CN107083249A - A kind of fine coal prepares air flow bed pyrolysis oven, the system and method vented one's spleen rich in methane thermal - Google Patents
A kind of fine coal prepares air flow bed pyrolysis oven, the system and method vented one's spleen rich in methane thermal Download PDFInfo
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- CN107083249A CN107083249A CN201710313601.1A CN201710313601A CN107083249A CN 107083249 A CN107083249 A CN 107083249A CN 201710313601 A CN201710313601 A CN 201710313601A CN 107083249 A CN107083249 A CN 107083249A
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- 239000003245 coal Substances 0.000 title claims abstract description 100
- 238000000197 pyrolysis Methods 0.000 title claims abstract description 98
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 title claims abstract description 81
- 238000000034 method Methods 0.000 title claims abstract description 49
- 210000000952 spleen Anatomy 0.000 title claims abstract description 16
- 238000002309 gasification Methods 0.000 claims abstract description 42
- 230000008569 process Effects 0.000 claims abstract description 28
- 230000003647 oxidation Effects 0.000 claims abstract description 25
- 238000007254 oxidation reaction Methods 0.000 claims abstract description 25
- 238000006243 chemical reaction Methods 0.000 claims abstract description 16
- 229930195733 hydrocarbon Natural products 0.000 claims abstract description 14
- 230000008676 import Effects 0.000 claims abstract description 14
- 238000005979 thermal decomposition reaction Methods 0.000 claims abstract description 12
- 239000006185 dispersion Substances 0.000 claims abstract description 9
- 239000007789 gas Substances 0.000 claims description 149
- 239000000047 product Substances 0.000 claims description 26
- 239000012265 solid product Substances 0.000 claims description 18
- 239000007787 solid Substances 0.000 claims description 15
- 230000015572 biosynthetic process Effects 0.000 claims description 13
- 238000001816 cooling Methods 0.000 claims description 12
- 238000003786 synthesis reaction Methods 0.000 claims description 12
- 239000000843 powder Substances 0.000 claims description 9
- -1 small molecule Hydrocarbons Chemical class 0.000 claims description 5
- 229920000742 Cotton Polymers 0.000 claims description 4
- 238000010504 bond cleavage reaction Methods 0.000 claims description 4
- 239000000567 combustion gas Substances 0.000 claims description 4
- 238000002485 combustion reaction Methods 0.000 claims description 4
- 238000004321 preservation Methods 0.000 claims description 4
- 230000007017 scission Effects 0.000 claims description 4
- 229910000323 aluminium silicate Inorganic materials 0.000 claims description 3
- 239000011449 brick Substances 0.000 claims description 3
- 239000000498 cooling water Substances 0.000 claims description 3
- HNPSIPDUKPIQMN-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical compound O=[Si]=O.O=[Al]O[Al]=O HNPSIPDUKPIQMN-UHFFFAOYSA-N 0.000 claims description 3
- 239000007790 solid phase Substances 0.000 claims description 3
- 150000002430 hydrocarbons Chemical class 0.000 abstract description 12
- 238000005336 cracking Methods 0.000 abstract description 6
- 239000002245 particle Substances 0.000 abstract description 5
- 238000010438 heat treatment Methods 0.000 description 11
- 239000004215 Carbon black (E152) Substances 0.000 description 7
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 6
- 239000000203 mixture Substances 0.000 description 6
- 239000003345 natural gas Substances 0.000 description 6
- 239000002994 raw material Substances 0.000 description 6
- 238000004458 analytical method Methods 0.000 description 4
- 239000002802 bituminous coal Substances 0.000 description 4
- 239000012159 carrier gas Substances 0.000 description 4
- 238000005516 engineering process Methods 0.000 description 4
- 239000001301 oxygen Substances 0.000 description 4
- 229910052760 oxygen Inorganic materials 0.000 description 4
- 238000002360 preparation method Methods 0.000 description 4
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 3
- 229910052757 nitrogen Inorganic materials 0.000 description 3
- 230000009257 reactivity Effects 0.000 description 3
- UFWIBTONFRDIAS-UHFFFAOYSA-N Naphthalene Chemical compound C1=CC=CC2=CC=CC=C21 UFWIBTONFRDIAS-UHFFFAOYSA-N 0.000 description 2
- 150000001722 carbon compounds Chemical class 0.000 description 2
- 230000008859 change Effects 0.000 description 2
- 229910052739 hydrogen Inorganic materials 0.000 description 2
- 239000007788 liquid Substances 0.000 description 2
- 229920002521 macromolecule Polymers 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 125000002496 methyl group Chemical group [H]C([H])([H])* 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 239000012071 phase Substances 0.000 description 2
- 239000002351 wastewater Substances 0.000 description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 2
- 239000002028 Biomass Substances 0.000 description 1
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 1
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 1
- ISWSIDIOOBJBQZ-UHFFFAOYSA-N Phenol Chemical compound OC1=CC=CC=C1 ISWSIDIOOBJBQZ-UHFFFAOYSA-N 0.000 description 1
- 150000001335 aliphatic alkanes Chemical class 0.000 description 1
- 125000000217 alkyl group Chemical group 0.000 description 1
- 230000001887 anti-feedant effect Effects 0.000 description 1
- 125000006615 aromatic heterocyclic group Chemical group 0.000 description 1
- 125000003118 aryl group Chemical group 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000008901 benefit Effects 0.000 description 1
- 239000000969 carrier Substances 0.000 description 1
- 238000006757 chemical reactions by type Methods 0.000 description 1
- 239000003034 coal gas Substances 0.000 description 1
- 239000000571 coke Substances 0.000 description 1
- 238000000354 decomposition reaction Methods 0.000 description 1
- 230000008021 deposition Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 239000003344 environmental pollutant Substances 0.000 description 1
- 239000003546 flue gas Substances 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 239000012634 fragment Substances 0.000 description 1
- 238000001754 furnace pyrolysis Methods 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- 230000007774 longterm Effects 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 125000000325 methylidene group Chemical group [H]C([H])=* 0.000 description 1
- GRVDJDISBSALJP-UHFFFAOYSA-N methyloxidanyl Chemical group [O]C GRVDJDISBSALJP-UHFFFAOYSA-N 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 239000010813 municipal solid waste Substances 0.000 description 1
- 239000002006 petroleum coke Substances 0.000 description 1
- 231100000719 pollutant Toxicity 0.000 description 1
- 238000006068 polycondensation reaction Methods 0.000 description 1
- 150000003254 radicals Chemical class 0.000 description 1
- 238000006722 reduction reaction Methods 0.000 description 1
- 239000011819 refractory material Substances 0.000 description 1
- 239000002002 slurry 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
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- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Materials Engineering (AREA)
- Organic Chemistry (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The air flow bed pyrolysis oven vented one's spleen rich in methane thermal is prepared the invention discloses a kind of fine coal, it includes burner hearth (3) and the entrance cavity (1) located at the burner hearth (3) above, separated at the top of the burner hearth (3) between the entrance cavity (1) by dividing plate (2), dispersion hole is evenly distributed with the dividing plate (2), entrance cavity (1) side is provided with the process burner (4) that tubular is provided with inside gas heat carrier import (7), the entrance cavity (1).The system and method vented one's spleen rich in methane thermal are prepared the invention also discloses fine coal, the system includes the air flow bed pyrolysis oven, and gasification furnace or oxidation furnace.During work, gas heat carrier cocurrent can flow downward with fine coal in the burner hearth, and direct contact heat transfer can effectively improve the heat transfer efficiency between pulverized coal particle and thermal source, fine coal is occurred fast pyrogenation reaction and secondary cracking, the yield of thermal decomposition product small molecular hydro carbons can be effectively increased.
Description
Technical field
The present invention relates to a kind of device for preparing and being vented one's spleen rich in methane thermal, and in particular to prepared by a kind of fine coal is rich in methane thermal
Air flow bed pyrolysis oven, the system and method vented one's spleen.
Background technology
Natural gas is the important source material of industrial process and civilian process, and natural gas is prepared by raw material of coal and is conducive to alleviating me
The natural gas supply and demand that state faces at present is nervous.In traditional gasification process, coal is synthesis first by vapor-oxygen gasified
Gas, then purified, conversion, methanation and sub-prime upgrading, can just obtain natural gas.The most important and most basic unit of this technique
It is the selection of gasification furnace.
Common natural gas from coal factory is typically using Lurgi moving bed lump coal pressurized gasifications technology production high methane content
Synthesis gas be used as prepare synthetic natural gas raw material.Moving bed crushed coal pressure gasifying by representative of Lurgi gasification furnaces it is thick
Methane content is high in coal gas, and this portion of methane accounts for the half of methane in final products synthetic natural gas, for natural gas from coal
For there is very big advantage.But the technology has the disadvantages that：Single furnace gas small scale；Diameter<5mm coal can not enter
Gasification furnace；Lurgi gasifier steam decomposition rate is low；Gasification waste water amount is big, and complicated component contains the pollutants such as tar, naphthalene and phenol, waste water
Processing is difficult.
No matter dry powder gasifies or coal water slurry gasification entrained flow gasification, there is good commercial Application, and coal feeding amount is big, technology
It is mature and stable, there is the experience run steadily in the long term.But gasification furnace outlet syngas temperatures are very high, wherein being practically free of first
Alkane, and H2/ CO is huge for follow-up synthesis air cooling and methanation device investment than low.
Pyrolysis of coal is an extremely complex process, with chemical reaction type, can be classified as cracking and the major class of polycondensation two
Reaction.Pyrolysis of coal is coal process change, such as the particularly important pilot process of burning, gasification, liquefaction technique.In the pyrolysis of coal
The composition influence of Cheng Zhong, temperature and heating rate on pyrolysis of coal product is very big, when the final temperature of heating is relatively low (about 500~600 DEG C)
When, increase heating rate, volatile producibility can be improved and increase the ratio of wherein product liquid and gaseous product；When heating
During final temperature higher (about 800~1100 DEG C), increase heating rate, the yield of volatile matter can be improved further, but wherein liquid
The ratio of product and gaseous product can be reduced on the contrary.The pyrolytic process of coal can produce CH4, in 500~700 DEG C of pyrolysis temperature ranges
It is interior, under inert atmosphere conditions, CH4Formation be mainly derived from the five kinds of presomas produced during pyrolysis of coal：Methoxyl group in coal
Fracture, the fracture of alkyl side chain, the fracture of methyl, the secondary pyrolysis of volatile matter, the reduction reaction of aromatic heterocyclic on aromatic rings.
Above-mentioned five kinds of presomas are main to be produced in 500~700 DEG C.When using some reducibility gas, such as H2, the gas such as CO, carry out generation
After inert atmosphere, methyl and methylene chain break in the cracking process of pyrolysis of coal free radical, influence texture of coal can be promoted, from
And promote CH4Formation.The growth of gas residence time, is conducive to the secondary cracking of tar molecules, generates CH4、C2H4Deng hydro carbons
Component.In existing coal powder pyrolysis oven, pyrolysis temperature typically at 470~900 DEG C, for improve pyrolysis rate more use fluid bed
Form, using the hot conditions of the method for internal heat type need to consume substantial amounts of heat to maintain more than the thermal efficiency to improve, due to
Heat carrier (flue gas, semicoke, circulating ash, air etc.) limitation of, thermal decomposition product itself separates difficulty with heat carrier, often leads to heat
Solve product purity inadequate.When using inert atmosphere as heat carrier, coal is stablized due to enough hydroperoxyl radicals can not be provided
The fragment group produced is pyrolyzed, so that the yield of hydrocarbon gas and tar light oil in thermal decomposition product can be reduced.In addition, when using hydrogen
When gas is as heat carrier, although the yield of hydrocarbon gas and tar light oil can be improved in thermal decomposition product but technique can be also greatly increased
Cost.Those skilled in the art are directed to a kind of pyrolysis gas for being used for pulverized coal pyrolysis device, methane being rich in preparation of exploitation always
The yield of wherein methane is improved, follow-up Methane Conversion is met.
The content of the invention
Therefore, CH in the pyrolysis gas prepared for pulverized coal pyrolysis stove in the prior art4、C2H4Deng the relatively low skill of hydrocarbon content
Art problem, the air flow bed pyrolysis oven vented one's spleen rich in methane thermal is prepared it is an object of the invention to provide a kind of fine coal, for making powder
Coal fast pyrogenation, prepares the pyrolysis gas rich in methane.
The air flow bed pyrolysis oven of the present invention includes the burner hearth (3) erect and the entrance cavity located at the burner hearth (3) above
(1), burner hearth (3) interlude is straight barrel type, and burner hearth (3) bottom is provided with outlet (5), burner hearth (3) top and institute
State and separated by dividing plate (2) between entrance cavity (1), dispersion hole, entrance cavity (1) top are evenly distributed with the dividing plate (2)
Portion is provided with burner flange (6), and entrance cavity (1) side is provided with inside gas heat carrier import (7), the entrance cavity (1) and set
There is the process burner (4) of tubular, process burner (4) upper end passes through the burner flange (6), and lower end passes through the dividing plate
(2)。
During the air flow bed pyrolysis oven work, using main component as reducibility gas (H2, CO etc.) high-temperature gas mixture body
For gas heat carrier (gas thermal source), by gas heat carrier pass sequentially through the gas heat carrier import (7), entrance cavity (1), every
The dispersion hole of plate (2) introduces burner hearth (3)；Meanwhile, fine coal to be pyrolyzed is introduced into burner hearth (3) by technique nozzle (4).Air heat
The cocurrent in burner hearth (3) flows downward carrier with fine coal, in flow process, gas heat carrier and fine coal direct contact heat transfer,
The heat transfer efficiency between pulverized coal particle and thermal source can be effectively improved, increases the heating rate of fine coal, the heating rate of the process
More than 100K/s, in the range of fast pyrogenation and flashing speed oven, fine coal can be made to occur fast pyrogenation reaction.Due to gas thermal source with
Based on reducibility gas, under high-temperature reductibility environment heat scission reaction will further occur for the product of fine coal fast pyrogenation, heat
The secondary conversion of product (macromolecule hydrocarbon such as tar) is solved, thermal decomposition product small molecular hydro carbons (CH can be effectively increased4、C2H4Deng)
Yield.Additionally by the volume flow of regulation gas heat carrier, residence time of the fine coal in stove can be controlled, to promote coal
CH in pyrolytic process4Generation, improve pyrolysis of coal in CH4Yield, so as to prepare the pyrolysis gas of methane rich content.Pulverized coal pyrolysis
After can obtain gas solid product, gas solid product from outlet (5) discharge, wherein gas be the pyrolysis gas rich in methane, Gu
Body is semicoke, and semicoke granularity is below 100 μm, and gasification reactivity is good.Therefore, the air flow bed pyrolysis oven can be with existing air-flow
Bed gasification furnace or oxidation furnace are used cooperatively, and connection forms the circulatory system.Gas in gas solid product can oxidized stove part
Oxidation, obtained high-temperature gas sends the air flow bed pyrolysis oven back to as gas heat carrier.Semicoke in gas solid product can be through
Gasification furnace gasifies, and obtained high-temperature synthesis gas can also send the air flow bed pyrolysis oven back to as gas heat carrier.
Preferably, the burner hearth (3), the process burner (4) and the entrance cavity (1) coaxial line.
Preferably, the side wall of the burner hearth (3) and the entrance cavity (1) is provided with refractory liner, the refractory liner is resistance to
Lining of fire-bricks or water-cooling wall.
Preferably, the process burner (4) has the cooling layer for being used for leading to burner cooling water outside, the cooling layer outside is attached
There is aluminosilicate heat-preservation cotton.The cooling layer and the aluminosilicate heat-preservation cotton can play heat-insulated effect, it is to avoid gas heat carrier and
Heat exchange is carried out before fine coal mixing.
Preferably, burner hearth (3) the direct tube section internal diameter (D1) and the ratio of the burner hearth (3) straight tube segment length (H1) are
D1:H1=0.05~0.2.The draw ratio of the burner hearth (3) direct tube section is set to above range, is conducive to extension fine coal gentle
Residence time of the body heat carrier in the burner hearth (3), be conducive to the secondary cracking of tar molecules, and then improve CH4、C2H4Deng
The yield of hydrocarbon component.
Preferably, burner hearth (3) bottom is tapered, the inclination angle (α) of tapered sidewalls is 30~60 °；The outlet (5)
The ratio of internal diameter (D2) and the burner hearth (3) direct tube section internal diameter (D1) is D2:D1=0.1~0.5.Burner hearth (3) bottom is set
The tapered solid for being easy to deposition is put to flow out；The internal diameter (D2) of the control outlet (5), can control the flow of gas-solid product,
The residence time of fine coal and gas heat carrier in the burner hearth (3) can also be controlled simultaneously.
Another object of the present invention is to provide a kind of fine coal to prepare the system vented one's spleen rich in methane thermal, it includes described
Air flow bed pyrolysis oven, it also includes gas heat carrier feedway, and the gas heat carrier feedway is：
Gasification furnace, provided with being pyrolyzed, solid inlet is gentle to dissolve mouth, the outlet (5) of burner hearth (3) bottom to the gasification furnace
Pyrolysis solid in the gas solid product of discharge can add the gasification furnace, the gasification outlet by the pyrolysis solid inlet
Connected by pipeline and the gas heat carrier import (7)；The gasification furnace can select existing powder, coke etc. of being used for and gasify
Airflow bed gasification furnace；
Or oxidation furnace, the oxidation furnace is provided with pyrolysis gas entrance and combustion gas outlet, the outlet of burner hearth (3) bottom
(5) pyrolysis gas in the gas solid product of discharge adds the oxidation furnace by the pyrolysis solid inlet, and the combustion gas goes out
Mouth passes through pipeline and the gas heat carrier import (7) is connected.The oxidation furnace is used for (the not exclusively combustion of pyrolysis gas partial oxidation
Burn)；The oxidation furnace can select existing combustion furnace.
The method vented one's spleen rich in methane thermal is prepared it is still another object of the present invention to provide a kind of fine coal, methods described is used
Described air flow bed pyrolysis oven, be specially：
Main component is passed sequentially through into gas heat carrier import (7), entrance cavity for the gas heat carrier of reducibility gas
(1), the dispersion hole of dividing plate (2) introduces burner hearth (3)；Meanwhile, fine coal is introduced into burner hearth (3) by technique nozzle (4)；Air heat is carried
The direct heat transfer in burner hearth (3) is contacted body with fine coal, and fast pyrogenation reaction occurs for fine coal, because gas heat carrier is with reproducibility gas
Based on body, under high-temperature reductibility environment heat scission reaction further occurs for the product of fine coal fast pyrogenation, so as to generate smaller
The hydrocarbons of molecule；Obtained gas solid product is finally pyrolyzed to discharge from outlet (5).
It is preferred that, the fine coal is the fine coal for the dry powder state that particle diameter is less than 100 μm, and technique is passed through with carrier gas conveying during introducing
Nozzle (4) enters, and the carrier gas can be nitrogen, CO2, pyrolysis gas, synthesis gas etc..
The gas heat carrier is the high-temperature gas after the gasification or oxidation of carbon compound.Temperature preferably 1000~130
℃.The preferred coal of carbon compound, petroleum coke, biomass, rubbish and other carbonaceous solids discarded objects.
It is preferred that, the gas heat carrier is the solid (semicoke) in the gas solid product of outlet (5) discharge through gasification furnace
Gasify the high-temperature synthesis gas produced.
Or preferably, described gas heat carrier is the partial thermal decomposition gas warp in the gas solid product of outlet (5) discharge
The high-temperature gas that oxidation furnace imperfect combustion is produced.
The beneficial effects of the present invention are：
1st, the air flow bed pyrolysis oven of fine coal of the invention preparation methane rich pyrolysis gas includes the burner hearth and entrance cavity of straight barrel type,
During work, the gas heat carrier of reproducibility can enter the entrance cavity (1), the entrance through the gas heat carrier entrance (7)
Chamber (1) can play a part of gas buffer, and then gas heat carrier enters the burner hearth by the dispersion hole of the dividing plate (2)
(3) in, while fine coal to be pyrolyzed is introduced by the process burner (4), gas heat carrier is with fine coal in the burner hearth (3)
Cocurrent flows downward.On the one hand, in flow process, gas heat carrier and fine coal direct contact heat transfer can effectively improve powder
Heat transfer efficiency between coal particle and thermal source, increases the heating rate of fine coal, and fine coal can be made to occur fast pyrogenation reaction and secondary
Cracking, is effectively increased thermal decomposition product small molecular hydro carbons (CH4、C2H4Deng) yield.On the other hand, using gas heat carrier as
Thermal source heat, can make fire box temperature be evenly distributed, and be conducive to thermal decomposition product to occur secondary pyrolytic reaction formation small molecule hydrocarbon
Thing.Additionally by the volume flow of regulation gas heat carrier, residence time of the fine coal in stove can be controlled, to promote pyrolysis of coal
During CH4Generation, improve pyrolysis of coal in CH4Yield, so as to prepare the pyrolysis gas of methane rich content.
2nd, it is the pyrolysis gas rich in methane that the gas in gas solid product can be obtained after pulverized coal pyrolysis, can oxidized stove part
Oxidation, obtained high-temperature gas sends the air flow bed pyrolysis oven back to as gas heat carrier.Semicoke granularity in gas solid product
Below 100 μm, gasification reactivity is good, can gasify through gasification furnace, and obtained high-temperature synthesis gas can also be sent back to as gas heat carrier
The air flow bed pyrolysis oven.Therefore, the air flow bed pyrolysis oven can constitute the circulatory system with existing oxidation furnace or gasification furnace,
The supply of gas heat carrier can effectively be solved the problems, such as, it is not necessary to which raw material in addition prepares the reducibility gas of high temperature, saves significantly
The about energy and equipment cost.
Brief description of the drawings
The schematic diagram for the air flow bed pyrolysis oven that Fig. 1 vents one's spleen for the preparation of the present invention rich in methane thermal.
Reference
1- entrance cavities；2- dividing plates；3- burner hearths；4- process burners；5- is exported；6- burner flanges；7- gas heat carrier imports；
S1- gas heat carriers；S2- fine coal；S3- burner cooling waters；S4- gas solid products.
Embodiment
Below in conjunction with specific embodiment, the invention will be further described.It should be understood that following examples are merely to illustrate this
Invention is not for restriction the scope of the present invention.
The fine coal of embodiment 1 prepares the air flow bed pyrolysis oven vented one's spleen rich in methane thermal
Fig. 1 show the gas that can be used for the preparation of fine coal fast pyrogenation to be vented one's spleen rich in methane thermal of a preferred embodiment of the present invention
Fluidized bed pyrolysis oven, it includes burner hearth 3 and entrance cavity 1, and entrance cavity 1 is above burner hearth 3, the side wall liner of burner hearth 3 and entrance cavity 1
Have a refractory material (refractory brick), burner hearth 3 be straight barrel type and bottom provided with outlet 5, between burner hearth 3 and entrance cavity 1 by dividing plate 2 every
Open, dispersion hole is evenly distributed with dividing plate 2, the top of entrance cavity 1 is provided with burner flange 6, and the side of entrance cavity 1 is provided with gas heat carrier
Import 7, the inside of entrance cavity 1 is provided with the process burner 4 of tubular, and the upper end of process burner 4 passes through burner flange 6, and lower end passes through dividing plate
2.Wherein burner hearth 3, process burner 4 and the coaxial line of entrance cavity 1.Process burner 4 is outer to be had outside cooling layer, cooling layer with sial
Sour heat-preservation cotton.
Preferably, the direct tube section internal diameter D1 of the burner hearth 3 and straight tube segment length H1 of burner hearth 3 ratio is D1:H1=0.05~0.2.
Preferably, the bottom of burner hearth 3 is tapered, the inclination alpha of tapered sidewalls is 30~60 °；The internal diameter D2 of outlet 5 and burner hearth 3
Direct tube section internal diameter D1 ratio is D2:D1=0.1~0.5.
During real work, by gas heat carrier S1 from gas heat carrier 7 passes sequentially through entrance cavity 1, the dispersion hole of dividing plate 2 is drawn
Enter burner hearth 3；Meanwhile, fine coal S2 is introduced into burner hearth 3 by technique nozzle 4；Lead to burner cooling outside process burner 4 in attached cooling layer
Water S3, it is to avoid fine coal S2 is thermally contacted in advance with gas heat carrier S1.Gas heat carrier S1 and fine coal S2 is in burner hearth (3) and flows to
Lower flowing, in flow process, gas heat carrier S1 and fine coal S2 direct contact heat transfers can effectively improve pulverized coal particle and gas
Heat transfer efficiency between body heat carrier S 1, increase fine coal S2 heating rate, the heating rate of the process is more than 100K/s, fast
In the range of speed heat solution and flashing speed oven, fine coal can be made to occur fast pyrogenation reaction.Because gas heat carrier S1 is with reducibility gas
Based on, under high-temperature reductibility environment heat scission reaction, thermal decomposition product will further occur for the product of fine coal S2 fast pyrogenations
The secondary conversion of (macromolecule hydrocarbon such as tar), can be effectively increased thermal decomposition product small molecular hydro carbons (CH4、C2H4Deng) yield.
The outlet 5 of final gas solid product S4 from the bottom of burner hearth 3 is discharged after fine coal S2 pyrolysis, is handled into follow-up workshop section.
Solid in gas solid product S4 is semicoke, and semicoke granularity is below 100 μm, and gasification reactivity is good, can add in gasification furnace and gasify
After obtain high-temperature synthesis gas, as gas heat carrier import 7 anti-feeding air flow bed pyrolysis oven in use (see embodiment 2).Gas-solid
Gas in phase product S4 is the pyrolysis gas rich in methane, and high-temperature gas can be obtained by oxidation furnace partial oxidation, can equally be made
It is that gas heat carrier is instead sent into air flow bed pyrolysis oven by gas heat carrier import 7, realizes circulation (see embodiment 3).
The pyrolysis of Shenmu County's bituminous coal of embodiment 2 (thermal source is char Gasification product)
Fine coal raw material：Shenmu County's bituminous coal, Industrial Analysis and elementary analysis are as shown in table 1.
The Industrial Analysis and elementary analysis of Shenmu County's bituminous coal of table 1
Pyrolysis system：Air flow bed pyrolysis oven (day handles 2200 tons of coal butts), the existing entrained flow gasification of embodiment 1
Stove.
The related parameter of air flow bed pyrolysis oven：Fine coal is conveyed by carrier gas (nitrogen), and fine coal inlet amount is 90926kg/h,
80 DEG C of temperature, pressure 4.3MPa；Carrier gas (nitrogen) air inflow 9864.4kg/h, 80 DEG C of temperature, pressure 4.3MPa；It is pyrolyzed outlet of still
700 DEG C of temperature, pyrolysis furnace pressure 4.3MPa；Gas heat carrier (thermal source)：Fine coal is after pyrolysis from the gas-solid phase of the discharge of outlet 5
The high-temperature synthesis gas that semicoke in product in S4 gasifies through gasification furnace.
The related parameter of gasification furnace：Vapor air inflow 20080kg/h, 350 DEG C of temperature, pressure 5.0MPa；Oxygen enters
Doses 60170kg/h, 25 DEG C of temperature, pressure 4.3MPa；Gasification of carbonaceous raw material is fine coal after pyrolysis from the gas-solid of the discharge of outlet 5
Whole semicokes in phase product in S4, temperature is 350 DEG C；The heater outlet temperature that gasifies is 1300 DEG C, gasification furnace furnace pressure
4.3MPa。
Table 2 give gasification furnace go out furnace gases composition and air flow bed pyrolysis oven go out furnace gases composition.Fine coal is fast through pyrolysis oven
All semicokes that speed heat solution is produced, high-temperature synthesis gas is produced through gasification furnace gasification, wherein about 16.32% high-temperature synthesis gas enters
In air flow bed pyrolysis oven, it is possible to meet the heat required for fine coal fast pyrogenation.The yield of methane is close to 10% in pyrolysis gas,
H2/ CO is close to 1.
Table 2 goes out furnace gases composition
The pyrolysis of Shenmu County's bituminous coal of embodiment 3 (thermal source is circulation pyrolysis gas)
Fine coal raw material：Be the same as Example 2
Pyrolysis system device：Pyrolysis oven (day handles 2200 tons of coal butts), the existing oxidation furnace of embodiment 1
The related parameter of air flow bed pyrolysis oven：Gas heat carrier is the pyrolysis gas portion of pyrolysis of coal generation in air flow bed pyrolysis oven
The pyrolysis gas that the high-temperature gas divided after oxidation, i.e. air flow bed pyrolysis oven are produced, is partly passed through in oxidation furnace, oxygen supply makes it work off one's feeling vent one's spleen
Temperature reaches 1000 DEG C, and the high-temperature gas is then returned in air flow bed pyrolysis oven by gas heat carrier entrance 7, is used as powder
The thermal source of pyrolysis of coal.Remaining parameter be the same as Example 2.
The related parameter of oxidation furnace：The inlet amount 2288.754kg/h of oxygen, 25 DEG C of temperature, pressure 4.3MPa；Oxidation is former
Expect for the partial thermal decomposition gas of air flow bed pyrolysis oven output, temperature is 350 DEG C；It is 1000 DEG C, oxidation furnace stove to aoxidize heater outlet temperature
Interior pressure 4.3MPa.
Table 3, which is given to circulate the air flow bed pyrolysis oven of pyrolysis gas as thermal source, goes out furnace gases composition.Fine coal fast pyrogenation is produced
Raw pyrolysis gas, wherein only needing about 1.82% pyrolysis gas to enter heating by ignition in oxidation furnace produces high-temperature gas, it is possible to full
Heat required for foot-powder coal fast pyrogenation.The yield of methane is close to 13%, H in pyrolysis gas2/ CO is close to 2.5.
The gas of table 3 is constituted
The preferred embodiment to the invention is illustrated above, but the invention is not limited to implement
Example, those skilled in the art are without prejudice to can also make a variety of equivalent modification under precondition for innovation of the present invention or replace
Change, these equivalent modifications or replacement are all contained in the application claim limited range.
Claims (10)
1. a kind of fine coal prepares the air flow bed pyrolysis oven vented one's spleen rich in methane thermal, it is characterised in that it includes the burner hearth (3) erect
With the entrance cavity (1) located at the burner hearth (3) above, burner hearth (3) interlude is straight barrel type, and burner hearth (3) bottom is set
Have and separated at the top of outlet (5), the burner hearth (3) between the entrance cavity (1) by dividing plate (2), it is uniform on the dividing plate (2)
It is distributed with the top of dispersion hole, the entrance cavity (1) and is provided with burner flange (6), entrance cavity (1) side is provided with gas heat carrier
The process burner (4) of tubular is provided with inside import (7), the entrance cavity (1), process burner (4) upper end is burnt through described
Mouth flange (6), lower end passes through the dividing plate (2).
2. air flow bed pyrolysis oven according to claim 1, it is characterised in that the burner hearth (3), the process burner (4)
With the entrance cavity (1) coaxial line.
3. air flow bed pyrolysis oven according to claim 1, it is characterised in that the burner hearth (3) and the entrance cavity (1)
Side wall is provided with refractory liner, and the refractory liner is lining of fire brick or water-cooling wall.
4. air flow bed pyrolysis oven according to claim 1, it is characterised in that the process burner (4) has outside to be used to lead to
Has aluminosilicate heat-preservation cotton outside the cooling layer of burner cooling water, the cooling layer.
5. air flow bed pyrolysis oven according to claim 1, it is characterised in that burner hearth (3) the direct tube section internal diameter (D1) with
The ratio of burner hearth (3) the straight tube segment length (H1) is D1:H1=0.05~0.2.
6. air flow bed pyrolysis oven according to claim 1, it is characterised in that burner hearth (3) bottom is tapered, tapered side
The inclination angle (α) of wall is 30~60 °；The ratio of internal diameter (D2) and the burner hearth (3) direct tube section internal diameter (D1) of the outlet (5) is
D2:D1=0.1~0.5.
7. a kind of fine coal prepares the system vented one's spleen rich in methane thermal, it is characterised in that it is included such as any one of claim 1~6
Described air flow bed pyrolysis oven, it also includes gas heat carrier feedway, and the gas heat carrier feedway is：
Gasification furnace, provided with being pyrolyzed, solid inlet is gentle to dissolve mouth, outlet (5) discharge of burner hearth (3) bottom to the gasification furnace
Gas solid product in pyrolysis solid the gasification furnace can be added by the pyrolysis solid inlet, the gasification outlet pass through
Pipeline is connected with the gas heat carrier import (7)；
Or oxidation furnace, the oxidation furnace is provided with pyrolysis gas entrance and combustion gas outlet, the outlet (5) of burner hearth (3) bottom
Pyrolysis gas in the gas solid product of discharge can partly pass through the pyrolysis solid inlet and add the oxidation furnace, the combustion gas
Outlet is connected by pipeline with the gas heat carrier import (7).
8. a kind of fine coal prepares the method vented one's spleen rich in methane thermal, it is characterised in that methods described used as claim 1~
Air flow bed pyrolysis oven described in 6 any one, methods described is specially：
By main component for reducibility gas gas heat carrier pass sequentially through gas heat carrier import (7), entrance cavity (1), every
The dispersion hole of plate (2) introduces burner hearth (3)；Meanwhile, fine coal is introduced into burner hearth (3) by technique nozzle (4)；Gas heat carrier and powder
Coal in burner hearth (3) direct heat transfer contact, fine coal occur fast pyrogenation reaction, due to gas heat carrier using reducibility gas as
Main, under high-temperature reductibility environment heat scission reaction further occurs for the product of fine coal fast pyrogenation, so as to generate more small molecule
Hydrocarbons；Obtained gas solid product is finally pyrolyzed to discharge from outlet (5).
9. method as claimed in claim 8, it is characterised in that the gas-solid phase that described gas heat carrier is discharged for outlet (5)
The high-temperature synthesis gas that solid in product is produced through gasification furnace gasification.
10. method as claimed in claim 8, it is characterised in that the gas-solid phase that described gas heat carrier is discharged for outlet (5)
The high-temperature gas that the oxidized stove imperfect combustion of partial thermal decomposition gas in product is produced.
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Application publication date: 20170822 |