CN203999499U - A kind of integrated form two-step approach biomass and coal copyrolysis device - Google Patents
A kind of integrated form two-step approach biomass and coal copyrolysis device Download PDFInfo
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- CN203999499U CN203999499U CN201420393879.6U CN201420393879U CN203999499U CN 203999499 U CN203999499 U CN 203999499U CN 201420393879 U CN201420393879 U CN 201420393879U CN 203999499 U CN203999499 U CN 203999499U
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- 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
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- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E50/00—Technologies for the production of fuel of non-fossil origin
- Y02E50/10—Biofuels, e.g. bio-diesel
Abstract
The utility model relates to a kind of integrated form two-step approach biomass and coal copyrolysis device, by two transfer lines are set, respectively coal and biomass are delivered in reactor, heat by superpower process furnace and mid power process furnace respectively, thereby realize the independent pyrolysis of biomass and coal, avoid the two unfavorable synergistic effect causing due to the difference of pyrolysis temperature, the pyrolysis of biomass pyrolytic and coal is integrated in a reactor, the pyrolysis of biomass pyrolytic and coal all arranges best temperature of reaction, rich hydrogen pyrolysis gas after hypomere biomass pyrolytic provides rich hydrogen atmosphere for the pyrolysis of epimere coal, be conducive to improve liquid fuel yield.By copyrolysis in an integrated reactor, realize the complementation of biomass pyrolytic tar and pyrolysis of coal tar, reduce the oxygen level of biomass pyrolytic tar, improve the quality of copyrolysis oil.Meanwhile, operating procedure is simple, can atmospheric operation, or pressurized operation, be conducive to the expansion of unit scale.
Description
Technical field
The utility model relates to a kind of biomass and coal copyrolysis device, is specifically related to a kind of integrated form two-step approach biomass and coal copyrolysis device.
Background technology
The energy is the necessary basis that the mankind depend on for existence and development, but along with the growth of world population and the minimizing day by day of fossil energy, under the pressure of the pressure of the aspects such as environment protection, minimizing environmental pollution, explores new alternative clean energy and seem particularly important simultaneously.Compared with fossil energy, biomass energy is a kind of reproducible, has the energy of outstanding advantage at the aspect such as energy-saving and emission-reduction, environmental protection.
The annual production of China's agricultural crop straw approximately has 600Mt, the about 50Mt of rice husk, and the resistates producing in the forestry course of processing approximately has 30Mt, and three totals are amounted to standard coal 215Mt.Biomass are important treasure-houses of potential energy source and chemical feedstocks, and the cleaning of biomass transforms the great attention that has caused countries in the world.
Pyrolysis is the important starting stage in coal or the biomass thermal course of processing, can obtain different chemical product and liquid fuel by pyrolysis.Due to less H/C value, pyrolysis transformation efficiency and the liquid product yield of coal are conventionally lower, and biomass have high H/C value and volatile content, and the bio-oil yield that pyrolysis obtains is higher, simultaneously can a large amount of hydrogen of by-product.If the hydrogen that coal can effectively utilize biomass pyrolytic to produce in pyrolytic process, realize the pyrolysis under hydrogen atmosphere, stablize the free radical in pyrolysis of coal process by hydropyrolysis, not only contribute to the raising of pyrolysis product liquid yield, thereby but also can significantly reduce production costs by instead of pure hydrogen.Therefore, utilize biomass and coal copyrolysis technology to produce liquid fuel, realize the two efficient, clean, comprehensive utilization, have great importance for protection of the environment, the raising level of resources utilization.
Existingly studies have shown that synergistic effect can occur for biomass and coal copyrolysis, liquid product yield is increased, but current research major part is in phase of basic research, the experimental study of normally carrying out in thermobalance or fixed bed.Dong Kyoo Park etc. utilizes TGA and fixed-bed reactor, by changing biomass and the ratio of mixture research sawdust of coal and the copyrolysis reaction process of bituminous coal, find that biomass energy promotes the pyrolysis of coal, when showing as the transformation efficiency of copyrolysis mixture and yield and reacting separately with coal higher than biomass add with.(reference: Dong Kyoo Park, Sang Done Kim, See Hoon Lee, etc.Co-pyrolysischaracteristics of sawdust and coal blend in TGA and a fixed bed reactor.Bioresource Technology, 2010,101:6151 – 6156).The research such as Li Zhang find the pyrolysis in the time falling tar yield that in bed bioreactor, copyrolysis produces and be greater than coal and the independent pyrolysis of biomass of coal and biomass generate adding of tar and, and burnt content lower than pyrolysis separately generate Jiao adding with.(reference: LiZhang, Shaoping Xu, Wei Zhao, Shuqin Liu.Co-pyrolysis of biomass andcoal in a free fall reactor.Fuel, 2007,86:353-359).Utility model patent 200710012661.6 has been mentioned a kind of method of biomass and coal manufacturing wet fuel by rapid common thermal decomposition, this patent is by the mode of solid thermal carriers rapid heating, realize relatively a large amount of biomass and a small amount of coal quick copyrolysis under rich hydrogen environment, the method is conducive to improve pyrolytic tar productive rate and quality, but these patent utilization solid thermal carriers are by biomass and coal Synchronous Heating, and pass into pyrolysis hydrogen-rich recycle, increase production liquid product yield, ignore the pyrolysis temperature range characteristic lower than the pyrolysis temperature range of coal of biomass, do not make full use of the synergistic effect of the two.
Comprehensive existing document and patent are known, there is synergistic effect in biomass and coal under certain condition copyrolysis, but the research many places of carrying out are at present at phase of basic researchs such as fixed beds, existing patent does not make full use of the attribute that biomass are different from pyrolysis of coal temperature yet, does not make full use of the synergistic effect of the two.
Utility model content
The purpose of this utility model is to overcome the shortcoming existing in above-mentioned prior art, a kind of integrated form two-step approach biomass and coal copyrolysis device are provided, utilize two-step approach that biomass pyrolytic and the pyrolysis of coal are separated, provide and add hydrogen atmosphere with the pyrolysis that the rich hydrogen pyrolysis gas of biomass pyrolytic is coal, thereby the synergy of generation, promotes the raising of liquid yield, in addition, device can pressurized operation, is beneficial to industrialization and amplifies.
For achieving the above object, the utility model by the following technical solutions: comprise cylinder, the pneumatic outlet of cylinder is divided into some roads, and the first via is connected to the bottom inlet of reactor through biomass conveying; The second tunnel is connected to the top entrance of reactor after coal e Foerderanlage; The outlet of reactor connects purification recovery unit; The process furnace of described reactor arranged outside is divided into the superpower process furnace that is positioned at the first half and the mid power process furnace that is positioned at Lower Half;
The material inlet of described coal e Foerderanlage connects coal hopper, and the material inlet of biomass conveying connects biomass hopper.
The bottom inlet of described reactor is also connected to the outlet of cylinder through being provided with the pipeline of gas preheater.
The entrance that the bottom of described reactor connects gas preheater is pre-hot gas entrance, and hot gas entrance is three to 12 in advance, and is circumference uniform distribution.
Between described coal hopper and coal e Foerderanlage, be in series with coal lock hopper and coal sending cans.
Between described biomass hopper and biomass conveying, be in series with biomass lock hopper and biomass fermentation tank sending.
Described purification recovery unit comprises: tornado dust collector, semicoke holding tank, tar washing tower and tar holding tank;
The pneumatic outlet of the gas inlet ligation device of described tornado dust collector, tornado dust collector pneumatic outlet connects tar washing tower, and the top of tar washing tower offers pneumatic outlet; And the outlet at bottom of tornado dust collector and tar washing tower is connected respectively semicoke holding tank and tar holding tank.
Described reactor is integrated reformer.
The coal tremie pipe of the top entrance of described coal e Foerderanlage ligation device, and the middle part of coal tremie pipe insertion reaction device.
Described reactor bottom biomass and the ratio of the feeding rate of reactor head coal are (95:5)～(50:50).
Pressure in described reactor is 0.001-4.0MPa, and the Heating temperature of first half superpower process furnace is 400-800 DEG C, and the Heating temperature of Lower Half mid power process furnace is 300-700 DEG C.
The utlity model has following beneficial effect: the prior art of comparing, the utility model is by arranging two transfer lines, respectively coal and biomass are delivered in reactor, heat by superpower process furnace and mid power process furnace respectively, thereby realize the independent pyrolysis of biomass and coal, avoid the two unfavorable synergistic effect causing due to the difference of pyrolysis temperature, the pyrolysis of biomass pyrolytic and coal is integrated in a reactor, the pyrolysis of biomass pyrolytic and coal all arranges best temperature of reaction, rich hydrogen pyrolysis gas after hypomere biomass pyrolytic provides rich hydrogen atmosphere for the pyrolysis of epimere coal, be conducive to improve liquid fuel yield.By copyrolysis in an integrated reactor, realize the complementation of biomass pyrolytic tar and pyrolysis of coal tar, reduce the oxygen level of biomass pyrolytic tar, improve the quality of copyrolysis oil.Meanwhile, operating procedure is simple, can atmospheric operation, or pressurized operation, be conducive to the expansion of unit scale, be conducive to spread and use, cost-saving, raise the efficiency.
Brief description of the drawings
Fig. 1 is one-piece construction schematic diagram of the present utility model;
In figure: 1: coal hopper; 2: coal lock hopper; 3: coal sending cans; 4: coal e Foerderanlage; 5: biomass hopper; 6: biomass lock hopper; 7: biomass fermentation tank sending; 8: biomass conveying; 9: cylinder; 10: gas preheater; 11: reactor; 12: superpower process furnace; 13: mid power process furnace; 14: coal tremie pipe; 15: tornado dust collector; 16: semicoke holding tank; 17: tar washing tower; 18: tar holding tank.
Embodiment
Below in conjunction with accompanying drawing, the utility model is described in further detail.
Referring to Fig. 1, the utility model comprises cylinder 9, and the pneumatic outlet of cylinder 9 is divided into some roads, and the first via is connected to the bottom inlet of reactor 11 through biomass conveying 8; The second tunnel is connected to the coal tremie pipe 14 of the top entrance of reactor 11 after coal e Foerderanlage 4, and coal tremie pipe slotting 14 enters the middle part of reactor 11; The bottom inlet of Third Road reactor 11 is also connected to the outlet of cylinder 9 through being provided with the pipeline of gas preheater 10; The outlet of reactor 11 connects purification recovery unit; The process furnace of described reactor 11 arranged outside is divided into the superpower process furnace 12 that is positioned at the first half and the mid power process furnace 13 that is positioned at Lower Half; Purification recovery unit comprises: tornado dust collector 15, semicoke holding tank 16, tar washing tower 17 and tar holding tank 18; The pneumatic outlet of the gas inlet ligation device 11 of tornado dust collector 15, tornado dust collector 15 pneumatic outlets connect tar washing tower 17, and the top of tar washing tower 17 offers pneumatic outlet; And the outlet at bottom of tornado dust collector 15 and tar washing tower 17 is connected respectively semicoke holding tank 16 and tar holding tank 18.
The material inlet of coal e Foerderanlage 4 connects coal hopper 1, is in series with coal lock hopper 2 and coal sending cans 3 between coal hopper 1 and coal e Foerderanlage 4; The material inlet of biomass conveying 8 connects biomass hopper 5, and between biomass hopper 5 and biomass conveying 8, is in series with biomass lock hopper 6 and biomass fermentation tank sending 7.Reactor 11 is integrated reformer, and bottom heating gas entrance is three to 12, and is circumference uniform distribution, and reactor 11 bottom biomass and the ratio of the feeding rate of reactor 11 top coals are (95:5)～(50:50); Pressure in reactor 11 is 0.001-4.0MPa, and the Heating temperature of first half superpower process furnace 12 is 400-800 DEG C, and the Heating temperature that Lower Half mid power process furnace is 13 is 300-700 DEG C.
Implementation method:
Feed coal is dried to moisture and is less than 3%, and granularity is less than 3mm, and biomass starting material is dried to moisture and is less than 5%, and granularity is less than 3mm, and the feeding rate of biomass and coal is than being (90:10)～(60:40).Feed coal enters coal e Foerderanlage 4 through coal hopper 1, coal lock hopper 2, coal sending cans 3, enters the pyrolysis section of coal in reactor 11 under the conveying of a certain amount of carrier gas, and the blanking mouth of pipe 14 of feed coal is at reactor middle part; Meanwhile, biomass starting material is sent into biomass conveying 8 through biomass hopper 5, biomass lock hopper 6, biomass fermentation tank sending 7, enters the pyrolysis section of biomass in reactor 11 under the conveying of a certain amount of carrier gas, and the feeding mouth of biomass starting material is in the bottom of reactor.Cylinder 9 Zhong mono-tunnels enter reactor 11 after gas preheater 10 heating, for the fluidized gas in post-reactor with partial thermal decomposition institute heat requirement is provided.
The working pressure of reactor 11 is generally 0.001～4.0MPa, the temperature of reactor 11 top pyrolysis of coal sections is generally 400～800 DEG C, optimal reaction temperature is 550～650 DEG C, the temperature of reactor 11 bottom biomass pyrolytic sections is generally 300～700 DEG C, optimal reaction temperature is 350～450 DEG C, controls the gentle speed of height of reactor 11, makes the residence time of material in reactor be less than 2s, by fast pyrogenation, at utmost improve the yield of product liquid.The pyrolysis that is coal by the rich hydrogen pyrolysis gas producing after biomass pyrolytic provides and has added hydrogen atmosphere, stablize the free radical in pyrolysis of coal process, increase on the one hand liquid yield, realize the synergistic effect of biomass and coal copyrolysis, on the other hand, add the character that hydrogen atmosphere can improve pyrolysis oil product, make more lightweight and more stable of oil product.Material after pyrolysis carries oil gas and enters tornado dust collector 15 from reactor 11 tops, semicoke after tornado dust collector 15 separate is disposed to semicoke holding tank 16, pyrolysis gas after dedusting enters tar washing tower 17, tar after the washing of tar washing lotion drains into tar holding tank 18 by the bottom of tar washing tower 17, and the coal gas after purification is discharged by tar washing tower 17 tower tops.
Reaction member reactor 11 comprises two sections, the pyrolysis section that epimere is coal, and the pyrolysis section that hypomere is biomass, controls respectively different temperature of reaction for two sections.The pyrolysis of biomass and coal is the independent pyrolysis of two-step approach, completes but be integrated in a reactor 11.Advantage is: biomass are separated independent pyrolysis with coal, avoid the two unfavorable synergistic effect causing due to the difference of pyrolysis temperature, rich hydrogen pyrolysis gas after hypomere biomass pyrolytic, for the pyrolysis of epimere coal provides rich hydrogen atmosphere, is conducive to improve the yield of product liquid.In addition, by an interior copyrolysis of reactor 11, realize the complementation of biomass coke tar and coal tar, reduce the oxygen level of biomass coke tar, improve the quality of copyrolysis oil.This device technique is simple, can atmospheric operation, also can pressurized operation, and be conducive to the expansion of unit scale.
Claims (10)
1. integrated form two-step approach biomass and coal copyrolysis device, it is characterized in that: comprise cylinder (9), the pneumatic outlet of cylinder (9) is divided into some roads, and the first via is connected to the bottom inlet of reactor (11) through biomass conveying (8); The second tunnel is connected to the top entrance of reactor (11) after coal e Foerderanlage (4); The outlet of reactor (11) connects purification recovery unit; The process furnace of described reactor (11) arranged outside is divided into the superpower process furnace (12) that is positioned at the first half and the mid power process furnace (13) that is positioned at Lower Half;
The material inlet of described coal e Foerderanlage (4) connects coal hopper (1), and the material inlet of biomass conveying (8) connects biomass hoppers (5).
2. a kind of integrated form two-step approach biomass according to claim 1 and coal copyrolysis device, is characterized in that: the bottom inlet of described reactor (11) is also connected to the outlet of cylinder (9) through being provided with the pipeline of gas preheater (10).
3. a kind of integrated form two-step approach biomass according to claim 2 and coal copyrolysis device, it is characterized in that: the entrance that the bottom of described reactor (11) connects gas preheater (10) is pre-hot gas entrance, and pre-hot gas entrance is three to 12, and is circumference uniform distribution.
4. a kind of integrated form two-step approach biomass according to claim 1 and coal copyrolysis device, is characterized in that: between described coal hopper (1) and coal e Foerderanlage (4), be in series with coal lock hopper (2) and coal sending cans (3).
5. a kind of integrated form two-step approach biomass according to claim 1 and coal copyrolysis device, is characterized in that: between described biomass hopper (5) and biomass conveying (8), be in series with biomass lock hopper (6) and biomass fermentation tank sending (7).
6. a kind of integrated form two-step approach biomass according to claim 1 and coal copyrolysis device, is characterized in that: described purification recovery unit comprises: tornado dust collector (15), semicoke holding tank (16), tar washing tower (17) and tar holding tank (18);
The pneumatic outlet of the gas inlet ligation device (11) of described tornado dust collector (15), tornado dust collector (15) pneumatic outlet connects tar washing tower (17), and the top of tar washing tower (17) offers pneumatic outlet; And tornado dust collector (15) are connected respectively semicoke holding tank (16) and tar holding tank (18) with the outlet at bottom of tar washing tower (17).
7. a kind of integrated form two-step approach biomass according to claim 1 and coal copyrolysis device, is characterized in that: described reactor (11) is integrated reformer.
8. a kind of integrated form two-step approach biomass according to claim 1 and coal copyrolysis device, it is characterized in that: the coal tremie pipe (14) of the top entrance of described coal e Foerderanlage (4) ligation device (11), and the middle part of coal tremie pipe (14) insertion reaction device (11).
9. a kind of integrated form two-step approach biomass according to claim 1 and coal copyrolysis device, is characterized in that: the ratio of the feeding rate of described reactor (11) bottom biomass and reactor (11) top coal is (95:5)～(50:50).
10. a kind of integrated form two-step approach biomass according to claim 1 and coal copyrolysis device, it is characterized in that: the pressure in described reactor (11) is 0.001-4.0MPa, the Heating temperature of first half superpower process furnace (12) is 400-800 DEG C, and the Heating temperature of Lower Half mid power process furnace (13) is 300-700 DEG C.
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Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107937006A (en) * | 2017-12-22 | 2018-04-20 | 北京神雾电力科技有限公司 | A kind of high temperature two-part pyrolysis reactor |
| CN109355074A (en) * | 2018-11-02 | 2019-02-19 | 武汉博立达农业科技发展有限公司 | Biomass and coal copyrolysis reactor |
| CN109355073A (en) * | 2018-11-02 | 2019-02-19 | 武汉博立达农业科技发展有限公司 | Biomass and coal copyrolysis reactor |
| CN109355070A (en) * | 2018-11-02 | 2019-02-19 | 武汉博立达农业科技发展有限公司 | Biomass and coal copyrolysis reactor |
| CN110713843A (en) * | 2019-10-14 | 2020-01-21 | 江苏海洋大学 | Coal and biomass co-pyrolysis reaction device and method |
-
2014
- 2014-07-16 CN CN201420393879.6U patent/CN203999499U/en active Active
Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107937006A (en) * | 2017-12-22 | 2018-04-20 | 北京神雾电力科技有限公司 | A kind of high temperature two-part pyrolysis reactor |
| CN109355074A (en) * | 2018-11-02 | 2019-02-19 | 武汉博立达农业科技发展有限公司 | Biomass and coal copyrolysis reactor |
| CN109355073A (en) * | 2018-11-02 | 2019-02-19 | 武汉博立达农业科技发展有限公司 | Biomass and coal copyrolysis reactor |
| CN109355070A (en) * | 2018-11-02 | 2019-02-19 | 武汉博立达农业科技发展有限公司 | Biomass and coal copyrolysis reactor |
| CN109355070B (en) * | 2018-11-02 | 2023-12-01 | 武汉兰多生物科技有限公司 | Biomass and coal co-pyrolysis reactor |
| CN109355074B (en) * | 2018-11-02 | 2023-12-01 | 武汉兰多生物科技有限公司 | Biomass and coal co-pyrolysis reactor |
| CN109355073B (en) * | 2018-11-02 | 2023-12-01 | 武汉兰多生物科技有限公司 | Biomass and coal co-pyrolysis reactor |
| CN110713843A (en) * | 2019-10-14 | 2020-01-21 | 江苏海洋大学 | Coal and biomass co-pyrolysis reaction device and method |
| CN110713843B (en) * | 2019-10-14 | 2021-05-11 | 江苏海洋大学 | Coal and biomass co-pyrolysis reaction device and method |
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