CN202576365U - Fluidized bed biomass and coal together gasified device - Google Patents
Fluidized bed biomass and coal together gasified device Download PDFInfo
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- CN202576365U CN202576365U CN2012201341141U CN201220134114U CN202576365U CN 202576365 U CN202576365 U CN 202576365U CN 2012201341141 U CN2012201341141 U CN 2012201341141U CN 201220134114 U CN201220134114 U CN 201220134114U CN 202576365 U CN202576365 U CN 202576365U
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- 239000002028 Biomass Substances 0.000 title claims abstract description 56
- 239000003245 coal Substances 0.000 title claims abstract description 33
- 238000002309 gasification Methods 0.000 claims abstract description 61
- 239000000428 dust Substances 0.000 claims abstract description 27
- 239000002893 slag Substances 0.000 claims abstract description 20
- 239000000463 material Substances 0.000 claims abstract description 12
- 239000007789 gas Substances 0.000 claims abstract description 11
- 239000002956 ash Substances 0.000 claims description 15
- 239000003034 coal gas Substances 0.000 claims description 12
- 239000012530 fluid Substances 0.000 claims description 12
- 238000009434 installation Methods 0.000 claims description 11
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 7
- 239000001301 oxygen Substances 0.000 claims description 7
- 229910052760 oxygen Inorganic materials 0.000 claims description 7
- 239000010881 fly ash Substances 0.000 claims description 6
- 238000000034 method Methods 0.000 claims description 6
- 239000000843 powder Substances 0.000 abstract description 6
- 238000011084 recovery Methods 0.000 abstract description 4
- 239000002918 waste heat Substances 0.000 abstract description 4
- 239000003795 chemical substances by application Substances 0.000 abstract description 2
- 239000011269 tar Substances 0.000 description 10
- 238000005336 cracking Methods 0.000 description 4
- 230000015572 biosynthetic process Effects 0.000 description 3
- 229910052799 carbon Inorganic materials 0.000 description 3
- 239000000470 constituent Substances 0.000 description 3
- 239000000839 emulsion Substances 0.000 description 3
- 238000005243 fluidization Methods 0.000 description 3
- 239000002737 fuel gas Substances 0.000 description 3
- 150000003254 radicals Chemical class 0.000 description 3
- 230000001932 seasonal effect Effects 0.000 description 3
- 239000000126 substance Substances 0.000 description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 3
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 2
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 239000001257 hydrogen Substances 0.000 description 2
- 229910052739 hydrogen Inorganic materials 0.000 description 2
- 238000006479 redox reaction Methods 0.000 description 2
- 239000002699 waste material Substances 0.000 description 2
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 description 1
- 229910052728 basic metal Inorganic materials 0.000 description 1
- 150000003818 basic metals Chemical class 0.000 description 1
- 238000009835 boiling Methods 0.000 description 1
- 239000003054 catalyst Substances 0.000 description 1
- 230000003197 catalytic effect Effects 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 239000011280 coal tar Substances 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 210000003608 fece Anatomy 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 230000005484 gravity Effects 0.000 description 1
- 238000005338 heat storage Methods 0.000 description 1
- 230000007774 longterm Effects 0.000 description 1
- 238000000465 moulding Methods 0.000 description 1
- 239000010815 organic waste Substances 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 238000007348 radical reaction Methods 0.000 description 1
- 238000010517 secondary reaction Methods 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 239000010902 straw Substances 0.000 description 1
- 230000009466 transformation Effects 0.000 description 1
- 239000002023 wood Substances 0.000 description 1
Images
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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
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
- Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
Landscapes
- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
Abstract
A fluidized bed biomass and coal together gasified device which comprises a charging system, a fluidized bed gasifier, a slag discharge system, a primary dedusting system, a waste heat recovery system and a moderate/depth dedusting system, wherein the charging system, the fluidized bed gasifier, the slag discharge system, the primary dedusting system, the waste heat recovery system and the moderate/depth dedusting system are connected in sequence; the charging system is communicated with a feed inlet of the fluidized bed gasifier, the bottom of the fluidized bed gasifier is connected with the slag discharge system, and a gas distributor is further arranged at the lower end of the fluidized bed gasifier; and a gas outlet at the upper end of the fluidized bed gasifier is connected with the primary dedusting system, the waste heat recovery system and the moderate/depth dedusting system in sequence, and a dust discharge outlet of the moderate/depth dedusting system is connected with a fine dust collection device. Due to the fact that biomass and coal have certain complementarity in gasification characteristics, and by means of the fluidized state principle, biomass powder and pulverized coal are continuously added into a gasifier dense-phase area, gasifying agent is blown in through the bottom of the gasifier, materials can be boiled and fluidized, and complete gasification of the biomass and the coal is finally achieved.
Description
Technical field
The utility model relates to a kind of biomass gasification device, is specifically related to a kind of biomass fluid bed and common gasification installation of coal.
Background technology
At present, China's energy expenditure is too relied on coal for counsel.The proportion of coal in China's primary energy source consumption has reached 69%, and new and renewable sources of energy proportion in China's energy consumption structure is low excessively, only reaches 9%, also has gap with world average level.Therefore, accelerating with water power, nuclear power, sun power, wind energy, Geothermal energy, sea energy, biomass energy etc. is the development of master's new forms of energy and renewable resources, is the strategic emphasis of China's Energy restructuring.
China's development biomass energy has great potential.According to statistics; About 600,000,000 tons of whole nation straw YO in recent years; Fuel wood YO (comprise timber felling waste) is about 200,000,000 tons, also has organic waste materials, the waste residue of a large amount of human and animal excretas and industrial discharge, and annual biomass resource total amount is amounted to into standard coal equivalent 2～400,000,000 ton.For a long time, the development and utilization of China's biomass energy is main with conventional combustion techniques, has developed technology such as gasifying biomass, liquefaction, curing molding now gradually.Wherein, gasifying biomass is a kind of principal mode that biomass clean utilizes, and has vast potential for future development.
The gasification process of biomass mainly contains gasification process such as fixed bed, fluidized-bed.The fixed bed of China's fuel gas with low heat value, biomass fluid bed gasification installation are succeeded in developing and are put goods on the market, and the characteristics of these gasification installations are that operation is fairly simple, but fuel gases calorific value is generally at 5MJ/m
3About, be still waiting to improve aspect tar processing and the operation steady in a long-term.In addition because the biomass calorific value is low, fugitive constituent is high, ash content is low etc. gasification property, when causing biomass fluid bed independent gasification service temperature low, produce that tar content is big, bed is difficult for problems generations such as foundation.Coal is compared with biomass, and coal has gasification properties such as calorific value height, fugitive constituent are low, ash content height.
Summary of the invention
The purpose of the utility model aims to provide a kind of biomass gasification device that can solve and produces low, the difficult removing of tar of fuel gases calorific value, especially solves biomass fluid bed gasification operation temperature biomass fluid bed and coal low, that produce problems such as tar content is big, the difficult foundation of bed and is total to gasification installation.
For achieving the above object, the utility model adopts technical scheme to be: comprise the charging system that links to each other successively, fluidized-bed gasification furnace, dreg removing system, elementary dust-removal system, WHRS and in/degree of depth dust-removal system;
Said charging system is connected with the feeding mouth of fluidized-bed gasification furnace, and the bottom of fluidized-bed gasification furnace links to each other with dreg removing system, and also is provided with the gas distributor that links to each other with oxygen enrichment or oxygen pipeline and vapour line in the fluidized-bed gasification furnace lower end;
The pneumatic outlet of described fluidized-bed gasification furnace upper end successively with elementary dust-removal system, in/degree of depth dust-removal system links to each other, in/outlet of degree of depth dust-removal system links to each other with the coal gas collection device.
Described charging system comprises feed bin, material lock, load hopper and the screw feeder that links to each other successively, and the output terminal of screw feeder links to each other with the feeding mouth of fluidized-bed gasification furnace.
Described dreg removing system comprise be connected successively receive slag bucket, slag lock and barrel slag cooler, be connected with the bottom of fluidized-bed gasification furnace by slag bucket.
Described elementary fly-ash separator comprises one-level tornado dust collector and the second cyclone dust extractor that links to each other successively; The inlet of one-level tornado dust collector links to each other with the pneumatic outlet of fluidized-bed gasification furnace, and the semicoke that separates through the I and II tornado dust collector returns fluidized-bed gasification furnace through the returning charge dipleg of I and II cyclonic separator respectively.
Described WHRS comprises vapour generator, vapor superheater and feedwater preheater, and wherein the inlet of vapour generator links to each other with the pneumatic outlet of second cyclone dust extractor.
In described/degree of depth fly-ash separator comprises successively circumfluent cyclone and the sack cleaner that links to each other; Wherein the inlet of circumfluent cyclone links to each other with the outlet of feedwater preheater; The lower end of circumfluent cyclone is provided with ash bucket No. one; The outlet of sack cleaner links to each other with the coal gas collection device, and the lower end of sack cleaner also is provided with ash bucket No. two.
The utility model has certain complementarity according to biomass and coal on gasification property; Utilize the fluidized principle; Biomass powder and fine coal are added the vapourizing furnace emulsion zone continuously, and vaporized chemical (pure oxygen or oxygen enrichment, steam) is blown into from the vapourizing furnace bottom, makes material boiling fluidisation.Under the hot conditions that burning produces, broken sticking, devolatilization, the cracking of tar, the redox reaction of carbon take place in two thorough mixing contacts of gas-solid, finally realize being gasified totally of biomass and coal.
The utility model increases secondary air at fluidized-bed gasification furnace and drops into facility (vapourizing furnace emulsion zone top).Because biomass volatile content high (accounting for 70%), after biomass are admitted to vapourizing furnace, have a large amount of fugitive constituents to separate out and rise rapidly, so the flame of centre district will on move; Simultaneously, be entrained to freeboard of fluidized bed from emulsion zone easily, increase the secondary reaction that secondary air implements to help material because biological particles density is little, can reduce again dust (tar) after move, carry the high-carbon transformation efficiency.
Description of drawings
Fig. 1 is an one-piece construction synoptic diagram of the present invention.
The 1-feed bin; 2-expects lock; The 3-load hopper; The 4-screw feeder; The 5-fluidized-bed gasification furnace; 6-level tornado dust collector; The 7-second cyclone dust extractor; The 8-vapour generator; The 9-vapor superheater; The 10-feedwater preheater; The 11-circumfluent cyclone; The 12-sack cleaner; 13-receives slag bucket; 14-slag lock; The 15-barrel slag cooler; 16-1
#Ash bucket; 17-2
#Ash bucket
Embodiment
Below in conjunction with accompanying drawing the structural principle and the principle of work of the utility model are done further explain.
Referring to Fig. 1, the utility model comprise successively the charging system that links to each other, fluidized-bed gasification furnace, dreg removing system, elementary dust-removal system, WHRS and in/degree of depth dust-removal system;
Said charging system comprises feed bin 1, material lock 2, load hopper 3 and the screw feeder 4 that links to each other successively; The output terminal of screw feeder 4 links to each other with the feeding mouth of fluidized-bed gasification furnace 5; The bottom of fluidized-bed gasification furnace 5 links to each other with dreg removing system; Described dreg removing system comprise be connected successively receive slag bucket 13, slag lock 14 and barrel slag cooler 15, and also be provided with the gas distributor that links to each other with oxygen enrichment or oxygen pipeline and vapour line in fluidized-bed gasification furnace 5 lower ends;
Described elementary fly-ash separator comprises the one-level tornado dust collector 6 and second cyclone dust extractor 7 that link to each other successively; The inlet of one-level tornado dust collector 6 links to each other with the pneumatic outlet of fluidized-bed gasification furnace 5, and the semicoke that separates through I and II tornado dust collector 6,7 returns fluidized-bed gasification furnace 5 through the returning charge dipleg of I and II cyclonic separator 6,7 respectively;
Described WHRS comprises vapour generator 8, vapor superheater 9 and feedwater preheater 10, and wherein the inlet of vapour generator 8 links to each other with the pneumatic outlet of second cyclone dust extractor 7;
In described/degree of depth fly-ash separator comprises successively the circumfluent cyclone 11 and sack cleaner 12 that links to each other; Wherein the inlet of circumfluent cyclone 11 links to each other with the outlet of feedwater preheater 10; The lower end of circumfluent cyclone 11 is provided with ash bucket 16 No. one; The outlet of sack cleaner 12 links to each other with the coal gas collection device, and the lower end of sack cleaner 12 also is provided with ash bucket 17 No. two.
The utility model biomass and fluidized bed altogether gasification process are as follows: at first with granularity less than 10mm; Water cut less than the biomass powder of 5wt% and granularity less than 6mm; Water cut mixes and delivers to feed bin 1 by a certain percentage less than the fine coal of 5wt%; Material in the feed bin gets into load hoppers 3 through material lock 2, and it is that 950-1000 ℃, pressure are in the fluidized-bed gasification furnace 5 of 0.05-1.0MPa that the material in the load hopper 3 gets into temperature through screw feeder 4 and feed gravity pipe; Vaporized chemical gets into the vapourizing furnace bottom through gas distributor makes biomass powder and fine coal that broken sticking, devolatilization, the cracking of tar, the redox reaction of carbon take place under fluidized state, and generation coal gas gasifies; The scum pipe of lime-ash through the vapourizing furnace bottom enters and receives slag bucket 13 and slag lock 14, is cooled to discharge below 80 ℃ through barrel slag cooler 15 again; The about 950 ℃ of dust-laden coal gas that generate get into one-level tornado dust collector 6 respectively by the vapourizing furnace top to carry out elementary dedusting with second cyclone dust extractor 7 (dust content of gas is about 50g/m
3), the semicoke that separates through one-level tornado dust collector 6 and second cyclone dust extractor 7 returns vapourizing furnace through the returning charge dipleg of I and II cyclonic separator respectively and further burns, gasifies; Coal gas gets into vapor superheater 9 and feedwater preheater 10 then and continues recovery coal gas waste heat through getting into vapour generator 8 after the elementary dedusting and producing saturation steam, makes gas temperature reduce to 220 ℃; (dust content of gas is about 4g/m through circumfluent cyclone 11 moderate dedustings to go out the coal gas of feedwater preheater
3); The fine powder that separates enters 1# ash bucket 16 backs and discharges, collects; Coal gas gets into degree of depth dedusting in the sack cleaner again after circumfluent cyclone 11 dedustings, the fine powder that separates enters 2# ash bucket 17 backs and discharges, collects, and finally makes dust content of gas reach 5mg/m
3Below, get into follow-up system.
The advantage of the utility model is following:
1, produces synergy
Coal and biomass gasify altogether at first and in the Wooden Biomass organic substance, in the most weak covalent linkage thermo-cracking to take place, and the volatile matter of formation is decomposed to form a lot of radicals, and these radicals have increased the oxygenolysis of coal; Wooden Biomass is rich hydrogen material, and hydrogen that produces in the devolatilization process and coal free radical reaction have stoped the burnt formation of secondary; Basic metal in the Wooden Biomass is the effective catalyst of gasification, has promoted the catalytic gasification reaction of coal.
2, improve gasification temperature
Because the coal calorific value is high, gasification temperature can reach more than 1000 ℃, so contains tar hardly in the coal gas.And the biomass calorific value is low, 700～750 ℃ of gasification temperatures, and the coal-tar middle oil content of coal gas is high, and this is a gasifying biomass problem anxious to be solved.With the gasification altogether in fluidized-bed of biomass and coal, can the formation temperature higher stable bed of material, not only can guarantee stablely, and under the effect of steam gasification agent, can quicken the thermo-cracking of tar, tar content is reduced, caloric power of gas improves.
3, helping bed sets up
Biomass ash content is little, carries out fluidized-bed gasification separately and is difficult to form bed, and fluidization characteristic is relatively poor.Biomass and fluidized bed gasification altogether; Coal can form the stable dense-phase bed of fluidized gasification as the fluidization media of biomass, and the dense-phase bed heat storage capacity is big; And heat and mass is violent in the bed, can stable gasification temperature (900～1000 ℃) be provided for the low-calorie biomass of high-moisture.
4, solve the seasonal problem of biomass supply
Biomass are owing to influenced by seasonal factor, and supply is unstable, and biomass and coal gasify altogether and can solve the seasonal problem of biomass supply.When biomass resource enriches, can improve the ratio row of biomass, and when biomass resource is under-supply, can improve the ratio row of coal, can reduce the business risk of biomass industrial utilization.
Claims (6)
1. biomass fluid bed and coal gasification installation altogether is characterized in that: comprise the charging system that links to each other successively, fluidized-bed gasification furnace, dreg removing system, elementary dust-removal system, WHRS and in/degree of depth dust-removal system;
Said charging system is connected with the feeding mouth of fluidized-bed gasification furnace (5), and the bottom of fluidized-bed gasification furnace (5) links to each other with dreg removing system, and also is provided with the gas distributor that links to each other with oxygen enrichment or oxygen pipeline and vapour line in fluidized-bed gasification furnace (5) lower end;
The pneumatic outlet of described fluidized-bed gasification furnace (5) upper end successively with elementary dust-removal system, WHRS and in/degree of depth dust-removal system links to each other, in/ash discharge of degree of depth dust-removal system exports and links to each other with thin grey collection device.
2. the biomass fluid bed and common gasification installation of coal according to claim 1; It is characterized in that: described charging system comprises feed bin (1), material lock (2), load hopper (3) and the screw feeder (4) that links to each other successively, and the output terminal of screw feeder (4) links to each other with the feeding mouth of fluidized-bed gasification furnace (5).
3. the biomass fluid bed and common gasification installation of coal according to claim 1; It is characterized in that: described dreg removing system comprise be connected successively receive slag bucket (13), slag lock (14) and barrel slag cooler (15), be connected with the bottom of fluidized-bed gasification furnace (5) by slag bucket (13).
4. the biomass fluid bed and common gasification installation of coal according to claim 1; It is characterized in that: described elementary fly-ash separator comprises one-level tornado dust collector (6) and the second cyclone dust extractor (7) that links to each other successively; The inlet of one-level tornado dust collector (6) links to each other with the pneumatic outlet of fluidized-bed gasification furnace (5), and the returning charge dipleg that the semicoke that process I and II tornado dust collector (6), (7) separate passes through I and II cyclonic separator (6), (7) respectively returns fluidized-bed gasification furnace (5).
5. the biomass fluid bed and common gasification installation of coal according to claim 1; It is characterized in that: described WHRS comprises vapour generator (8), vapor superheater (9) and feedwater preheater (10), and wherein the inlet of vapour generator (8) links to each other with the pneumatic outlet of second cyclone dust extractor (7).
6. the biomass fluid bed and common gasification installation of coal according to claim 5; It is characterized in that: in described/degree of depth fly-ash separator comprises successively circumfluent cyclone (11) and the sack cleaner (12) that links to each other; Wherein the inlet of circumfluent cyclone (11) links to each other with the outlet of feedwater preheater (10); The lower end of circumfluent cyclone (11) is provided with an ash bucket (16); The outlet of sack cleaner (12) links to each other with the coal gas collection device, and the lower end of sack cleaner (12) also is provided with No. two ash buckets (17).
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| Application Number | Priority Date | Filing Date | Title |
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| CN2012201341141U CN202576365U (en) | 2012-04-01 | 2012-04-01 | Fluidized bed biomass and coal together gasified device |
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| Application Number | Priority Date | Filing Date | Title |
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| CN2012201341141U CN202576365U (en) | 2012-04-01 | 2012-04-01 | Fluidized bed biomass and coal together gasified device |
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Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105132039A (en) * | 2015-08-14 | 2015-12-09 | 新奥科技发展有限公司 | Fluidized-bed fly ash back-to- furnace gasification apparatus and method |
| CN106010660A (en) * | 2016-05-13 | 2016-10-12 | 北京航天动力研究所 | Dry slag gasification device and method |
| CN108373934A (en) * | 2018-05-18 | 2018-08-07 | 华北电力大学（保定） | Multiple types Biomass Gasification in Circulating Fluidized Bed reactor and its gasification process |
| CN108753367A (en) * | 2018-07-25 | 2018-11-06 | 上海正申建设工程有限公司 | A kind of the fluid bed powder coal gasification device and technique of flying dust zero-emission |
| CN109679695A (en) * | 2018-12-05 | 2019-04-26 | 新地能源工程技术有限公司 | A kind of gasification of biomass Poly-generation charcoal thermoelectric device and technique |
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-
2012
- 2012-04-01 CN CN2012201341141U patent/CN202576365U/en not_active Expired - Lifetime
Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105132039A (en) * | 2015-08-14 | 2015-12-09 | 新奥科技发展有限公司 | Fluidized-bed fly ash back-to- furnace gasification apparatus and method |
| CN105132039B (en) * | 2015-08-14 | 2018-01-12 | 新奥科技发展有限公司 | CFB fly ash returns furnace gas device and method |
| CN106010660A (en) * | 2016-05-13 | 2016-10-12 | 北京航天动力研究所 | Dry slag gasification device and method |
| CN108373934A (en) * | 2018-05-18 | 2018-08-07 | 华北电力大学（保定） | Multiple types Biomass Gasification in Circulating Fluidized Bed reactor and its gasification process |
| CN108753367A (en) * | 2018-07-25 | 2018-11-06 | 上海正申建设工程有限公司 | A kind of the fluid bed powder coal gasification device and technique of flying dust zero-emission |
| CN109679695A (en) * | 2018-12-05 | 2019-04-26 | 新地能源工程技术有限公司 | A kind of gasification of biomass Poly-generation charcoal thermoelectric device and technique |
| CN109679695B (en) * | 2018-12-05 | 2024-02-06 | 新地能源工程技术有限公司 | Biomass gasification poly-generation carbon thermoelectric device and process |
| CN110714251A (en) * | 2019-08-29 | 2020-01-21 | 郑州市君芝友纺织品有限公司 | Yarn for antibacterial fabric, and manufacturing method and special equipment thereof |
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| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| PE01 | Entry into force of the registration of the contract for pledge of patent right |
Denomination of utility model: Fluidized bed biomass and coal together gasified device Effective date of registration: 20140103 Granted publication date: 20121205 Pledgee: Commercial Bank of China Limited by Share Ltd Xi'an branch Pledgor: Shaanxi Huaxiang Energy Technology Group Co., Ltd. Registration number: 2013610000005 |
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Denomination of utility model: Fluidized bed biomass and coal together gasified device Effective date of registration: 20140103 Granted publication date: 20121205 Pledgee: Commercial Bank of China Limited by Share Ltd Xi'an branch Pledgor: Shaanxi Huaxiang Energy Technology Group Co., Ltd. Registration number: 2013610000005 |
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Denomination of utility model: Fluidized bed biomass and coal together gasified device Effective date of registration: 20150618 Granted publication date: 20121205 Pledgee: Commercial Bank of China Limited by Share Ltd Xi'an branch Pledgor: Shaanxi Huaxiang Energy Technology Group Co., Ltd. Registration number: 2015610000008 |
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Denomination of utility model: Fluidized bed biomass and coal together gasified device Effective date of registration: 20180126 Granted publication date: 20121205 Pledgee: Shaanxi Qin Nong rural commercial bank Limited by Share Ltd science and Technology Road Branch Pledgor: Shaanxi Huaxiang Energy Technology Group Co., Ltd. Registration number: 2018610000014 |
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