device used by the calcium carbide smelting unit is a calcium carbide furnace.
4. The system of claim 3,
the device used by the oil-gas separation and purification unit is a water spraying device, a plurality of nozzles are arranged on a cooling water inlet pipe in the water spraying device, the nozzles are arranged in a staggered mode, a baffle is arranged in the vertical direction of the cooling water inlet pipe, and the lower end of the baffle is located below the purified gas outlet.
5. The system of claim 1,
the number of the clean coal gas nozzles is even, and the clean coal gas nozzles are symmetrically arranged on the periphery of the pulverized coal nozzle;
the system also comprises a heat-preservation conveying device, and the high-temperature solid pellet inlet is connected with the pyrolysis solid pellet outlet through the heat-preservation conveying device; the high-temperature conveying device is a heat-insulating barrel or a heat-insulating chain plate.
6. A method for the classification and quality-grading treatment of coal by using the system of any one of claims 1 to 5, comprising the steps of:
A. pyrolysis: feeding the mixed balls of the coal powder and the calcium-based raw materials into the pyrolysis unit for high-temperature pyrolysis to obtain raw coke oven gas and high-temperature solid pellets which are coal pyrolysis products;
B. oil-gas separation and purification: sending the raw coke oven gas into the oil-gas separation and purification unit for water spraying, cooling and dedusting treatment, conveying the obtained purified gas serving as a hydrogen source to the hydro-gasification unit, and spraying the heavy tar obtained after oil-water separation of the obtained liquid serving as a chilling agent into the gasification furnace;
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; the heavy tar is used as a chilling agent for coal hydro-gasification, and secondary cracking is carried out while the gasification synthesis gas is cooled;
D. calcium carbide production: and smelting the high-temperature solid pellets generated by pyrolysis in the calcium carbide smelting unit to obtain liquid calcium carbide and calcium carbide furnace gas.
7. The method of claim 6, further comprising,
pretreatment: and crushing and screening the pulverized coal and the calcium-based raw material in the pulverized coal and calcium-based raw material pretreatment unit, mixing the pulverized coal and the calcium-based raw material with a binder, and performing compression molding to obtain the pulverized coal and calcium-based raw material mixed pellet.
8. The method as claimed in claim 6 or 7, wherein the pyrolysis temperature of the pyrolysis unit is controlled at 750 ℃ and 950 ℃ and the pyrolysis time is 20-60 min.
9. The method according to claim 7, wherein the crushed particle size of the pulverized coal in the mixed type pellet of the pulverized coal and the calcium-based raw material is controlled to be less than 1mm, the crushed particle size of the calcium-based raw material is controlled to be less than 3mm, the addition amount of the binder is 1.0-10.0 wt% of the mixed material, and the addition mass ratio of the calcium-based raw material to the pulverized coal is 0.8-1.2: 1.
10. The method as claimed in claim 6, wherein the reaction temperature of the hydro-gasification unit is controlled to be 800-.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201611111577.5A CN106479547A (en) | 2016-12-06 | 2016-12-06 | The system and method that a kind of coal is classified dual treatment |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201611111577.5A CN106479547A (en) | 2016-12-06 | 2016-12-06 | The system and method that a kind of coal is classified dual treatment |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN106479547A true CN106479547A (en) | 2017-03-08 |
Family
ID=58275025
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201611111577.5A Pending CN106479547A (en) | 2016-12-06 | 2016-12-06 | The system and method that a kind of coal is classified dual treatment |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN106479547A (en) |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107523316A (en) * | 2017-10-17 | 2017-12-29 | 榆林煤化工产业促进中心 | A kind of hydrogen source stably decomposes complex function low temperature upgrading furnace |
| CN109850900A (en) * | 2017-11-30 | 2019-06-07 | 神雾环保技术股份有限公司 | A kind of system for producing calcium carbide |
| CN110452723A (en) * | 2019-07-25 | 2019-11-15 | 内蒙古万众炜业科技环保股份公司 | A kind of conservation of energy system of coal production |
| CN112694088A (en) * | 2021-01-21 | 2021-04-23 | 东南大学 | Device and method for preparing hydrogen storage carbon material by adopting biomass pyrolysis gas |
Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20130205727A1 (en) * | 2010-02-05 | 2013-08-15 | The Texas A&M University System | Devices and Methods for a Pyrolysis and Gasification System for Biomass Feedstock |
| CN105462618A (en) * | 2015-12-08 | 2016-04-06 | 新奥科技发展有限公司 | Hydrogasification furnace, hydrogasification system and hydrogasification method |
| CN106006555A (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 |
| CN205709884U (en) * | 2016-04-29 | 2016-11-23 | 神雾环保技术股份有限公司 | A kind of preparation system of carbide |
| CN205709883U (en) * | 2016-04-29 | 2016-11-23 | 神雾环保技术股份有限公司 | A kind of preparation system of carbide |
| CN206266493U (en) * | 2016-12-06 | 2017-06-20 | 神雾环保技术股份有限公司 | The system that a kind of coal is classified dual treatment |
-
2016
- 2016-12-06 CN CN201611111577.5A patent/CN106479547A/en active Pending
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20130205727A1 (en) * | 2010-02-05 | 2013-08-15 | The Texas A&M University System | Devices and Methods for a Pyrolysis and Gasification System for Biomass Feedstock |
| CN105462618A (en) * | 2015-12-08 | 2016-04-06 | 新奥科技发展有限公司 | Hydrogasification furnace, hydrogasification system and hydrogasification method |
| CN205709884U (en) * | 2016-04-29 | 2016-11-23 | 神雾环保技术股份有限公司 | A kind of preparation system of carbide |
| CN205709883U (en) * | 2016-04-29 | 2016-11-23 | 神雾环保技术股份有限公司 | A kind of preparation system of carbide |
| CN106006555A (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 |
| CN206266493U (en) * | 2016-12-06 | 2017-06-20 | 神雾环保技术股份有限公司 | The system that a kind of coal is classified dual treatment |
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107523316A (en) * | 2017-10-17 | 2017-12-29 | 榆林煤化工产业促进中心 | A kind of hydrogen source stably decomposes complex function low temperature upgrading furnace |
| CN109850900A (en) * | 2017-11-30 | 2019-06-07 | 神雾环保技术股份有限公司 | A kind of system for producing calcium carbide |
| CN110452723A (en) * | 2019-07-25 | 2019-11-15 | 内蒙古万众炜业科技环保股份公司 | A kind of conservation of energy system of coal production |
| CN112694088A (en) * | 2021-01-21 | 2021-04-23 | 东南大学 | Device and method for preparing hydrogen storage carbon material by adopting biomass pyrolysis gas |
| CN112694088B (en) * | 2021-01-21 | 2023-08-04 | 东南大学 | Device and method for preparing hydrogen storage carbon material by adopting biomass pyrolysis gas |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN102181315B (en) | Process for producing natural gas by coal coking and pyrolysis coal gas thereof | |
| CN106479547A (en) | The system and method that a kind of coal is classified dual treatment | |
| CN104152164B (en) | Coal gas circulation coal wholegrain radial sector pyrolytic process and system | |
| CN106479541A (en) | A kind of system and method for processing coal dust and living beings | |
| CN206266493U (en) | The system that a kind of coal is classified dual treatment | |
| CN109517612B (en) | Continuous, efficient and green waste tire superheated steam energy conversion method | |
| CN109652103B (en) | Down bed-fixed bed pyrolysis-gasification integrated method and device | |
| CN111088057A (en) | Method for producing hydrogen by using waste plastics to produce oil | |
| CN110591745B (en) | Pyrolysis-gasification integrated device and process | |
| CN104560100A (en) | Waste tire pyrolysis system and pyrolysis method | |
| CN105419879B (en) | Device and method for catalytic decomposition and high-temperature separation of coal substances | |
| CN102226112A (en) | Microwave entrained flow bed two-stage biomass gasifying technique | |
| CN111088058A (en) | Method for preparing oil from waste plastics | |
| CN106675596A (en) | System and method for pyrolyzing biomass and liquefied residue | |
| UA120384C2 (en) | Process and apparatus for continuous extracting hydrocarbons from medium/low-rank coal by indirect heating stepwise pyrolysis | |
| CN102899093B (en) | High-efficiency cleaning coal gasifying process | |
| CN106635096A (en) | System and method for treating pulverized coal and calcium-based raw material | |
| CN206266492U (en) | A kind of system for processing coal dust and calcium based raw material | |
| CN206428193U (en) | A kind of system of coal hydrogenation pyrolysis | |
| CN204039331U (en) | Coal gas circulation coal wholegrain radial sector pyrolysis system | |
| CN206279147U (en) | A kind of coal dust and the system of calcium based raw material treatment | |
| CN217173631U (en) | Pulverized coal hydrogasification and biomass pyrolysis coupling device | |
| CN206706019U (en) | The system that a kind of pulverized coal pyrolysis coupling calcium carbide production and acetylene occur | |
| CN115717090A (en) | Method for preparing synthesis gas from semi-coke oven gas | |
| CN106479577A (en) | A kind of system and method for coal sub-prime cascade utilization |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| WD01 | Invention patent application deemed withdrawn after publication | ||
| WD01 | Invention patent application deemed withdrawn after publication |
Application publication date: 20170308 |