CN109355070A - Biomass and coal copyrolysis reactor - Google Patents
Biomass and coal copyrolysis reactor Download PDFInfo
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- CN109355070A CN109355070A CN201811303140.0A CN201811303140A CN109355070A CN 109355070 A CN109355070 A CN 109355070A CN 201811303140 A CN201811303140 A CN 201811303140A CN 109355070 A CN109355070 A CN 109355070A
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- 239000003245 coal Substances 0.000 title claims abstract description 246
- 239000002028 Biomass Substances 0.000 title claims abstract description 198
- 238000000197 pyrolysis Methods 0.000 claims abstract description 131
- 238000009825 accumulation Methods 0.000 claims abstract description 43
- 239000000463 material Substances 0.000 claims abstract description 41
- 230000005855 radiation Effects 0.000 claims 2
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 abstract description 24
- 239000001257 hydrogen Substances 0.000 abstract description 23
- 229910052739 hydrogen Inorganic materials 0.000 abstract description 23
- 230000002195 synergetic effect Effects 0.000 abstract description 11
- 239000000047 product Substances 0.000 description 26
- 238000000034 method Methods 0.000 description 20
- 239000007789 gas Substances 0.000 description 19
- 238000006243 chemical reaction Methods 0.000 description 16
- 238000010438 heat treatment Methods 0.000 description 13
- 230000008569 process Effects 0.000 description 11
- 239000007787 solid Substances 0.000 description 10
- 239000000969 carrier Substances 0.000 description 8
- 239000003921 oil Substances 0.000 description 7
- 238000002309 gasification Methods 0.000 description 6
- 238000000926 separation method Methods 0.000 description 6
- 230000005484 gravity Effects 0.000 description 5
- 239000003077 lignite Substances 0.000 description 5
- 238000012545 processing Methods 0.000 description 5
- 230000008901 benefit Effects 0.000 description 4
- 239000003034 coal gas Substances 0.000 description 4
- 239000000446 fuel Substances 0.000 description 4
- 239000007788 liquid Substances 0.000 description 4
- 229910052573 porcelain Inorganic materials 0.000 description 4
- 239000000126 substance Substances 0.000 description 4
- 238000005979 thermal decomposition reaction Methods 0.000 description 4
- 238000001035 drying Methods 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 239000010828 animal waste Substances 0.000 description 2
- 230000015572 biosynthetic process Effects 0.000 description 2
- 230000008859 change Effects 0.000 description 2
- 238000002485 combustion reaction Methods 0.000 description 2
- 238000009833 condensation Methods 0.000 description 2
- 230000005494 condensation Effects 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 239000002994 raw material Substances 0.000 description 2
- 238000007670 refining Methods 0.000 description 2
- 238000005507 spraying Methods 0.000 description 2
- 239000010902 straw Substances 0.000 description 2
- 238000012546 transfer Methods 0.000 description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 2
- 239000002023 wood Substances 0.000 description 2
- 230000009471 action Effects 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 239000012075 bio-oil Substances 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 238000013461 design Methods 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000002635 electroconvulsive therapy Methods 0.000 description 1
- 238000004134 energy conservation Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 238000011031 large-scale manufacturing process Methods 0.000 description 1
- 239000012263 liquid product Substances 0.000 description 1
- 230000007246 mechanism Effects 0.000 description 1
- 239000010742 number 1 fuel oil Substances 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 230000026676 system process Effects 0.000 description 1
- 239000011269 tar 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
-
- 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
- C10B47/00—Destructive distillation of solid carbonaceous materials with indirect heating, e.g. by external combustion
- C10B47/18—Destructive distillation of solid carbonaceous materials with indirect heating, e.g. by external combustion with moving charge
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B53/00—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form
- C10B53/04—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form of powdered coal
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B57/00—Other carbonising or coking processes; Features of destructive distillation processes in general
- C10B57/02—Multi-step carbonising or coking processes
-
- 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
- Y02P20/141—Feedstock
- Y02P20/145—Feedstock the feedstock being materials of biological origin
Abstract
The invention discloses a kind of biomass and coal copyrolysis reactor, it include: reactor body, reactor body includes the internal biomass pyrolytic cylinder and pyrolysis of coal cylinder to communicate with each other, biomass pyrolytic cylinder is located at the top of pyrolysis of coal cylinder, the side wall of biomass pyrolytic cylinder is equipped at least one biomass feeding mouth, the side wall of pyrolysis of coal cylinder is equipped at least one coal material inlet and bottom is equipped with product exit, the cross-sectional area of biomass pyrolytic cylinder is less than the cross-sectional area of pyrolysis of coal cylinder, multiple heat accumulation type radiant tubes of uniform intervals setting are respectively equipped in biomass pyrolytic cylinder and pyrolysis of coal cylinder.Biomass according to the present invention and coal copyrolysis reactor, by the top that biomass pyrolytic cylinder is arranged in pyrolysis of coal cylinder, and make the cross-sectional area of biomass pyrolytic cylinder less than the cross-sectional area of pyrolysis of coal cylinder, hydrogen-rich in biomass is effectively transferred in coal, biomass and coal synergistic effect are obvious, improve the converting rate of coal.
Description
Technical field
The present invention relates to chemical industry, energy technology field, more particularly, to a kind of biomass and coal copyrolysis reactor.
Background technique
Coal is one of proved reserves conventional resource the most abundant in the world.As maximum coal production in the world and
Country of consumption, the energy resource structure feature in China are rich coal, oil-poor, few gas.It is the urgent of national product that the clean and effective of coal, which utilizes,
Demand.
Meanwhile China's biomass resource is also very rich, is often only agricultural crop straw, fuel wood, animal wastes and life rubbish
The yield of the four biolobic material raw material such as rubbish is equivalent to 7.8 hundred million toe (abbreviation of Ton Oil Equivalent, ton oil equivalent),
50% than China's total energy consumption in 2000 is more.Biomass as the renewable energy that uniquely can be stored and transport it
One, it is huge in global yield, it is widely distributed, it is smaller by territory restriction, it can regenerate.With countries in the world to energy conservation,
The attention of the problems such as environmental protection and Global climate change, so that strategic position of the renewable energy in energy development is more prominent
Out, biomass is converted into high-grade gas and liquid fuel has caused the great attention of countries in the world.
Relative to coal burning, gasification, liquefaction process, fast pyrogenation converts coal into solid-state, liquid and gaseous product, is
It realizes the important method of coal clean utilization, and converts biomass into a kind of important channel of liquid fuel and gas.Coal is
A kind of poor hydrogen substance, pyrolysis yield is low, and therefore, the mode that added hydrogen is typically employed to during to pyrolysis of coal improves coal
Conversion ratio, but the production cost of general additional pure hydrogen is higher, finds a kind of cheap hydrogen source and has become a hot topic of research.Biology
Matter is as a kind of hydrogen-rich materials, and not only pyrolysis temperature is lower than pyrolysis of coal temperature, is pyrolyzed prior to coal, and rich hydrogen producing, can
Using the hydrogen source as pyrolysis of coal, bio oil high income, but oxygen content are high.In order to both overcome individually pyrolysis insufficient, by coal with
Biomass copyrolysis gasification, the two pyrolytic gasification process can be effectively combined, advantage gives full play to, reduce at produce at
This, improves target product yield.
Currently, domestic and international existing pyrolytic process mostly uses porcelain ball and thermal decomposition product semicoke conduct from the point of view of heating method
Coal gas after solid thermal carriers or product char Gasification is as heating methods such as gas heat carriers.This heating method is related to
The processes such as heating, the separation of heat carrier cause system process long, and system failure rate is higher.The solid thermals such as semicoke, porcelain ball carry
Body has seriously affected the processing capacity of pyrolysis furnace apparatus, and there is also larger security risks for the preheating of the gas heat carriers such as coal gas.
From the point of view of type of reactor angle, majority using thermobalance, fixed bed, fluidized bed, air flow bed etc. to biomass with
Coal copyrolysis is studied.According to the difference of type of reactor, it is broadly divided into slow pyrolysis and fast pyrogenation two types, but
Result of study is fresh to show there is synergistic effect between the two less, and main cause is that the temperature range of biomass and pyrolysis of coal does not almost have
There are overlapping, 100 DEG C of difference or more.For the slow pyrolysis reaction carried out on thermobalance and fixed bed, when coal starts heat
Xie Shi, completely, the hydrogen having more than needed in biomass cannot be used effectively for pyrolysis of coal biomass for pyrolysis substantially, cause to be difficult to assist
Same-action；And for the fast pyrogenation for being carried out on fluidized bed or air flow bed, both the fast rate of heat addition can reduce pyrolysis
The temperature difference, but due to the two density contrast and airflow function, the hydrogen-rich in biomass is also not easy to be transferred in pyrolysis of coal oil gas, and collaboration is made
With also unobvious.
Summary of the invention
The present invention is directed at least solve one of the technical problems existing in the prior art.For this purpose, one object of the present invention
It is to propose a kind of biomass and coal copyrolysis reactor, the synergistic effect of biomass and pyrolysis of coal is more preferable.
Biomass according to an embodiment of the present invention and coal copyrolysis reactor, comprising: reactor body, the reactor sheet
Body includes the internal biomass pyrolytic cylinder and pyrolysis of coal cylinder to communicate with each other, and the biomass pyrolytic cylinder is located at the coal heat
The top of cylinder is solved, the side wall of the biomass pyrolytic cylinder is equipped at least one biomass feeding mouth, the pyrolysis of coal cylinder
The side wall of body is equipped at least one coal material inlet and bottom is equipped with product exit, the cross-sectional area of the biomass pyrolytic cylinder
Less than the cross-sectional area of the pyrolysis of coal cylinder, it is respectively equipped in the biomass pyrolytic cylinder and the pyrolysis of coal cylinder uniformly
Spaced multiple heat accumulation type radiant tubes.
Biomass according to an embodiment of the present invention and coal copyrolysis reactor, by the way that biomass pyrolytic cylinder is arranged in coal
It is pyrolyzed the top of cylinder, and makes the cross-sectional area of biomass pyrolytic cylinder less than the cross-sectional area of pyrolysis of coal cylinder, in biomass
Hydrogen-rich be effectively transferred in coal, biomass and coal synergistic effect are obvious, improve the converting rate of coal.Moreover, passing through
Multiple heat accumulation type radiant tubes of uniform intervals setting are respectively arranged in biomass pyrolytic cylinder and pyrolysis of coal cylinder, and it is traditional
Using porcelain ball and thermal decomposition product semicoke as the coal gas after solid thermal carriers or product char Gasification as gas heat carrier etc.
Heating method is compared, and process flow is simple, system temperature control is accurate, temperature adjustment is convenient, without gas and solid thermal carriers heating, point
From process, the failure rate of system is reduced.
According to some embodiments of the present invention, between the biomass feeding mouth and biomass pyrolytic cylinder top
Distance accounts for the 1/12~1/6 of the biomass pyrolytic cylinder height；Between at the top of the coal material inlet and the pyrolysis of coal cylinder
Distance account for the 1/12~1/6 of the pyrolysis of coal cylinder height.
According to some embodiments of the present invention, the biomass feeding mouth is two, two biomass feeding mouths point
Not Wei Yu the biomass pyrolytic cylinder two sides；The coal material inlet is two, and two coal material inlets are located at institute
State the two sides of pyrolysis of coal cylinder.
According to some embodiments of the present invention, the diameter of the biomass pyrolytic cylinder is the diameter of the pyrolysis of coal cylinder
20%~50%.
According to some embodiments of the present invention, the height of the biomass pyrolytic cylinder is the height of the pyrolysis of coal cylinder
30%~80%.
According to some embodiments of the present invention, the both ends of each heat accumulation type radiant tube are respectively equipped with burner, each
The burner at the both ends of the heat accumulation type radiant tube alternately burns.
According to some embodiments of the present invention, the temperature difference on each heat accumulation type radiant tube is not higher than 40 DEG C.
According to some embodiments of the present invention, the temperature of the intracorporal heat accumulation type radiant tube of the biomass pyrolytic cylinder is
350 DEG C~550 DEG C, the temperature of the intracorporal heat accumulation type radiant tube of pyrolysis of coal cylinder is 650 DEG C~950 DEG C.
According to some embodiments of the present invention, multiple heat accumulation type radiant tubes are in the horizontal and vertical upper equidistant water of difference
It is flat to be arranged in the reactor body.
According to some embodiments of the present invention, the biomass and the feed flow rates of coal ratio are between 1:6~1:1.
Additional aspect and advantage of the invention will be set forth in part in the description, and will partially become from the following description
Obviously, or practice through the invention is recognized.
Detailed description of the invention
Above-mentioned and/or additional aspect of the invention and advantage will become from the description of the embodiment in conjunction with the following figures
Obviously and it is readily appreciated that, in which:
Fig. 1 is the schematic diagram of biomass according to an embodiment of the present invention Yu coal copyrolysis reactor.
Appended drawing reference:
100: biomass and coal copyrolysis reactor；
1: biomass pyrolytic cylinder；11: biomass feeding mouth；
2: pyrolysis of coal cylinder；21: product exit；22: coal material inlet；
3: heat accumulation type radiant tube.
Specific embodiment
Biomass according to an embodiment of the present invention and coal copyrolysis reactor 100 are described below with reference to Fig. 1.
As shown in Figure 1, biomass according to an embodiment of the present invention and coal copyrolysis reactor 100, including reactor body.
Specifically, reactor body includes the internal biomass pyrolytic cylinder 1 and pyrolysis of coal cylinder 2 to communicate with each other.Example
Such as, in the example of fig. 1, biomass pyrolytic cylinder 1 and pyrolysis of coal cylinder 2 coaxially arranged and can extend along the vertical direction,
It is connected to inside biomass pyrolytic cylinder 1 and pyrolysis of coal cylinder 2.
The side wall of biomass pyrolytic cylinder 1 is equipped at least one biomass feeding mouth 11, biomass such as crops straw
Stalk, fuel wood, animal wastes and house refuse etc. can be entered in biomass pyrolytic cylinder 1 by biomass feeding mouth 11.Coal
The side wall for being pyrolyzed cylinder 2 is equipped at least one coal material inlet 22, for example non-caking coal of coal, Iight sticky coal, strong cohesiveness
Coal etc. can be entered in pyrolysis of coal cylinder 2 by coal material inlet 22.The bottom of pyrolysis of coal cylinder 2 is equipped with product exit 21, raw
The product that substance and coal obtain after being pyrolyzed in reactor body is discharged by product exit 21.
Multiple heat accumulation type radiant tubes of uniform intervals setting are respectively equipped in biomass pyrolytic cylinder 1 and pyrolysis of coal cylinder 2
3.In the description of the present invention, the meaning of " plurality " is two or more.Heat accumulation type radiant tube 3 is biomass and coal heat together
The pyrolytic reaction solved in reactor 100 provides heat source.It, can be by biomass pyrolytic cylinder when the work of multiple heat accumulation type radiant tubes 3
Body 1 and biomass in pyrolysis of coal cylinder 2 and coal are pyrolyzed respectively.Moreover, by biomass pyrolytic cylinder 1 and pyrolysis of coal
Evenly-spaced multiple heat accumulation type radiant tubes 3 are respectively arranged in cylinder 2, the coal and biomass that can be individually in reactor body
Heat source is provided, biomass and coal is heated evenly, so that the product quality arrived is uniform, while ensure that thermal decomposition product
Yield, moreover, because without heat carrier and mechanical rotation device, process flow is simple, system temperature control is accurate, temperature adjustment is convenient,
Heating, separation process without gas and solid thermal carriers, reduce the failure rate of system.
Biomass pyrolytic cylinder 1 is located at the top of pyrolysis of coal cylinder 2.As a result, by the way that biomass pyrolytic cylinder 1 to be arranged in
The top of pyrolysis of coal cylinder 2 is pyrolyzed coal completely under biomass pyrolytic atmosphere rapidly, while by the richness in biomass
Hydrogen is effectively transferred in coal, improves the converting rate of coal.Specifically, biomass is entered by biomass feeding mouth 11
It will flow downward under the effect of gravity after in biomass pyrolytic cylinder 1, and by the heat accumulation type radiant tube in biomass pyrolytic cylinder 1
Pyrolytic reaction occurs for 3 heating, generates oil gas；These oil gas can be under the action of its own gravity into pyrolysis of coal cylinder 2
Top, and mixed with the coal from coal material inlet 22, required environment rich is provided for pyrolysis of coal, 2 top of pyrolysis of coal cylinder
Coal is flowed downward in the environment of hydrogen-rich by gravity, and is heated by the heat accumulation type radiant tube 3 in pyrolysis of coal cylinder 2, hair
Raw pyrolytic reaction, generates gaseous state, liquid product and solid semicoke；These products flow downward along pyrolysis of coal cylinder 2 simultaneously, and
It is removed from the product exit 21 of 2 bottom of pyrolysis of coal cylinder.
The cross-sectional area of biomass pyrolytic cylinder 1 is less than the cross-sectional area of pyrolysis of coal cylinder 2.Make to give birth to by setting as a result,
The cross-sectional area of material pyrolysis cylinder 1 is less than the cross-sectional area of pyrolysis of coal cylinder 2, and biomass can be effectively ensured and reach with pyrolysis of coal
To synergistic effect, specifically, for example, the cross-sectional area due to biomass pyrolytic cylinder 1 is less than the cross section of pyrolysis of coal cylinder 2
Product, in this way, the hydrogen generated in biomass pyrolysis process can first be assembled in the relatively small biomass pyrolytic cylinder 1 in space, from
And formed be rich in hydrogen gas, and then when these rich in hydrogen gases when downwardly into the top of pyrolysis of coal cylinder 2 still
It is maintained at the state rich in hydrogen.
Biomass according to an embodiment of the present invention and coal copyrolysis reactor 100, by arranging biomass pyrolytic cylinder 1
In the top of pyrolysis of coal cylinder 2, and make the cross-sectional area of biomass pyrolytic cylinder 1 less than the cross-sectional area of pyrolysis of coal cylinder 2, it is raw
Hydrogen-rich in substance is effectively transferred in coal, and biomass and coal synergistic effect are obvious, improves the converting rate of coal.And
And multiple heat accumulation type radiant tubes by being respectively arranged uniform intervals setting in biomass pyrolytic cylinder 1 and pyrolysis of coal cylinder 2
3, with it is traditional using porcelain ball and thermal decomposition product semicoke as the coal gas after solid thermal carriers or product char Gasification as gas
The heating methods such as body heat carrier are compared, and process flow is simple, system temperature control is accurate, temperature adjustment is convenient, are carried without gas and solid thermal
Heating, the separation process of body, reduce the failure rate of system.
According to some embodiments of the present invention, referring to Fig.1, biomass feeding mouth 11 is located at the upper of biomass pyrolytic cylinder 1
Portion, coal material inlet 22 are located at the top of pyrolysis of coal cylinder 2.As a result, by the way that biomass feeding mouth 11 is arranged in biomass pyrolytic
The top of cylinder 1, biomass can be filled during flowing downward by the heat accumulation type radiant tube 3 in biomass pyrolytic cylinder 1
Divide heating and be sufficiently pyrolyzed, to provide good environment rich for pyrolysis of coal.By the way that coal material inlet 22 is arranged in coal heat
The top of cylinder 2 is solved, the coal newly entered from coal material inlet 22 can be pyrolyzed completely in the environment of hydrogen-rich, so as to further
Improve the converting rate of coal.
Still optionally further, the distance between 1 top of biomass feeding mouth 11 and biomass pyrolytic cylinder accounts for biomass thermal
Solve 1/12~1/6 (including endpoint value) of 1 height of cylinder.As a result, if by biomass feeding mouth 11 and biomass pyrolytic cylinder 1
The distance between top accounts for 1 height of biomass pyrolytic cylinder less than 1/12, then biomass feeding mouth 11 and biomass pyrolytic cylinder 1
The distance between top is relatively close, so as to be not easy to the processing of biomass feeding mouth 11；If by biomass feeding mouth 11 with
The distance between 1 top of biomass pyrolytic cylinder accounts for 1 height of biomass pyrolytic cylinder greater than 1/6, then is likely to occur biomass not
The case where being sufficiently pyrolyzed, to be unfavorable for providing good environment rich for pyrolysis of coal.That is, by by biomass feeding
The distance between 1 top of mouth 11 and biomass pyrolytic cylinder accounts for biomass pyrolytic cylinder 1 and is highly arranged between 1/12~1/6,
Guarantee biomass pyrolytic completely, provide good environment rich for pyrolysis of coal while, facilitate biomass feeding mouth 11
Processing, reduce costs.
Still optionally further, the distance between 2 top of coal material inlet 22 and pyrolysis of coal cylinder accounts for 2 height of pyrolysis of coal cylinder
1/12~1/6 (including endpoint value).As a result, if the distance between 2 top of coal material inlet 22 and pyrolysis of coal cylinder is accounted for coal heat
2 height of cylinder is solved less than 1/12, then the distance between coal material inlet 22 and biomass pyrolytic cylinder 1 are relatively close, so as to occur
Hydrogen-rich cannot enter the case where pyrolysis of coal cylinder 2 well, and be not easy to the processing of coal material inlet 22；If by coal material inlet
The distance between 22 and 2 top of pyrolysis of coal cylinder account for 2 height of pyrolysis of coal cylinder greater than 1/6, due to the cross section of pyrolysis of coal cylinder 2
Product is larger, and the space in pyrolysis of coal cylinder 2 is larger, and the coal entered from coal material inlet 22 may be not in good environment rich,
It is unfavorable for improving the converting rate of coal.In other words, by accounting for the distance between coal material inlet 22 and 2 top of pyrolysis of coal cylinder
Pyrolysis of coal cylinder 2 is highly arranged between 1/12~1/6, while guaranteeing to improve the converting rate of coal, facilitates biology
The processing of matter material inlet 11, reduces costs.
According to some embodiments of the present invention, the diameter of biomass pyrolytic cylinder 1 is the 20% of the diameter of pyrolysis of coal cylinder 2
~50% includes endpoint value).The cross-sectional shape of biomass pyrolytic cylinder 1 and pyrolysis of coal cylinder 2 is circle at this time.As a result,
If the 20% of the diameter for making the diameter of biomass pyrolytic cylinder 1 be less than pyrolysis of coal cylinder 2 is arranged, at this time biomass pyrolytic cylinder
1 diameter is smaller, possibly required environment rich can not be provided for pyrolysis of coal；If being arranged makes the straight of biomass pyrolytic cylinder 1
Diameter is greater than the 50% of the diameter of pyrolysis of coal cylinder 2, may not can guarantee biomass and pyrolysis of coal reaches good synergistic effect.?
That is making the 20%~50% of the diameter of the diameter pyrolysis of coal cylinder 2 of biomass pyrolytic cylinder 1 by setting, guaranteeing
While providing required environment rich for pyrolysis of coal, biomass can be effectively ensured and pyrolysis of coal reaches collaboration well and makees
With.
Further, the height of biomass pyrolytic cylinder 1 be pyrolysis of coal cylinder 2 height 30%~80% (including end
Point value).Thus, it is possible to be further ensured that biomass and pyrolysis of coal reach synergistic effect.
Optionally, biomass and the feed flow rates of coal ratio are between 1:6~1:1 (including endpoint value).Thus, it is possible into one
Step guarantees that biomass and pyrolysis of coal reach synergistic effect.
According to some embodiments of the present invention, the both ends of each heat accumulation type radiant tube 3 are respectively equipped with burner, each accumulation of heat
The burner at the both ends of formula radiant tube 3 alternately burns.In particular, for example, heat accumulation type radiant tube 3 is at its tube body both ends point
It is not provided with burner, the flame that the burner combustion in one end of heat accumulation type radiant tube 3 generates formation temperature ladder when spraying
Degree, i.e., gradually decrease from the outside temperature of burner.Similarly, it is generated in the burner combustion of the other end of heat accumulation type radiant tube 3
Flame when spraying also formation temperature gradient.When the burner at 3 both ends of heat accumulation type radiant tube alternately burns, formed
The superposition of two temperature gradients so that entire 3 bulk temperature of heat accumulation type radiant tube is evenly distributed, and then can make entire
Reaction mass in biomass pyrolytic cylinder 1 and pyrolysis of coal cylinder 2 is heated evenly.
Further, the temperature difference on each heat accumulation type radiant tube 3 is not higher than 40 DEG C.Each heat accumulation type radiant tube 3 at this time
On maximum temperature and minimum temperature difference be less than or equal to 40 DEG C.As a result, if the temperature difference on each heat accumulation type radiant tube 3 is big
In 40 DEG C, the temperature difference at this time on each heat accumulation type radiant tube 3 is relatively large, so as to biomass pyrolytic cylinder 1 or coal occur
In other words the even phenomenon of the reaction mass uneven heating being pyrolyzed in cylinder 2 is made on each heat accumulation type radiant tube 3 by setting
Temperature difference is not higher than 40 DEG C, and reaction mass in biomass pyrolytic cylinder 1 and pyrolysis of coal cylinder 2 can be effectively ensured and be heated evenly.
Optionally, the temperature of the heat accumulation type radiant tube 3 in biomass pyrolytic cylinder 1 is 350 DEG C~550 DEG C (including endpoints
Value), the temperature of the heat accumulation type radiant tube 3 in pyrolysis of coal cylinder 2 is 650 DEG C~950 DEG C (including endpoint value).Thus, it is possible to protect
Card biomass and pyrolysis of coal reach synergistic effect.Specifically, sectional temperature-controlled method is used at this time, is respectively reached in the same time
The optimum temperature of biomass and pyrolysis of coal, so that the hydrogen-rich in biomass is efficiently transferred in coal, so that pyrolysis of coal can be in life
It is pyrolyzed completely under material pyrolysis atmosphere, and then improves pyrolysis of coal conversion ratio and target product yield.
Two biomass feeding mouths 11 and two coal material inlets 22 are shown in Fig. 1 for illustration purposes, still
Those of ordinary skill after having read following technical solution, be clearly understood that the program be applied to three or more
In the technical solution of a biomass feeding mouth 11 and coal material inlet 22, this is also fallen within protection scope of the present invention.
Specifically, for example, in the example of fig. 1, biomass feeding mouth 11 is two, and two biomass feeding mouths 11 are distinguished
Positioned at the two sides of biomass pyrolytic cylinder 1；Coal material inlet 22 is two, and two coal material inlets 22 are located at pyrolysis of coal cylinder 2
Two sides.Further, two biomass feeding mouths 11 can be along biomass pyrolytic cylinder 1 diametrically, two coal feeds
Mouth 22 can be along pyrolysis of coal cylinder 2 diametrically.
Optionally, biomass feeding mouth 11 and coal material inlet 22 are respectively screw feeder mouth.Biomass feeding mouth 11 at this time
With spiral feeding mechanism can be respectively equipped at coal material inlet 22, reaction mass is respectively screw and is delivered to corresponding material inlet
(i.e. above-mentioned biomass feeding mouth 11 and coal material inlet 22).But not limited to this.
According to some embodiments of the present invention, as shown in Figure 1, multiple heat accumulation type radiant tubes 3 are in horizontal and vertical upper difference
Equidistant horizontal arrangement is in reactor body.Thus, it is possible to be further ensured that biomass pyrolytic cylinder 1 and pyrolysis of coal cylinder 2
Interior biomass and coal is heated evenly.
In the description of the present invention, it is to be understood that, term " center ", " longitudinal direction ", " transverse direction ", " length ", " width ",
" thickness ", "upper", "lower", "front", "rear", "left", "right", "vertical", "horizontal", "top", "bottom", "inner", "outside", " axis
To ", " radial direction ", the orientation or positional relationship of the instructions such as " circumferential direction " be to be based on the orientation or positional relationship shown in the drawings, be only for
Convenient for the description present invention and simplify description, rather than the device or element of indication or suggestion meaning there must be specific side
Position is constructed and operated in a specific orientation, therefore is not considered as limiting the invention.
According to some embodiments of the present invention, when reactor body operates under normal pressure (i.e. an atmospheric pressure), reaction
The cross-sectional shape of device ontology is rectangular or round.But not limited to this.It is understood that pressure in reactor body and outer
When portion's atmospheric pressure is roughly the same, the concrete shape of reactor body can be designed according to actual needs, with preferably full
Sufficient practical application.
Certainly, the invention is not limited thereto, other embodiments according to the present invention, when reactor body is (i.e. big in high pressure
In an atmospheric pressure) under when operating, the cross-sectional shape of reactor body is circle.At this time due to the pressure in reactor body
Reactor can be effectively ensured by the way that the cross-sectional shape of reactor body to be provided in round greater than the pressure of outside atmosphere
Ontology has good pressure-resistant performance.
Biomass according to an embodiment of the present invention and the operating process of coal copyrolysis reactor 100 are as follows:
By the temperature after drying, preheating be 100 DEG C~270 DEG C, granularity 80% be less than 10mm and 6mm biomass below and
Coal enters biomass pyrolytic cylinder 1 and pyrolysis of coal cylinder 2 through biomass feeding mouth 11 and coal material inlet 22 respectively.Biomass is by weight
Power effect flows downward along biomass pyrolytic cylinder 1, is added in 2~8s by the heat accumulation type radiant tube 3 in biomass pyrolytic cylinder 1
To 350~550 DEG C pyrolytic reaction occurs for heat, generates oil gas.The oil gas under the effect of gravity, into the top of pyrolysis of coal cylinder 2
Portion, and mixed with the coal of the coal material inlet 22 from 2 top of pyrolysis of coal cylinder, required environment rich is provided for pyrolysis of coal.Coal
The coal at 2 top of cylinder is pyrolyzed in the environment of hydrogen-rich, is affected by gravity, flows downward along pyrolysis of coal cylinder 2, in 3~12s
The interior heat accumulation type radiant tube 3 by pyrolysis of coal cylinder 2 is heated to 650~950 DEG C, and pyrolytic reaction occurs, and generates gaseous state, liquid produces
Object and solid semicoke.Above-mentioned product flows downward along pyrolysis of coal cylinder 2 simultaneously, and goes out from the product of 2 bottom of pyrolysis of coal cylinder
Mouth 21 removes, and hereafter can enter subsequent product dedusting, condensation, separation and refining system.
It is below sawdust and coal such as white tone China lignite as raw material using biomass, through crushing, drying, preheating, sawdust is dry
It is less than 6mm less than 10%, 80% granularity to moisture；White tone China brown coal drying is less than 4mm less than 15%, 80% granularity to moisture
Example is illustrated.
Sawdust feed flow rates are 5kg/s, and white tone China lignite feed flow rates are 15kg/s.By biomass pyrolytic cylinder 1 and coal
Pyrolysis cylinder 2 is cylindrical shape, and diameter is respectively 1m and 3m, and height is respectively 3m and 6m.Biomass feeding mouth 11 is located at biology
Matter is pyrolyzed the 1 following 0.2m in top of cylinder, and coal material inlet 22 is located at the 2 following 0.7m in top of pyrolysis of coal cylinder.By sawdust and white tone China
Lignite is added to the biomass feeding mouth 11 of biomass pyrolytic cylinder 1 and the coal material inlet 22 of pyrolysis of coal cylinder 2.To reactor body
It heats up, 3 temperature of heat accumulation type radiant tube in 3~4s or so, biomass pyrolytic cylinder 1 is increased to 450~500 DEG C；?
5-6s or so, 3 temperature of heat accumulation type radiant tube in pyrolysis of coal cylinder 2 are increased to 800~850 DEG C or so.Biomass pyrolytic cylinder 1
Pyrolytic reaction occurs for interior sawdust, generates hydrogen-rich gas, flows downward along biomass pyrolytic cylinder 1, and enters pyrolysis of coal cylinder
2, it is mixed with the white tone China lignite in pyrolysis of coal cylinder 2, pyrolytic reaction occurs, generate pyrolysis gas, tar, water and half
It is burnt.These products flow downward along pyrolysis of coal cylinder 2 simultaneously, and remove from the product exit 21 of 2 bottom of pyrolysis of coal cylinder, enter
Subsequent product dedusting, condensation, separation and refining system.
It carries out the brown copyrolysis of sawdust and white tone China using above-mentioned biomass and coal copyrolysis reactor 100 to study, discovery is burnt
Oil yield pyrolysis yield more independent than the two is averagely higher by 35~45%, and conversion ratio is higher by 10~20%, illustrates using according to this hair
There are apparent synergistic effects with pyrolysis of coal for the biomass that bright biomass and coal copyrolysis reactor 100 is pyrolyzed.
Biomass according to an embodiment of the present invention and coal copyrolysis reactor 100 are a kind of downlink heat accumulating type biomass and coal
Copyrolysis reactor 100, has the advantage that
1) two sections of down-flow fluidized bed using ECTs are set on same reactor body, and the feed entrance point of biomass and coal is respectively set (i.e.
Biomass feed inlet and coal feed inlet), and sectional temperature-controlled method is used, the best of the two pyrolysis is respectively reached in the same time
Temperature；
2) more heat accumulation type radiant tubes 3 are used, coal and biomass in reactor can be individually for, heat source is provided, without heat carrier
And mechanical rotation device, process flow is simple, system temperature control is accurate, temperature adjustment is convenient, without gas and solid thermal carriers heating,
Separation process reduces the failure rate of system；
3) biomass pyrolytic cylinder 1 is mounted on to the top of pyrolysis of coal cylinder 2, so that coal is rapidly in biomass pyrolytic atmosphere
Lower pyrolysis completely, the hydrogen-rich in biomass is efficiently transferred in coal, the converting rate of coal is improved；
4) convection current, heat transfer and radiant heat transfer are combined, the thermal efficiency of system is improved；
5) compared with semicoke is as heat carrier, tar dustiness is reduced；
6) strong to coal adaptability, no matter non-caking coal, Iight sticky coal, strong caking coal etc. are suitable for；
7) biomass and the structure design of coal copyrolysis reactor 100 are simple and convenient to operate, large-scale production easy to accomplish.
In the description of this specification, reference term " one embodiment ", " some embodiments ", " illustrative examples ",
The description of " example ", " specific example " or " some examples " etc. means specific features described in conjunction with this embodiment or example, knot
Structure, material or feature are included at least one embodiment or example of the invention.In the present specification, to above-mentioned term
Schematic representation may not refer to the same embodiment or example.
Although an embodiment of the present invention has been shown and described, it will be understood by those skilled in the art that: not
A variety of change, modification, replacement and modification can be carried out to these embodiments in the case where being detached from the principle of the present invention and objective, this
The range of invention is defined by the claims and their equivalents.
Claims (10)
1. a kind of biomass and coal copyrolysis reactor characterized by comprising
Reactor body, the reactor body include the internal biomass pyrolytic cylinder and pyrolysis of coal cylinder to communicate with each other, institute
The top that biomass pyrolytic cylinder is located at the pyrolysis of coal cylinder is stated, the side wall of the biomass pyrolytic cylinder is equipped at least one
A biomass feeding mouth, the side wall of the pyrolysis of coal cylinder is equipped at least one coal material inlet and bottom is equipped with product exit,
The cross-sectional area of the biomass pyrolytic cylinder be less than the pyrolysis of coal cylinder cross-sectional area, the biomass pyrolytic cylinder and
Multiple heat accumulation type radiant tubes of uniform intervals setting are respectively equipped in the pyrolysis of coal cylinder.
2. biomass according to claim 1 and coal copyrolysis reactor, which is characterized in that the biomass feeding mouth with
The 1/12~1/6 of the biomass pyrolytic cylinder height is accounted for the distance between at the top of the biomass pyrolytic cylinder；
The 1/12~1/ of the pyrolysis of coal cylinder height is accounted for the distance between at the top of the coal material inlet and the pyrolysis of coal cylinder
6。
3. biomass according to claim 1 and coal copyrolysis reactor, which is characterized in that the biomass feeding mouth is
Two, two biomass feeding mouths are located at the two sides of the biomass pyrolytic cylinder；
The coal material inlet is two, and two coal material inlets are located at the two sides of the pyrolysis of coal cylinder.
4. biomass according to claim 1 and coal copyrolysis reactor, which is characterized in that the biomass pyrolytic cylinder
Diameter be the pyrolysis of coal cylinder diameter 20%~50%.
5. biomass according to claim 1 and coal copyrolysis reactor, which is characterized in that the biomass pyrolytic cylinder
Height be the pyrolysis of coal cylinder height 30%~80%.
6. biomass according to any one of claims 1-5 and coal copyrolysis reactor, which is characterized in that each described
The both ends of heat accumulation type radiant tube are respectively equipped with burner, and the burner at the both ends of each heat accumulation type radiant tube is handed over
For burning.
7. biomass according to claim 6 and coal copyrolysis reactor, which is characterized in that each heat accumulating type radiation
Temperature difference on pipe is not higher than 40 DEG C.
8. biomass according to claim 1 and coal copyrolysis reactor, which is characterized in that the biomass pyrolytic cylinder
The temperature of the interior heat accumulation type radiant tube is 350 DEG C~550 DEG C, the intracorporal heat accumulation type radiant tube of pyrolysis of coal cylinder
Temperature is 650 DEG C~950 DEG C.
9. biomass according to claim 1 and coal copyrolysis reactor, which is characterized in that multiple heat accumulating type radiation
Pipe is in the horizontal and vertical upper equidistant horizontal arrangement of difference in the reactor body.
10. biomass according to claim 1 and coal copyrolysis reactor, which is characterized in that the biomass with it is described
The feed flow rates ratio of coal is between 1:6~1:1.
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