CN103013584A - Purification method of biomass flash pyrolysis tail gas and device thereof - Google Patents
Purification method of biomass flash pyrolysis tail gas and device thereof Download PDFInfo
- Publication number
- CN103013584A CN103013584A CN2012105929602A CN201210592960A CN103013584A CN 103013584 A CN103013584 A CN 103013584A CN 2012105929602 A CN2012105929602 A CN 2012105929602A CN 201210592960 A CN201210592960 A CN 201210592960A CN 103013584 A CN103013584 A CN 103013584A
- Authority
- CN
- China
- Prior art keywords
- gas
- pyrolysis
- tail gas
- adsorption
- tar
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
Images
Classifications
-
- 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
- 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
Landscapes
- Industrial Gases (AREA)
Abstract
The invention relates to a purification method of biomass flash pyrolysis tail gas and a device thereof, and belongs to the technical field of biomass recycling and energy equipment thereof. According to the device disclosed by the invention, an adsorption type device and an electrical tar precipitator are used for carrying out combined decoking and impurity-removing on the biomass flash pyrolysis tail gas; a gas-liquid separator is used simultaneously; the structure is simple and the energy consumption is low; a secondary pollution problem caused by wastewater generated in wet-method decoking is avoided; an adsorption tower of the device is internally provided with a reciprocated channel to form three layers of adsorption beds; and by-product pyrolysis carbon generated by flash pyrolysis is used as an adsorbent to realize the comprehensive coproduction application of a pyrolysis product. With the adoption of the method and the device thereof, the pyrolysis tail gas is purified to obviously reduce the content of impurities in the pyrolysis tail gas, such as tar, dust, water and the like, so that the resource utilization quality of the pyrolysis tail gas is improved.
Description
Technical field
The present invention relates to a kind of purifying method and device thereof of biomass fast pyrogenation tail gas, belong to biomass regeneration and energy equipment technical field thereof.
Background technology
In numerous renewable energy sources, biomass energy is unique a kind of mineral fuel attribute that both had, have again can store, transport, regenerate, the characteristics such as conversion, and be subjected to the energy of natural condition less-restrictive.As a kind of green regenerative energy sources, its status in the energy structure system is more and more important.The rapidly pyrolysing and liquefying biomass technology can be converted to the biomass of low energy densities bio oil and other energy product of higher-grade, high-energy-density, to produce fuel or Chemicals, has very large development potentiality and wide application prospect.
The product of rapidly pyrolysing and liquefying biomass has three kinds in solid-state coke, liquid bio oil and pyrolysis tail gas (not condensible gas).Wherein the main component of pyrolysis tail gas comprises CO, CO
2, H
2, CH
4Deng, have certain calorific value, can be the pyrolysis system recycle as fuel gas buring or as circulating carried with it, to realize the efficient utilization of pyrolysis tail gas, energy-conserving and environment-protective.
Yet in the tail gas that fast pyrogenation produces, water ratio is higher, and can contain the impurity such as a certain amount of dust, tar, has had a strong impact on burning and the efficient utilization of circulation of pyrolysis tail gas.The tar that particularly contains in the pyrolysis tail gas, it condenses into liquid at low temperatures, and the dust such as Yi Heshui, carbon granules are combined into dope, stop up gas pipe line, valve and blower fan, have affected normal operation and the safety of system.Simultaneously, the small droplets tar that contains in the pyrolysis tail gas is difficult for after-flame, easily produces the particles such as carbon black during burning, adds the existence of moisture, the thermal transition efficient in the time of can reducing exhaust combustion.Thus, must carry out purifying treatment to the dust in the biomass fast pyrogenation tail gas, tar and water etc.
At present, the purifying method of the impurity such as dust, tar mainly contains following several in the biomass fast pyrogenation tail gas: (1) wet method (WATER-WASHING METHOD): this method is simple, the tar removal efficiency is high, but the washing water consumption is large, can cause the waste of water resources, and the sewage after the washing easily causes secondary pollution to environment.(2) dry method (absorption method): this method has solved the secondary pollution problem of tar washing water, and equipment is simple.But its pressure-losses is larger, and macrobead easily results in blockage, and the filter material life-span is short, normal and other decoking impurity-removing method coupling.(3) electric method of trapping: this method especially has good separation efficiency to 0.01-1 μ m tar ash grit, has a drag losses little, the advantage that the gas processing amount is large, but need consider coke cleaning and Explosion-Proof in actual applications.
Summary of the invention
The object of the invention is to propose a kind of purifying method and device thereof of biomass fast pyrogenation tail gas, advantage in conjunction with adsorption process and static decoking, remove simultaneously moisture contained in the biomass fast pyrogenation tail gas, solve the tar blockage problem by stage purification, realize that the circulation of pyrolysis tail gas efficiently utilizes.
The purifying method of the biomass fast pyrogenation tail gas that the present invention proposes may further comprise the steps:
(1) biomass material is ground into particle diameter less than 2 millimeters particle, makes granular material carry out pyrolytic reaction under 450 ℃～600 ℃, the reaction times is 0.5～2.5 second;
(2) the high temperature pyrolysis gas that above-mentioned reaction is obtained carries out gas solid separation, separates pyrolytic carbon wherein;
(3) above-mentioned high temperature pyrolysis gas through carbon removal is carried out condensation, after the condensation, condensable gases wherein becomes liquid bio oil collects, and making condensed pyrolysis exhaust temperature is 35 ℃～60 ℃;
(4) above-mentioned condensed not condensable gases is carried out the static decoking, make to purify the rear coal-tar middle oil content≤40mg/Nm of pyrolysis tail gas
3
(5 remove defocused not condensable gases with above-mentioned static adsorbs the decoking removal of impurities, makes the tar content≤15mg/Nm in the pyrolysis tail gas
3
(6) the not condensable gases that step (5) is obtained is carried out gas-liquid separation, removes the moisture in the pyrolysis tail gas, makes the dew point of water in the pyrolysis tail gas≤-8 ℃;
(7) the purification pyrolysis tail gas that step (6) is obtained is drawn, as combustion gas.
The refining plant of the biomass fast pyrogenation tail gas that the present invention proposes comprises:
Pyrolysis reactor is used for making material carry out pyrolytic reaction under 450 ℃～600 ℃, and the bottom, left side of pyrolysis reactor is provided with opening for feed, and the upper gas outlet links to each other with the entrance of gas-solid separator;
Gas-solid separator, be used for pyrolysis reactor high temperature pyrolysis gas is out carried out gas solid separation, remove the particulate state pyrolytic carbon that carries in the pyrolysis gas, the gas-solid separator bottom is provided with ash discharging hole, and the pneumatic outlet of gas-solid separator links to each other with the left side lower inlet of condenser;
Condenser, be used for the high temperature pyrolysis gas through carbon removal is carried out condensation, after the condensation, condensable gases wherein becomes liquid bio oil and collects, making condensed pyrolysis exhaust temperature is 35 ℃～60 ℃, condenser is provided with air outlet, top and bottom discharge mouth, and the air outlet, top links to each other with electrical tar precipitator left side lower inlet, and the bottom discharge mouth discharges the bio oil that condensation obtains to collect;
Electrical tar precipitator is used for above-mentioned condensed not condensable gases is carried out the static decoking, makes to purify the rear coal-tar middle oil content≤40mg/Nm of pyrolysis tail gas
3, the outlet of electrical tar precipitator left upper portion links to each other with adsorption tower left side lower inlet, is used for the contained tar of pyrolysis tail gas is captured;
Adsorption tower is used for above-mentioned static is adsorbed decoking except defocused not condensable gases, makes the tar content≤15mg/Nm in the pyrolysis tail gas
3, the adsorption tower top exit links to each other with the tangential inlet of gas-liquid separator left upper portion;
Gas-liquid separator is used for above-mentioned absorption is carried out gas-liquid separation except defocused not condensable gases, removes the moisture in the pyrolysis tail gas, make the dew point of water in the pyrolysis tail gas≤-8 ℃, the gas-liquid separator bottom is provided with leakage fluid dram, and the top is provided with the air outlet, and the air outlet links to each other with the roots blower inlet mouth;
Roots blower is used for purifying pyrolysis tail gas and draws, as combustion gas.
Purifying method and the device thereof of the biomass fast pyrogenation tail gas that the present invention proposes, adopt adsorption type device and electrical tar precipitator that biomass fast pyrogenation tail gas is united the decoking removal of impurities, be aided with simultaneously gas-liquid separator, simple in structure, energy consumption is low, the secondary pollution problem that the waste water of having avoided producing in the wet method decoking brings; Reciprocating type passage is set in the adsorption tower, forms 3 layers of adsorption bed, and the by product pyrolytic carbon that adopts fast pyrogenation self generation realizes that as sorbent material the comprehensive coproduction of pyrolysis product is used.Adopt method of the present invention and device thereof, pyrolysis tail gas is purified, realized the remarkable minimizing of the foreign matter contents such as pyrolysis tail gas is coal-tar middle oil, dust, moisture, improved the recycling quality of pyrolysis tail gas.
Description of drawings
Fig. 1 is the structural representation of the biomass fast pyrogenation exhaust gas cleaner that proposes of the present invention.
Fig. 2 is the structural representation of adsorption tower in the refining plant of the present invention.
Among Fig. 1, the 1st, pyrolysis reactor, the 2nd, gas-solid separator, the 3rd, condenser, the 4th, electrical tar precipitator, the 5th, adsorption tower, the 6th, gas-liquid separator, the 7th, roots blower.Among Fig. 2,5-1 is the first adsorption bed, and 5-2 is the second adsorption bed, and 5-3 is the 3rd adsorption bed.
Embodiment
The purifying method of the biomass fast pyrogenation tail gas that the present invention proposes may further comprise the steps:
(1) biomass material is ground into particle diameter less than 2 millimeters particle, makes granular material carry out pyrolytic reaction under 450 ℃～600 ℃, the reaction times is 0.5～2.5 second; Wherein, biomass material can be timber, agricultural crop straw, bamboo wood etc.;
(2) the high temperature pyrolysis gas that above-mentioned reaction is obtained carries out gas solid separation, separates pyrolytic carbon wherein;
(3) above-mentioned high temperature pyrolysis gas through carbon removal is carried out condensation, after the condensation, condensable gases wherein becomes liquid bio oil collects, and cooling medium can be water or thermal oil, and making condensed pyrolysis exhaust temperature is 35 ℃～60 ℃;
(4) above-mentioned condensed not condensable gases is carried out the static decoking, make to purify the rear coal-tar middle oil content≤40mg/Nm of pyrolysis tail gas
3
(5 remove defocused not condensable gases with above-mentioned static adsorbs the decoking removal of impurities, makes the tar content≤15mg/Nm in the pyrolysis tail gas
3
(6) the not condensable gases that step (5) is obtained is carried out gas-liquid separator, removes the moisture in the pyrolysis tail gas, makes the dew point of water in the pyrolysis tail gas≤-8 ℃;
(7) the purification pyrolysis tail gas that step (6) is obtained is drawn, as combustion gas.
The refining plant of the biomass fast pyrogenation tail gas that the present invention proposes, its structure comprises as shown in Figure 1:
Pyrolysis reactor 1 is used for making material carry out pyrolytic reaction under 450 ℃～600 ℃, and the bottom, left side of pyrolysis reactor is provided with opening for feed, and the upper gas outlet links to each other with the entrance of gas-solid separator;
Gas-solid separator 2, be used for pyrolysis reactor high temperature pyrolysis gas is out carried out gas solid separation, remove the particulate state pyrolytic carbon that carries in the pyrolysis gas, the gas-solid separator bottom is provided with ash discharging hole, and the pneumatic outlet of gas-solid separator links to each other with the left side lower inlet of condenser;
Condenser 3, be used for the high temperature pyrolysis gas through carbon removal is carried out condensation, after the condensation, condensable gases wherein becomes liquid bio oil and collects, cooling medium can be water or thermal oil, and making condensed pyrolysis exhaust temperature is 35 ℃～60 ℃, and condenser is provided with air outlet, top and bottom discharge mouth, the air outlet, top links to each other with electrical tar precipitator left side lower inlet, and the bottom discharge mouth discharges the bio oil that condensation obtains to collect;
Electrical tar precipitator 4, be used for above-mentioned condensed not condensable gases is carried out the static decoking, voltage is 30-60KV, gas flow rate 0.6-2.0 meter per second, residence time 3-10 second in the electrical tar precipitator, the purification efficiency of pyrolysis tail gas makes to purify the rear coal-tar middle oil content≤40mg/Nm of pyrolysis tail gas as 80-90% after electric fishing integrates
3, the outlet of electrical tar precipitator left upper portion links to each other with adsorption tower left side lower inlet, is used for the contained tar of pyrolysis tail gas is captured;
Gas-liquid separator 6, be used for above-mentioned absorption is carried out gas-liquid separation except defocused not condensable gases, remove the moisture in the pyrolysis tail gas, the gas-liquid separator working pressure range is 0.02-0.2MPa, through gas-liquid separation, make the dew point of water in the pyrolysis tail gas≤-8 ℃, the gas-liquid separator bottom is provided with leakage fluid dram, the top is provided with the air outlet, and the air outlet links to each other with the roots blower inlet mouth;
Roots blower 7 is used for purifying pyrolysis tail gas and draws, and as fuel gas buring or circulating carried pyrolysis system is carried out heat supply.。
In one embodiment of the present of invention, adopt following parameter to realize:
(1) biomass material fast pyrogenation: the temperature of pyrolysis reactor 1 is 450-600 ℃, and reaction times 0.5-2.5 second, wherein, the biomass material particle diameter can be timber, agricultural crop straw, bamboo wood etc. less than 2mm;
(2) gas solid separation carbon removal: the high temperature pyrolysis gas that above-mentioned reaction is obtained carries out gas solid separation, gas-solid separator 2 separation efficiency 85-95%;
(3) pyrolysis gas condensation: make above-mentioned high temperature pyrolysis air cooling through carbon removal solidifying, condensable gases becomes liquid bio oil and collects after the condensation, and cooling medium can be water, thermal oil, makes that the pyrolysis exhaust temperature is 35-60 ℃ after the condensation;
(4) static decoking: make pyrolysis tail gas obtained above carry out the static decoking, voltage is 30-60KV, gas flow rate 0.6-2.0 meter per second, residence time 3-10 second in the electrical tar precipitator 4, the purification efficiency of pyrolysis tail gas makes to purify rear pyrolysis tail gas tar content≤40mg/Nm as 80-90% after electric fishing integrates
3
(5) adsorption-edulcoration: pyrolysis tail gas obtained above is sent into adsorption tower 5 further decoking removal of impurities, the first adsorption bed 5-1 sorbent material is corn cob, sawdust, the sorbent material of the second adsorption bed 5-2 is steel wire fibre ball, iron filings, the sorbent material of the 3rd adsorption bed 5-3 is the pyrolytic carbon that gas solid separation obtains in the inventive method, every layer of height of bed is 200-300mm, gas flow rate is the 0.4-1.2 meter per second in the tower, after adsorption filtration, and the tar content≤15mg/Nm in the pyrolysis tail gas
3
(6) gas-liquid separation: pyrolysis tail gas obtained above is sent into centrifugal gas-liquid separator 6, remove the moisture in the pyrolysis tail gas, the gas-liquid separator working pressure range is 0.02-0.2MPa, through gas-liquid separation, makes the dew point of water in the condensable gases not≤-8 ℃;
(7) purification pyrolysis tail gas obtained above is drawn by roots blower 7, as fuel gas buring or circulating carried pyrolysis system is carried out heat supply.
The operating process of one embodiment of the present of invention is as follows:
The temperature that pyrolysis reactor 1 is set is 500 ℃, opens heating system pyrolysis reactor 1 is preheated.To respectively connect valve open in the system pipeline, open roots blower 7, open simultaneously recycle pump and the external cooling medium circulation line of condenser 3, the operation condenser system.Start electrical tar precipitator, connect high-voltage power supply, slowly boost to 40KV.When treating that fast pyrolysis reactor 1 internal temperature reaches 500 ℃, will pulverize dried poplar wood powder and be transported in the pyrolysis reactor 1, carry out pyrolytic reaction.The high temperature pyrolysis pneumatic transmission that subsequently pyrolytic reaction is obtained enters gas-solid separator 2 and carries out gas solid separation, separates the pyrolytic carbon that obtains and collects, and pyrolysis gas carries out condensation by condenser 3, obtains the liquid product bio oil.Pyrolysis tail gas is sent into electrical tar precipitator 4 and is carried out the static decoking, pyrolysis tail gas behind the electric fishing collection carries out multistage adsorption filtration by adsorption tower 5, and the adsorption material agent is that sorbent material is that sorbent material is pyrolytic carbon among steel wire fibre ball, the 3rd adsorption bed 5-3 among corn cob, the second adsorption bed 5-2 among adsorption tower 5 interior the first adsorption bed 5-1.The pyrolysis tail gas of adsorption filtration is sent into gas-liquid separator 6 remove moisture, final purification tail gas is drawn by roots blower 7.After raw material all enters and reacts completely, close heating system.When pyrolysis reactor 1 temperature drops to below 100 ℃, close condenser 3 recycle systems, electrical tar precipitator 4 out of service.When pyrolysis reactor 1 interior temperature drops to below 50 ℃, close roots blower 7, end-of-job.By stage purification, the coal-tar middle oil content of pyrolysis tail gas is 11mg/Nm
3, the water dew point temperature is-10 ℃ in the pyrolysis tail gas.
Among the embodiment of apparatus of the present invention, the pyrolysis reactor model of using is BL-SCFB-6, and by Beijing Forestry University's design, Beijing clock rising sun Rui Kang Science and Technology Ltd. produces.The gas-solid separator model of using is BL-CYS-6, and by Beijing Forestry University's design, Beijing clock rising sun Rui Kang Science and Technology Ltd. produces.The condenser model of using is BL-CDS-6, and by Beijing Forestry University's design, Beijing clock rising sun Rui Kang Science and Technology Ltd. produces.The electrical tar precipitator model of using is FD22, produces by rising mechanical company limited in Zibo.The adsorption tower model of using is BLASPT-6, and by being designed by Beijing Forestry University, Beijing clock rising sun Rui Kang Science and Technology Ltd. produces.The gas-liquid separator model of using is YJQY, sells company limited by the auspicious bright glass reinforced plastic in Hengshui and produces.The roots blower model of using is SR65, is produced by Zhangqiu City's roots blower company limited.
Claims (4)
1. the purifying method of a biomass fast pyrogenation tail gas is characterized in that the method may further comprise the steps:
(1) biomass material is ground into particle diameter less than 2 millimeters particle, makes granular material carry out pyrolytic reaction under 450 ℃～600 ℃, the reaction times is 0.5～2.5 second;
(2) the high temperature pyrolysis gas that above-mentioned reaction is obtained carries out gas solid separation, separates pyrolytic carbon wherein;
(3) above-mentioned high temperature pyrolysis gas through carbon removal is carried out condensation, after the condensation, condensable gases wherein becomes liquid bio oil collects, and making condensed pyrolysis exhaust temperature is 35 ℃～60 ℃;
(4) above-mentioned condensed not condensable gases is carried out the static decoking, make to purify the rear coal-tar middle oil content≤40mg/Nm of pyrolysis tail gas
3
(5 remove defocused not condensable gases with above-mentioned static adsorbs the decoking removal of impurities, makes the tar content≤15mg/Nm in the pyrolysis tail gas
3
(6) the not condensable gases that step (5) is obtained is carried out gas-liquid separation, removes the moisture in the pyrolysis tail gas, makes the dew point of water in the pyrolysis tail gas≤-8 ℃;
(7) the purification pyrolysis tail gas that step (6) is obtained is drawn, as combustion gas.
2. the refining plant of a biomass fast pyrogenation tail gas is characterized in that this device comprises:
Pyrolysis reactor is used for making material carry out pyrolytic reaction under 450 ℃～600 ℃, and the bottom, left side of pyrolysis reactor is provided with opening for feed, and the upper gas outlet links to each other with the entrance of gas-solid separator;
Gas-solid separator, be used for pyrolysis reactor high temperature pyrolysis gas is out carried out gas solid separation, remove the particulate state pyrolytic carbon that carries in the pyrolysis gas, the gas-solid separator bottom is provided with ash discharging hole, and the pneumatic outlet of gas-solid separator links to each other with the left side lower inlet of condenser;
Condenser, be used for the high temperature pyrolysis gas through carbon removal is carried out condensation, after the condensation, condensable gases wherein becomes liquid bio oil and collects, making condensed pyrolysis exhaust temperature is 35 ℃～60 ℃, condenser is provided with air outlet, top and bottom discharge mouth, and the air outlet, top links to each other with electrical tar precipitator left side lower inlet, and the bottom discharge mouth discharges the bio oil that condensation obtains to collect;
Electrical tar precipitator is used for above-mentioned condensed not condensable gases is carried out the static decoking, makes to purify the rear coal-tar middle oil content≤40mg/Nm of pyrolysis tail gas
3, the outlet of electrical tar precipitator left upper portion links to each other with adsorption tower left side lower inlet, is used for the contained tar of pyrolysis tail gas is captured;
Adsorption tower is used for above-mentioned static is adsorbed the decoking removal of impurities except defocused not condensable gases, makes the tar content≤15mg/Nm in the pyrolysis tail gas
3, the adsorption tower top exit links to each other with the tangential inlet of gas-liquid separator left upper portion;
Gas-liquid separator is used for above-mentioned absorption is carried out gas-liquid separation except defocused not condensable gases, removes the moisture in the pyrolysis tail gas, make the dew point of water in the pyrolysis tail gas≤-8 ℃, the gas-liquid separator bottom is provided with leakage fluid dram, and the top is provided with the air outlet, and the air outlet links to each other with the roots blower inlet mouth;
Roots blower is used for purifying pyrolysis tail gas and draws, as combustion gas.
3. refining plant as claimed in claim 1 is characterized in that the top of wherein said adsorption tower is provided with outlet, and the bottom of adsorption tower is provided with import, is provided with the first adsorption bed, the second adsorption bed and the 3rd adsorption bed in the adsorption tower from bottom to top; Described the first adsorption bed, the second adsorption bed and the 3rd adsorption bed stagger up and down mutually.
4. refining plant as claimed in claim 3, it is characterized in that the sorbent material in wherein said the first adsorption bed is corn cob or sawdust, sorbent material in the second adsorption bed is steel wire fibre ball or iron filings, the sorbent material of the 3rd adsorption bed is pyrolytic carbon, every layer of height of bed is 200-300mm, and gas flow rate is the 0.4-1.2 meter per second in the tower.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2012105929602A CN103013584A (en) | 2012-12-29 | 2012-12-29 | Purification method of biomass flash pyrolysis tail gas and device thereof |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2012105929602A CN103013584A (en) | 2012-12-29 | 2012-12-29 | Purification method of biomass flash pyrolysis tail gas and device thereof |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN103013584A true CN103013584A (en) | 2013-04-03 |
Family
ID=47962706
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2012105929602A Pending CN103013584A (en) | 2012-12-29 | 2012-12-29 | Purification method of biomass flash pyrolysis tail gas and device thereof |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN103013584A (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103627418A (en) * | 2013-11-30 | 2014-03-12 | 云南榕正生物能源有限公司 | Method for preparing charcoal by using straw |
| CN107903928A (en) * | 2017-11-21 | 2018-04-13 | 新奥科技发展有限公司 | The recovery method and system of a kind of coal tar |
| CN109022050A (en) * | 2018-06-06 | 2018-12-18 | 大唐长山热电厂 | The combined type fractional condensing unit and gasification of biomass pyrolysis gas separation method vented one's spleen for separating biomass heat of gasification |
Citations (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE4235893C2 (en) * | 1992-10-23 | 2000-07-13 | Siemens Ag | Process and device for cleaning dusty, hot, flammable gas |
| CN1730609A (en) * | 2005-08-24 | 2006-02-08 | 王华峰 | Biomass pyrogenation gasification and purification method |
| JP2008222978A (en) * | 2007-03-15 | 2008-09-25 | Mitsui Eng & Shipbuild Co Ltd | Wood charcoal gasification apparatus |
| CN101302430A (en) * | 2008-01-14 | 2008-11-12 | 张建超 | Method for preparing gas with crop wastes and organic refuses |
| CN101564630A (en) * | 2009-06-08 | 2009-10-28 | 南京林业大学 | Gas-liquid separation and purification system for pyrolysis gas of agriculture and forestry biomass materials |
| CN201376953Y (en) * | 2009-04-27 | 2010-01-06 | 李立新 | Combustible gas collecting and utilizing device for carbonization furnace |
| CN101817012A (en) * | 2009-02-27 | 2010-09-01 | 上海神工环保股份有限公司 | Gasification treatment device for household refuse |
| CN102010729A (en) * | 2010-12-03 | 2011-04-13 | 北京林业大学 | Multifunctional fluidized bed type biomass pyrolysis conversion device |
| CN201942654U (en) * | 2010-08-30 | 2011-08-24 | 陈荣均 | Civil man-made coal gas purifier |
| CN102703121A (en) * | 2012-01-12 | 2012-10-03 | 无锡湖光工业炉有限公司 | Biomass gas generation system |
-
2012
- 2012-12-29 CN CN2012105929602A patent/CN103013584A/en active Pending
Patent Citations (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE4235893C2 (en) * | 1992-10-23 | 2000-07-13 | Siemens Ag | Process and device for cleaning dusty, hot, flammable gas |
| CN1730609A (en) * | 2005-08-24 | 2006-02-08 | 王华峰 | Biomass pyrogenation gasification and purification method |
| JP2008222978A (en) * | 2007-03-15 | 2008-09-25 | Mitsui Eng & Shipbuild Co Ltd | Wood charcoal gasification apparatus |
| CN101302430A (en) * | 2008-01-14 | 2008-11-12 | 张建超 | Method for preparing gas with crop wastes and organic refuses |
| CN101817012A (en) * | 2009-02-27 | 2010-09-01 | 上海神工环保股份有限公司 | Gasification treatment device for household refuse |
| CN201376953Y (en) * | 2009-04-27 | 2010-01-06 | 李立新 | Combustible gas collecting and utilizing device for carbonization furnace |
| CN101564630A (en) * | 2009-06-08 | 2009-10-28 | 南京林业大学 | Gas-liquid separation and purification system for pyrolysis gas of agriculture and forestry biomass materials |
| CN201942654U (en) * | 2010-08-30 | 2011-08-24 | 陈荣均 | Civil man-made coal gas purifier |
| CN102010729A (en) * | 2010-12-03 | 2011-04-13 | 北京林业大学 | Multifunctional fluidized bed type biomass pyrolysis conversion device |
| CN102703121A (en) * | 2012-01-12 | 2012-10-03 | 无锡湖光工业炉有限公司 | Biomass gas generation system |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103627418A (en) * | 2013-11-30 | 2014-03-12 | 云南榕正生物能源有限公司 | Method for preparing charcoal by using straw |
| CN107903928A (en) * | 2017-11-21 | 2018-04-13 | 新奥科技发展有限公司 | The recovery method and system of a kind of coal tar |
| CN107903928B (en) * | 2017-11-21 | 2020-12-29 | 新奥科技发展有限公司 | Coal tar recovery method and system |
| CN109022050A (en) * | 2018-06-06 | 2018-12-18 | 大唐长山热电厂 | The combined type fractional condensing unit and gasification of biomass pyrolysis gas separation method vented one's spleen for separating biomass heat of gasification |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN202279806U (en) | Biomass carbonizing cracking gas purifier | |
| CN201473491U (en) | Biomass fast thermal decomposition device | |
| CN204400934U (en) | A kind of biomass gasification burning deep purifying device | |
| CN102304381B (en) | Combined type coal tar recovery equipment and coal tar recovery method using same | |
| CN102807884B (en) | Method for preparing biological oil and biological char by thermal cracking and liquefying bamboo wood | |
| CN111530441A (en) | Powdered activated carbon regeneration system and regeneration method thereof | |
| CN104861992A (en) | Pyrolysis device and method for producing light tar and clean gas | |
| CN103013584A (en) | Purification method of biomass flash pyrolysis tail gas and device thereof | |
| CN105778951B (en) | A kind of charcoal, gas, oil, electricity, hot coproduction carbonizing processing method | |
| CN202808710U (en) | Ore catalyst bed biomass flash pyrolysis oil production device | |
| CN101530710B (en) | Process and equipment for purifying flue gas in dry type for biomass electric power plant | |
| CN202346983U (en) | Dry type filtering and microwave regeneration recovery device for biomass gasification tar | |
| CN101974351A (en) | Scale fixed bed biomass gasification power generation production technology and complete equipment | |
| CN201342379Y (en) | Biomass electric power plant smoke gas dry type purification apparatus | |
| CN201737900U (en) | High-efficiency quick coal pyrolyzing device | |
| CN111826201A (en) | Process, system and application for flash pyrolysis gasification and tar removal of biomass | |
| CN110295064B (en) | Vibrator control method of biomass gasification power generation system | |
| CN205774362U (en) | A kind of dedusting decoking integration biomass gasification stove | |
| CN110295065B (en) | Integrated downdraft biomass gasification power generation system and method | |
| CN205170747U (en) | Novel revolving bed living beings pyrolysis system | |
| CN213680553U (en) | Particle moving bed device for high-temperature oil gas dust removal | |
| CN204799059U (en) | Petrochemical industry high temperature flue gas takes off dirt purifier | |
| CN104745237B (en) | A kind of process for being pyrolyzed high-temperature oil gas dedusting oil recovery | |
| CN204848754U (en) | Reduce outer hot type rotary furnace low temperature pyrolysis system of coal tar dustiness | |
| CN202359084U (en) | Coal gas purification system |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C02 | Deemed withdrawal of patent application after publication (patent law 2001) | ||
| WD01 | Invention patent application deemed withdrawn after publication |
Application publication date: 20130403 |