CN102260538B - Method and device for air-floatation flow-state high-temperature heat-transfer gasification of biomass - Google Patents
Method and device for air-floatation flow-state high-temperature heat-transfer gasification of biomass Download PDFInfo
- Publication number
- CN102260538B CN102260538B CN 201110173914 CN201110173914A CN102260538B CN 102260538 B CN102260538 B CN 102260538B CN 201110173914 CN201110173914 CN 201110173914 CN 201110173914 A CN201110173914 A CN 201110173914A CN 102260538 B CN102260538 B CN 102260538B
- Authority
- CN
- China
- Prior art keywords
- gas
- tubulation
- carbon
- pyrolyzer
- burnt
- 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.)
- Expired - Fee Related
Links
- 239000002028 Biomass Substances 0.000 title claims abstract description 63
- 238000002309 gasification Methods 0.000 title claims abstract description 58
- 238000000034 method Methods 0.000 title claims abstract description 43
- 238000010438 heat treatment Methods 0.000 claims abstract description 37
- 239000000446 fuel Substances 0.000 claims abstract description 27
- 239000002994 raw material Substances 0.000 claims abstract description 25
- 230000008569 process Effects 0.000 claims abstract description 24
- 239000000571 coke Substances 0.000 claims abstract description 20
- 238000005336 cracking Methods 0.000 claims abstract description 14
- 238000002485 combustion reaction Methods 0.000 claims abstract description 11
- 239000007787 solid Substances 0.000 claims abstract description 11
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 113
- 229910052799 carbon Inorganic materials 0.000 claims description 113
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 58
- 239000003546 flue gas Substances 0.000 claims description 58
- 239000002245 particle Substances 0.000 claims description 46
- 239000007789 gas Substances 0.000 claims description 42
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 24
- 239000000567 combustion gas Substances 0.000 claims description 21
- 238000006243 chemical reaction Methods 0.000 claims description 20
- 230000008676 import Effects 0.000 claims description 16
- 229910052739 hydrogen Inorganic materials 0.000 claims description 15
- 125000006850 spacer group Chemical group 0.000 claims description 12
- 239000000463 material Substances 0.000 claims description 10
- 239000002817 coal dust Substances 0.000 claims description 5
- 238000004140 cleaning Methods 0.000 claims description 4
- 238000009833 condensation Methods 0.000 claims description 4
- 230000005494 condensation Effects 0.000 claims description 4
- 238000003756 stirring Methods 0.000 abstract description 4
- 238000001914 filtration Methods 0.000 abstract description 3
- 239000000779 smoke Substances 0.000 abstract 2
- 239000003595 mist Substances 0.000 abstract 1
- 239000011269 tar Substances 0.000 description 25
- 238000000197 pyrolysis Methods 0.000 description 14
- 239000003921 oil Substances 0.000 description 13
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 8
- 239000000843 powder Substances 0.000 description 6
- 238000007789 sealing Methods 0.000 description 5
- 239000006200 vaporizer Substances 0.000 description 5
- 239000002918 waste heat Substances 0.000 description 5
- 230000008901 benefit Effects 0.000 description 4
- 238000005516 engineering process Methods 0.000 description 4
- 239000002737 fuel gas Substances 0.000 description 4
- 238000002955 isolation Methods 0.000 description 4
- 229910052757 nitrogen Inorganic materials 0.000 description 4
- 241000196324 Embryophyta Species 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 239000000835 fiber Substances 0.000 description 3
- 239000000295 fuel oil Substances 0.000 description 3
- 238000010907 mechanical stirring Methods 0.000 description 3
- 235000008733 Citrus aurantifolia Nutrition 0.000 description 2
- 235000008331 Pinus X rigitaeda Nutrition 0.000 description 2
- 235000011613 Pinus brutia Nutrition 0.000 description 2
- 241000018646 Pinus brutia Species 0.000 description 2
- 235000011941 Tilia x europaea Nutrition 0.000 description 2
- 239000000654 additive Substances 0.000 description 2
- 230000000996 additive effect Effects 0.000 description 2
- 230000005540 biological transmission Effects 0.000 description 2
- 239000003245 coal Substances 0.000 description 2
- 238000002474 experimental method Methods 0.000 description 2
- 239000004571 lime Substances 0.000 description 2
- 230000033001 locomotion Effects 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 239000002184 metal Substances 0.000 description 2
- 229910052751 metal Inorganic materials 0.000 description 2
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 description 1
- 238000004378 air conditioning Methods 0.000 description 1
- 239000011285 coke tar Substances 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 230000002950 deficient Effects 0.000 description 1
- 230000008021 deposition Effects 0.000 description 1
- 238000010790 dilution Methods 0.000 description 1
- 239000012895 dilution Substances 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 239000000428 dust Substances 0.000 description 1
- 230000005611 electricity Effects 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 238000005243 fluidization Methods 0.000 description 1
- 238000013467 fragmentation Methods 0.000 description 1
- 238000006062 fragmentation reaction Methods 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 229910052500 inorganic mineral Inorganic materials 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 230000007246 mechanism Effects 0.000 description 1
- 238000002844 melting Methods 0.000 description 1
- 230000008018 melting Effects 0.000 description 1
- 239000011707 mineral Substances 0.000 description 1
- 239000003345 natural gas Substances 0.000 description 1
- 229910052755 nonmetal Inorganic materials 0.000 description 1
- 238000005457 optimization Methods 0.000 description 1
- 239000010815 organic waste Substances 0.000 description 1
- 238000010248 power generation Methods 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 230000005855 radiation Effects 0.000 description 1
- 230000035484 reaction time Effects 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 239000013535 sea water Substances 0.000 description 1
- 239000000243 solution Substances 0.000 description 1
- 230000009885 systemic effect Effects 0.000 description 1
- 238000004227 thermal cracking Methods 0.000 description 1
- 230000009466 transformation Effects 0.000 description 1
- 239000012808 vapor phase Substances 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
- 239000002351 wastewater Substances 0.000 description 1
Images
Landscapes
- Processing Of Solid Wastes (AREA)
Abstract
The invention discloses a method and a device for air-floatation flow-state high-temperature heat-transfer gasification of biomass. The method comprises the following steps: (1) stirring a biomass gasifying raw material so as to form a mist state; (2) cracking under the heating of high temperature smoke at 800-1000 DEG C so as to obtain high temperature tar gas; (3) carrying out high temperature cracking and gasification on the high temperature tar gas and steam at the temperature of 1050-1150 DEG C; and (4) filtering, condensing and purifying solid residue and gas while stirring so as to obtain gas with a middle heat value. The device comprises a gas making furnace and at least one coke cracking furnace, wherein the gas making furnace comprises a gas collecting chamber and a stirring chamber; and the coke cracking furnace comprises an upper coke cracking furnace gas collecting chamber provided with a coke cracking furnace row tube, and a coke cracking furnace row tube shell layer is communicated with a gas making furnace row tube shell layer. According to the invention, a heat source in the whole cracking and gasification process is derived from high temperature smoke generated by combustion of a biomass micrometer fuel which is a renewable clean energy and is wide in source and low in cost. The method and device provided by the invention have the characteristics of high heat efficiency, high gas making efficiency and high gas heat value.
Description
Technical field
The invention belongs to biomass energy technology, be specifically related to a kind of biomass air supporting fluidised form high temperature heat exchange gasification process and device, be applicable to organism and coal, be particularly useful for agriculture and forestry organic waste material and coal dust pyrolysis gasification reformation and produce combustion gas.
Background technology
Day by day serious along with the day by day exhausted and environmental problem of fossil energy, the recycling treatment of developing clean renewable resources, refuse has become urgent problem.Biomass fuel will become the substitute of the mineral fuel such as coal, oil and natural gas, and its crucial part converts low-grade biomass energy to the high-grade energy exactly.
The internal heat type gasification process that generally adopts both at home and abroad, it be biomass at vaporizer and air incomplete combustion, the direct heating biomass make it to gasify.This method heating efficiency is high, but a large amount of nitrogen that the air that internal combustion needs is brought into have reduced the combustion gas quality, so the calorific value of combustion gas is low, only has 1200 kilocalories/M
3Below.The gasification efficiency of this method only is below 70%, awkward tar and the residual carbon to utilize of resultant product, and the combustion gas transformation efficiency is low, the serious waste energy.In the gas-purification process, can produce a large amount of tar and waste waters, contaminate environment simultaneously.Although it has been carried out improvement for many years both at home and abroad, the internal heat type gasification process can't be applied because of the defective of self eventually.Therefore, must gasify to the biomass indirect heating, avoiding bringing calorific value and the quality that a large amount of nitrogen reduce combustion gas into because of internal combustion heating, and tar, residual carbon must be converted into combustion gas as much as possible in gasification, the economic benefit of utilizing to improve biomass.The gasification of biomass external-heat exists heat and moisture transfer problems, because heat carries out thermal conduction and radiation heat transfer by the outer wall of pyrolysis vaporizer to the center, this will cause outside excess Temperature, and the temperature at center is on the low side, thereby affected the reaction times, and the heating and cooling time of pyrolysis vaporizer is also long.
Chinese patent literature CN101935568A discloses " a kind of high-temperature biomass micron fuel " (open day is on 01 05th, 2011), it comprises plant fibre powder and additive, wherein, the plant fibre powder massfraction accounts for 75～100%, additive is at least a during coal dust, lime powder and red mud account for, and the plant fibre powder particle diameter accounts for more than 70% less than the particle diameter of 250 μ m.Its temperature of combustion improves about 1 times than traditional method, and efficiency of combustion improves more than 1 times.Ordinary student material filamentary material can be carried by the micronization technology in fluidization, has become a kind of higher-grade fluid fuel near fuel oil and combustion gas.Can be widely used in that thermal power generation, Metal Melting, sea water desaltination, cities and towns heating, lime are fired, heat air-conditioning processed, industry heating etc.
Currently used biomass gasification method Main Problems:
(1) the internal heat type gasification contains a large amount of N take air as vaporized chemical in the gasification burning
2And CO
2, fuel gases calorific value is lower, and gasification efficiency is low, produces a large amount of tar.
(2) the internal heat type gasification is take pure oxygen as vaporized chemical, and cost is high, and investment is large.
(3) traditional external-heat gasification, the solid gasified raw material stockpiles at vaporizer, by the furnace wall indirect heating, because the vaporizer diameter is large (usually at 300-800mm), heat transfer distances is long, and heat transmission resistance is large, thereby heat transfer efficiency is low, and gasification efficiency is low, causes energy conversion efficient low.
(4) if the external-heat gasification adopts electricity, combustion gas or fuel oil as external heat source, heating cost is high.
Summary of the invention
The object of the invention is to overcome above-mentioned the deficiencies in the prior art part, biomass air supporting fluidised form high-temperature tubular heat exchange gasification square law device is provided, the present invention has the advantages that cost is low, thermo-efficiency is high, gas producing efficiency is high and fuel gases calorific value is high.
A kind of biomass air supporting fluidised form high temperature heat exchange gasification process provided by the invention is characterized in that the method comprises the steps:
The 1st step stirred the gasifying biomass raw material, can form fog flow with air-flow, and wherein, the particle diameter that in the initial gasifying biomass raw material particle more than 80% is arranged is below 2mm, and the particle diameter of the particle more than 30% is below 0.5mm; If gasified raw material is coal dust, the particle diameter that in the initial gasified raw material particle more than 80% is arranged is below 1mm, and the particle diameter of the particle more than 30% is below 0.3mm;
The material that the 2nd step obtained the 1st step carries out cracking under 800-1400 ℃ high-temperature flue gas indirect heating condition in the air supporting campaign, obtain high-temperature coke oil gas;
The 3rd step was gasified high-temperature coke oil gas high-temperature flue gas indirect heating Pintsch process by 1000-1800 ℃ under the condition that water vapour exists, and reaction generates CO, H
2And CH
4, also reaction generates CO and H to the residual carbon particle with water vapour in the high-temperature coke oil gas
2
The 4th step filtered with condensation cleaning and processes solid residue and combustion gas that the 3rd step obtained, obtained medium calorific value gas.
A kind of device of realizing above-mentioned biomass air supporting fluidised form high temperature heat exchange gasification process provided by the invention is characterized in that, this device comprises Gas-making Furnace and the burnt pyrolyzer of at least one carbon;
Gas-making Furnace comprises teeter column, tubulation pipe layer, upper collection chamber and tubulation shell.Be communicated with by tubulation pipe layer between the teeter column of Gas-making Furnace and the upper collection chamber.The upper and lower dividing plate that is provided with of Gas-making Furnace tubulation is fixed, by dividing plate with hermetic seal between teeter column, tubulation pipe layer, upper collection chamber three and the Gas-making Furnace tubulation shell; Gas-making Furnace tubulation shell is provided with high-temperature flue gas import and the outlet that is communicated with the outside, and is provided with one or more ash buckets in the shell bottom;
The teeter column is positioned at tubulation pipe layer below, and upper collection chamber is positioned at tubulation pipe layer top, is provided with biomass feed inlet in the teeter column, and agitating vane is installed in the bottom of teeter column, and agitating vane links to each other with the first motor;
The burnt pyrolyzer of carbon comprises tubulation pipe layer, tubulation shell, upper collection chamber and lower collection chamber.Be communicated with by tubulation pipe layer between upper collection chamber and the lower collection chamber.The upper and lower dividing plate that is provided with of the burnt pyrolyzer tubulation of carbon is fixed, by dividing plate with hermetic seal between upper collection chamber, tubulation pipe layer, lower collection chamber three and the tubulation shell; The burnt pyrolyzer tubulation of carbon shell is provided with high-temperature flue gas import and the outlet that is communicated with the outside; Upper collection chamber is provided with the water vapour import, and upper collection chamber communicates with collection chamber on the Gas-making Furnace by the tar gas pipeline; Lower collection chamber is provided with the air outlet, and its bottom is equipped with the burnt pyrolyzer agitating vane of the carbon that links to each other with the second motor; The burnt pyrolyzer tubulation of carbon shell communicates by the high-temperature flue gas pipeline with Gas-making Furnace tubulation shell.
The another kind of device of realizing above-mentioned biomass air supporting fluidised form high temperature heat exchange gasification process provided by the invention is characterized in that, this device comprises Gas-making Furnace and the burnt pyrolyzer of at least one carbon; Gas-making Furnace comprises tubulation pipe layer, upper collection chamber, lower collection chamber, teeter column and tubulation shell;
Gas-making Furnace tubulation shell bottom is provided with the teeter column, and the teeter column is provided with biomass feed inlet, and agitating vane is installed in the bottom of teeter column, and agitating vane links to each other with motor; Collection chamber is provided with the high-temperature flue gas mouth on the Gas-making Furnace; The upper collection chamber of Gas-making Furnace and lower collection chamber are communicated with by tubulation pipe layer.The upper and lower dividing plate that is provided with of Gas-making Furnace tubulation is fixed, by dividing plate with hermetic seal between upper collection chamber, tubulation pipe layer, lower collection chamber and the Gas-making Furnace tubulation shell;
The burnt pyrolyzer of carbon comprises collection chamber, tubulation pipe layer, lower collection chamber and tubulation shell.Upper collection chamber and the lower collection chamber of the burnt pyrolyzer of carbon are communicated with by tubulation pipe layer, the upper and lower dividing plate that is provided with of the burnt pyrolyzer tubulation of carbon is fixed, by dividing plate with hermetic seal between the upper collection chamber of the burnt pyrolyzer of carbon, tubulation pipe layer, lower collection chamber three and the carbon Jiao pyrolyzer tubulation shell.Collection chamber and lower collection chamber respectively are provided with the high-temperature flue gas mouth on the burnt pyrolyzer of carbon.The lower collection chamber of the burnt pyrolyzer of carbon is communicated with by the high-temperature flue gas pipe with the lower collection chamber of Gas-making Furnace, is provided with ash bucket in the middle of the high-temperature flue gas pipeline; The burnt pyrolyzer tubulation of carbon shell is provided with the water vapour import; The burnt pyrolyzer tubulation of carbon shell top communicates with Gas-making Furnace tubulation shell top by the tar gas pipeline; The burnt pyrolyzer tubulation of carbon shell bottom is provided with the oil gas vent that discharges of the coke.
The present invention has the following advantages compared to existing technology:
(1) biomass air-isolation sealing charging under the condition of pressure, guaranteed that the pyrolysis gasification product is pressed into gasification system and continues cracking, the combustion gas that has guaranteed simultaneously to produce does not contain the nitrogen that derives from air not by airborne nitrogen dilution in the combustion gas of generation, fuel gases calorific value is high
(2) biological particles relies on mechanical stirring in Gas-making Furnace, makes it be vaporific fluidised form, is conducive to the raising of solid particulate homogeneous heating and heat transfer efficiency.
(3) gasified raw material flows in tubulation and is gasified by indirect heating, so just the indirect heating to solid is transformed into indirect heating to vapor phase stream, greatly increase unit heat transfer area, shorten heat transfer distances, improve heat transfer efficiency, solved the low problem of external-heat gasified raw material indirect heating thermo-efficiency.
(4) adopt tubular heat exchange to conduct heat in the burnt pyrolyzer of carbon, tubulation shell district adopts the thermal-flame heating of biomass micron fuel burning, tubulation pipe floor district passes through gas-gas heat-exchange method to tar gas and semicoke high temperature cracking steam gasification, be conducive to tar uniform high-efficiency ground and obtain high temperature, it is high to have coke tar cracking efficient, and char Gasification is advantage completely.
(5) after the high-temperature flue gas of biomass micron fuel burning carries out indirect heating to the tubulation shell in the burnt pyrolyzer of carbon, again the tubulation shell in the Gas-making Furnace is carried out indirect heating, its using waste heat from tail gas and then be used for to the indirect heating preheating of gasifying biomass raw material with to participating in the indirect heating preheating with the air of biomass micron fuel burning, realize the multistage cascade utilization of heat energy, improved the efficiency of utilization of gasification system
(6) mechanical movement of solid gasified raw material in whole gasification system is transformed into liquid motion, designs simplification, and process is controlled easily; Raw material pyrolysis gasification in the air supporting campaign, systemic resistance is little.
(7) biomass micron fuel of the thermal source use of whole pyrolysis gasification process heating is a kind of reproducible clean energy, and the source is wide, cost is low.
Description of drawings
Fig. 1 is the structural representation of the first embodiment of apparatus of the present invention;
Fig. 2 is the structural representation of the second embodiment of apparatus of the present invention;
Among the figure: 1, collection chamber on the Gas-making Furnace; 2, Gas-making Furnace tubulation upper spacer; 3, exhanst gas outlet; 4, Gas-making Furnace tubulation shell; 5, Gas-making Furnace tubulation pipe layer; 6, teeter column; 7, opening for feed; 8, Gas-making Furnace agitating vane; 9, tar gas pipeline; 10, water vapour import; 11, high-temperature flue gas import; 12, the burnt pyrolyzer tubulation of carbon pipe layer; 13, the burnt pyrolyzer tubulation of carbon shell; 14, air outlet; 15, collection chamber on the burnt pyrolyzer of carbon; 16, the burnt pyrolyzer agitating vane of carbon; 17, the burnt pyrolyzer tubulation of carbon upper spacer; 18, high-temperature flue gas pipeline; 19, ash bucket; 20, Gas-making Furnace tubulation lower clapboard; 21, collection chamber under the burnt pyrolyzer of carbon; 22, the burnt pyrolyzer tubulation of carbon lower clapboard; 23, collection chamber under the Gas-making Furnace.
Embodiment
The inventive method comprises the steps:
(1) the gasifying biomass raw material is stirred, can form fog flow with air-flow, wherein, the particle diameter that in the initial gasifying biomass raw material particle more than 80% is arranged is below 2mm, and the particle diameter of the particle more than 30% is below 0.5mm; If gasified raw material is coal dust, the particle diameter that in the initial gasified raw material particle more than 80% is arranged is below 1mm, and the particle diameter of the particle more than 30% is below 0.3mm;
(2) in 800-1400 ℃ high-temperature flue gas, optimal temperature is to carry out cracking under 900-1050 ℃ the high-temperature flue gas indirect heating condition to the material that step (1) is obtained, and obtains high-temperature coke oil gas in the air supporting campaign;
(3) with high-temperature coke oil gas high-temperature flue gas by 1000-1800 ℃ under the water vapour existence condition, optimal temperature is under 1100-1400 ℃ the high-temperature flue gas indirect heating, to carry out the Pintsch process gasification, and reaction generates CO, H
2And CH
4, also reaction generates CO and H to residual carbon with water vapour in the high-temperature coke oil gas
2Water vapour intake S/B is best in the 0.73-1.02 scope, and S represents the flow velocity of water vapour, and B represents the feeding rate of gasifying biomass raw material.
(4) to the resulting solid residue of step (3) and combustion gas, filter with condensation cleaning and process, with regard to available CO, H
2And CH
4Content accounts for the medium calorific value gas about 80%, contains hardly tar in the combustion gas.
Optimization as technique scheme, the biomass micron fuel burning that high-temperature flue gas in step (2) and (3) provides by CN101935568A produces, and 1800 ℃ high-temperature flue gas is that air through preheating produces biomass micron fuel generation high-temp combustion.
The thermal source air-flow of gas-air-tube type heat-exchange method can be walked shell, also can walk the pipe layer.Fig. 1 is the embodiment that the thermal source air-flow is walked shell.In this embodiment, device comprises Gas-making Furnace and the burnt pyrolyzer of at least one carbon.Gas-making Furnace comprises collection chamber 1 and Gas-making Furnace tubulation shell 4 on teeter column 6, Gas-making Furnace tubulation pipe layer 5, the Gas-making Furnace.The teeter column 6 of Gas-making Furnace and upper collection chamber 1 are communicated with by tubulation pipe layer 5.The Gas-making Furnace tubulation is provided with upper spacer 2 and lower clapboard 20, and fixes by upper and lower dividing plate, by dividing plate with hermetic seal between teeter column 6, tubulation pipe layer 5, upper collection chamber 1 three and the Gas-making Furnace tubulation shell 4; Gas-making Furnace tubulation shell 4 is provided with the high-temperature flue gas outlet 3 that is communicated with the outside, and is provided with ash bucket 19 in the shell bottom;
Be positioned at Gas-making Furnace tubulation pipe layer 5 below in the teeter column 6, collection chamber 1 is positioned at Gas-making Furnace tubulation pipe layer 5 top on the Gas-making Furnace, be provided with biomass feed inlet 7 in the teeter column 6, Gas-making Furnace agitating vane 8 is installed in the bottom of teeter column 6, and agitating vane 8 links to each other with the first motor.
The burnt pyrolyzer of carbon comprises on the burnt pyrolyzer tubulation of carbon pipe layer 12, the burnt pyrolyzer tubulation of carbon shell 13, the burnt pyrolyzer of carbon collection chamber 21 under collection chamber 15, the burnt pyrolyzer of carbon.Be communicated with by tubulation pipe layer 12 between upper collection chamber 15 and the lower collection chamber 21.The burnt pyrolyzer tubulation of carbon is provided with upper spacer 17 and lower clapboard 22, and fix by upper and lower dividing plate, by dividing plate with hermetic seal between collection chamber 21 threes under collection chamber 15, tubulation pipe layer 12, the burnt pyrolyzer of carbon on the burnt pyrolyzer of carbon and the carbon Jiao pyrolyzer tubulation shell 13; The burnt pyrolyzer tubulation of carbon shell 13 is provided with the high-temperature flue gas import 11 that is communicated with the outside; Upper collection chamber 15 is provided with water vapour import 10, and upper collection chamber 15 tops are communicated with collection chamber 1 on the Gas-making Furnace by tar gas pipeline 18; Lower collection chamber 21 is provided with air outlet 14, and its bottom is equipped with the burnt pyrolyzer agitating vane 16 of the carbon that links to each other with the second motor; The burnt pyrolyzer tubulation of carbon shell 13 and Gas-making Furnace tubulation shell 4 communicate by high-temperature flue gas pipeline 18.
The high-temperature flue gas of biomass micron fuel burning enters the burnt pyrolyzer tubulation of carbon shell 13 by high-temperature flue gas import 11 its tubulation pipe layer 12 is carried out heat.The high-temperature flue gas of the burnt pyrolyzer tubulation of carbon shell 13 carries out indirect heating by the tubulation shell 4 that high-temperature flue gas pipeline 18 enters Gas-making Furnace to its tubulation pipe layer 5 subsequently, the part ash deposition is in ash bucket 19 in the final high temperature flue gas, flue gas is from exhanst gas outlet 3 dischargings, can utilize its waste heat to the indirect heating preheating of gasifying biomass raw material with to participating in the indirect heating preheating of the air that burns with biomass micron fuel, to improve the efficiency of utilization of gasification system.
Biological particles pressure sealing enters the teeter column of Gas-making Furnace bottom 6 from opening for feed 7, relies on agitating vane 8 mechanical stirring, and with the biological particles atomizing, atomizing particle rises with air-flow and enters Gas-making Furnace tubulation pipe layer 5.Gas-making Furnace tubulation shell 4 adopts high-temperature flue gas 900-1050 ℃ of biomass micron fuel burning, for the vaporific biological particles pyrolysis gasification in the tubulation pipe layer provides heat energy, the high-temperature coke oil gas that produces rises under the effect of hot gas buoyant flow, enter the upper collection chamber 1 of Gas-making Furnace tubulation upper spacer 2 tops, the high-temperature coke oil gas that carries residual carbon enters the upper collection chamber 15 of the burnt pyrolyzer tubulation of carbon upper spacer 17 tops by tar gas pipeline 9 and the water vapor 10 added, then in the 12 interior generation pyrolysis gasifications reaction of the burnt pyrolyzer tubulation of carbon pipe layer.1300-1500 ℃ of thermal-flame of biomass micron fuel burning enters its tubulation shell 13 by high-temperature flue gas import 11, and tar and water vapor by in 1100-1400 ℃ the high-temperature flue gas indirect heating tubulation pipe layer in the tubulation shell make it reaction and generate CO, H
2And CH
4, residual carbon also generates CO and H with steam reaction
2, tar and residual carbon are gasified by high temperature pyrolysis by gas-air-tube type interchanger at the volley.And the mechanical stirring by agitating vane 16, preventing that solid residue is deposited on collection chamber 21 under the burnt pyrolyzer of carbon, last combustion gas and solid residue lime-ash 14 are gone out from the air outlet, carry out next step gas filtration and condensation cleaning, contain hardly tar in the combustion gas.The CO that obtains, H
2And CH
4Content accounts for the medium calorific value gas about 80%.
90% particle is at the following gasified raw material of 2mm, the air-isolation sealing enters the teeter column 6 of gasifier bottom section under the condition of pressure, relies on blade mechanism to stir, and has certain crushing effect, with the biological particles atomizing, atomizing particle rises with air-flow and enters Gas-making Furnace tubulation pipe layer.Gas-making Furnace tubulation shell district passes into the high-temperature flue gas waste-heat of micron fuel burning, its high-temperature flue gas waste heat comes from the high-temperature flue gas in the tubulation shell district of the burnt pyrolyzer of carbon, vaporific granular fuel in the Gas-making Furnace tubulation pipe layer is heated, make it pyrolysis gasification, the high-temperature coke oil gas that produces rises under the effect of hot gas buoyant flow, and carry residual carbon and the water vapor added enters in the tubulation pipe layer of the burnt pyrolyzer of carbon, its tubulation shell district passes into biomass micron fuel combustion high temperature flue gas, tar and water vapor in the heating tubulation pipe layer make it reaction and generate CO, H
2And CH
4, residual carbon also generates CO and H with steam reaction
2, tar and residual carbon are passed through gas-air-tube type heat-exchange method by high temperature solution thermal cracking gasification in transmission.
Wherein the burnt pyrolyzer of carbon can be 1-6, and optimum quantity is 2-3, and the thermal source air-flow of gas-air-tube type heat-exchange method can be walked shell, also can walk the pipe layer; The diameter of heat exchanging pipe is 10-220mm, and optimum diameter is 30-80mm.The material of the burnt pyrolyzer tubulation of Gas-making Furnace tubulation and shell and carbon and shell can be metal heat-stable material or nonmetal heatproof material.The inorganics of minority separates with combustion gas by dedusting in the rear gasification product of the burnt pyrolyzer gasification of carbon; High-temperature fuel gas obtains tar and the required water vapor of residual carbon gasification through pre-thermal utilization, and gasification gas purifies after filtration and obtains required combustion gas.The energy of heating can be biomass micron fuel, combustion gas, fuel oil and residual carbon dust.The diameter of the particle of biomass micron fuel is main powder below 400 μ m, and optimum particle diameter is to be main powder below 250 μ m.The particle diameter of the particle more than 80% is below 2mm, and the particle diameter of the particle more than 30% is below 0.5mm.Out the waste heat of high-temperature flue gas tail gas of micron fuel burning is used for to the preheating of solid particle fuel indirect heating with to participating in the indirect heating preheating with the air of biomass micron fuel burning, to improve the efficiency of utilization of gasification system from Gas-making Furnace tubulation shell district.
Fig. 2 is the embodiment that the thermal source air-flow is walked the pipe layer, and among Fig. 2, apparatus of the present invention comprise Gas-making Furnace and the burnt pyrolyzer of at least one carbon.Gas-making Furnace comprises on tubulation pipe layer 5, the Gas-making Furnace collection chamber 23, teeter column 6 and tubulation shell 4 under collection chamber 1, the Gas-making Furnace.
Gas-making Furnace tubulation shell 4 bottoms are provided with teeter column 6, are provided with biomass feed inlet 7 in the teeter column 6, and agitating vane 8 is installed in the bottom of teeter column 6, and agitating vane 8 links to each other with motor; Collection chamber 1 is provided with high-temperature flue gas outlet 3 on the Gas-making Furnace; On the Gas-making Furnace under collection chamber 1 and the Gas-making Furnace collection chamber 23 be communicated with by tubulation pipe layer 5.The upper spacer 2 that the Gas-making Furnace tubulation is provided with and lower clapboard 20, and fix by upper and lower dividing plate, by dividing plate with hermetic seal between collection chamber 23 and the tubulation shell 4 under upper collection chamber 1, tubulation pipe layer 5, the Gas-making Furnace;
The burnt pyrolyzer of carbon comprises collection chamber 21 and the burnt pyrolyzer tubulation of carbon shell 13 under collection chamber 15 on the burnt pyrolyzer of carbon, the burnt pyrolyzer tubulation of carbon pipe layer 12, the burnt pyrolyzer of carbon.Upper collection chamber 15 and lower collection chamber 21 communicate by tubulation pipe layer 12, upper spacer 17 and lower clapboard 22 that the burnt pyrolyzer tubulation of carbon is provided with, and fix by upper and lower dividing plate, by dividing plate with hermetic seal between upper collection chamber 15, tubulation pipe layer 12, lower collection chamber 21 threes and the burnt pyrolyzer tubulation of the carbon shell 13, collection chamber 15 tops are provided with high-temperature flue gas import 11 on the burnt pyrolyzer of carbon, collection chamber 21 is communicated with collection chamber 20 under the Gas-making Furnace by high-temperature flue gas pipeline 18 under the burnt pyrolyzer of carbon, and is provided with ash bucket 19 in the middle of high-temperature flue gas pipeline 18; The burnt pyrolyzer tubulation of carbon shell 13 is provided with water vapour import 10; The burnt pyrolyzer tubulation of carbon shell 13 tops communicate with Gas-making Furnace tubulation shell 4 tops by tar gas pipeline 9; The burnt pyrolyzer tubulation of carbon shell 13 bottoms are provided with air outlet 14.
Below by by embodiment the present invention being described in further detail, but following examples only are illustrative, and protection scope of the present invention is not subjected to the restriction of these embodiment.
Example 1:
Used gasified raw material is pine sawdust, be processed into particle diameter less than 3mm through homemade crusher, adopt this gasification process, the air-isolation sealing enters Gas-making Furnace, after atomizing, enter Gas-making Furnace tubulation pipe layer, it is that 1050 ℃ high-temperature flue gas carries out pyrolysis gasification to pine sawdust particle in the pipe layer that the tubulation shell passes into temperature, the high-temperature coke oil gas that produces and the water vapor of adding enter the burnt pyrolyzer of carbon, wherein S/B is 1.02, carry out the pyrolysis gasification reaction of tar gas through pipe type heat transfer, under 1400 ℃ high-temperature flue gas heating, make the reaction of tar generating gasification generate CO, H
2And CH
4, residual carbon also generates CO and H with steam reaction
2
High-temperature flue gas in this experiment be by diameter less than the thermal-flame that the biomass micron fuel high-temp combustion of 250 μ m produces, progressively pass into the burnt tubulation furnace shell layer of carbon and Gas-making Furnace tubulation shell.
By present method, the combustion gas total gas production of acquisition is 1.77Nm
3/ kg.Tar content is 0.12%, and gaseous product mainly comprises H
2, CO, CH
4, C
2H
4, C
2H
6And CO
2Deng, content is respectively 40.8%, 25.4%, 8.5%, 2.2%, 0.1% and 23% separately, carbon conversion efficiency is 88.2%.
Used gasified raw material is stalk, make the biomass material that particle diameter is 3-15mm after the fragmentation, adopt this gasification process, the air-isolation sealing enters Gas-making Furnace, after atomizing, enter Gas-making Furnace tubulation pipe layer, it is that 900 ℃ high-temperature flue gas carries out pyrolysis gasification to stalk particle in the pipe layer that the tubulation shell passes into temperature, the high-temperature coke oil gas that produces and the water vapor of adding enter the burnt pyrolyzer of carbon, wherein S/B is 0.73, carry out the pyrolysis gasification reaction of tar gas through pipe type heat transfer, under 1100 ℃ high-temperature flue gas heating, make the reaction of tar generating gasification generate CO, H
2And CH
4, residual carbon also generates CO and H with steam reaction
2
High-temperature flue gas in this experiment be by diameter less than the thermal-flame that the biomass micron fuel high-temp combustion of 250 μ m produces, progressively pass into the burnt tubulation furnace shell layer of carbon and Gas-making Furnace tubulation shell.
By present method, the combustion gas total gas production of acquisition is 1.23Nm
3/ kg.Tar content is 0.96%, and gaseous product mainly comprises H
2, CO, CH
4, C
2H
4, C
2H
6And CO
2Deng, content is respectively 36.3%, 20.4%, 12.2%, 2.3%, 0.8% and 28% separately, carbon conversion efficiency is 73%.
The above is preferred embodiment of the present invention, but the present invention should not be confined to the disclosed content of this embodiment and accompanying drawing.So everyly do not break away from the equivalence of finishing under the spirit disclosed in this invention or revise, all fall into the scope of protection of the invention.
Claims (8)
1. a biomass air supporting fluidised form high temperature heat exchange gasification process is characterized in that the method comprises the steps:
The 1st step stirred the gasifying biomass raw material, made it vaporific, wherein, the particle diameter of 80% particle was arranged in the gasifying biomass raw material below 2mm, and the particle diameter of the particle more than 30% is below 0.5mm; If gasified raw material is coal dust, the particle diameter that in the initial gasified raw material particle more than 80% is arranged is below 1mm, and the particle diameter of the particle more than 30% is below 0.3mm;
The material that the 2nd step obtained the 1st step carries out cracking under 800-1400 ℃ high-temperature flue gas indirect heating condition in the air supporting campaign, obtain high-temperature coke oil gas;
The 3rd step was gasified high-temperature coke oil gas high-temperature flue gas indirect heating Pintsch process by 1000-1800 ℃ under the condition that water vapour exists, and reaction generates CO, H
2And CH
4, also reaction generates CO and H to residual carbon with water vapour in the high-temperature coke oil gas
2
The 4th step filtered with condensation cleaning and processes solid residue and combustion gas that the 3rd step obtained, obtained medium calorific value gas.
2. biomass air supporting fluidised form high temperature heat exchange gasification process according to claim 1 is characterized in that water vapour intake S/B is in the 0.73-1.02 scope, and S represents the flow velocity of water vapour, and B represents the feeding rate of gasifying biomass raw material.
3. biomass air supporting fluidised form high temperature heat exchange gasification process according to claim 1 and 2, it is characterized in that, high-temperature flue gas in the 2nd step and the 3rd step is by biomass micron fuel burning generation, and 1800 ℃ high-temperature flue gas is that air through preheating produces biomass micron fuel generation high-temp combustion.
4. biomass air supporting fluidised form high temperature heat exchange gasification process according to claim 3 is characterized in that, in the 2nd step, the temperature of high-temperature flue gas is 900-1050 ℃.
5. biomass air supporting fluidised form high temperature heat exchange gasification process according to claim 3 is characterized in that, in the 3rd step, the temperature of high-temperature flue gas is 1100-1400 ℃.
6. a device of realizing the described biomass air supporting of claim 1 fluidised form high temperature heat exchange gasification process is characterized in that, this device comprises Gas-making Furnace and the burnt pyrolyzer of at least one carbon;
Gas-making Furnace comprises collection chamber (1) and Gas-making Furnace tubulation shell (4) on teeter column (6), Gas-making Furnace tubulation pipe layer (5), the Gas-making Furnace; The teeter column of Gas-making Furnace (6) and upper collection chamber (1) are communicated with by tubulation pipe layer (5); The Gas-making Furnace tubulation is provided with upper spacer (2) and lower clapboard (20), and fixes by upper and lower dividing plate, by dividing plate with hermetic seal between teeter column (6), tubulation pipe layer (5), upper collection chamber (1) three and the Gas-making Furnace tubulation shell (4); Gas-making Furnace tubulation shell (4) is provided with the high-temperature flue gas outlet (3) that is communicated with the outside, and is provided with ash bucket (19) in the shell bottom;
Be positioned at Gas-making Furnace tubulation pipe layer (5) below in the teeter column (6), collection chamber on the Gas-making Furnace (1) is positioned at Gas-making Furnace tubulation pipe layer (5) top, be provided with biomass feed inlet (7) in the teeter column (6), Gas-making Furnace agitating vane (8) is installed in the bottom of teeter column (6), and agitating vane (8) links to each other with the first motor;
The burnt pyrolyzer of carbon comprises on the burnt pyrolyzer tubulation pipe layer (12) of carbon, the burnt pyrolyzer tubulation shell (13) of carbon, the burnt pyrolyzer of carbon collection chamber (21) under collection chamber (15), the burnt pyrolyzer of carbon; Be communicated with by tubulation pipe layer (12) between upper collection chamber (15) and the lower collection chamber (21); The burnt pyrolyzer tubulation of carbon is provided with upper spacer (17) and lower clapboard (22), and fix by upper and lower dividing plate, by dividing plate with hermetic seal between collection chamber (21) three under collection chamber (15), tubulation pipe layer (12), the burnt pyrolyzer of carbon on the burnt pyrolyzer of carbon and the carbon Jiao's pyrolyzer tubulation shell (13); The burnt pyrolyzer tubulation shell of carbon (13) is provided with the high-temperature flue gas import (11) that is communicated with the outside; Upper collection chamber (15) is provided with water vapour import (10), and upper collection chamber (15) top is communicated with collection chamber (1) on the Gas-making Furnace by tar gas pipeline (9); Lower collection chamber (21) is provided with air outlet (14), and its bottom is equipped with the burnt pyrolyzer agitating vane (16) of the carbon that links to each other with the second motor; The burnt pyrolyzer tubulation shell of carbon (13) communicates by high-temperature flue gas pipeline (18) with Gas-making Furnace tubulation shell (4).
7. device according to claim 6 is characterized in that, wherein the quantity of the burnt pyrolyzer of carbon is 2-3.
8. a device of realizing the described biomass air supporting of claim 1 fluidised form high temperature heat exchange gasification process is characterized in that, this device comprises Gas-making Furnace and the burnt pyrolyzer of at least one carbon; Gas-making Furnace comprises on tubulation pipe layer (5), the Gas-making Furnace collection chamber (23), teeter column (6) and tubulation shell (4) under collection chamber (1), the Gas-making Furnace;
Gas-making Furnace tubulation shell (4) bottom is provided with teeter column (6), is provided with biomass feed inlet (7) in teeter column (6), and agitating vane (8) is installed in the bottom of teeter column (6), and agitating vane (8) links to each other with motor; Collection chamber on the Gas-making Furnace (1) is provided with high-temperature flue gas outlet (3); Collection chamber (23) is communicated with by tubulation pipe layer (5) under collection chamber on the Gas-making Furnace (1) and the Gas-making Furnace; The upper spacer that the Gas-making Furnace tubulation is provided with (2) and lower clapboard (20), and fix by upper and lower dividing plate, by dividing plate with hermetic seal between collection chamber (23) and the tubulation shell (4) under upper collection chamber (1), tubulation pipe layer (5), the Gas-making Furnace;
The burnt pyrolyzer of carbon comprises collection chamber (21) and the burnt pyrolyzer tubulation shell (13) of carbon under collection chamber (15) on the burnt pyrolyzer of carbon, the burnt pyrolyzer tubulation pipe layer (12) of carbon, the burnt pyrolyzer of carbon; On the burnt pyrolyzer of carbon under the burnt pyrolyzer of collection chamber (15) and carbon collection chamber (21) by the burnt pyrolyzer tubulation pipe layer of carbon (12) connection, upper spacer (17) and lower clapboard (22) that the burnt pyrolyzer tubulation of carbon is provided with, and by upper, lower clapboard is fixed, by dividing plate with upper collection chamber (15), tubulation pipe layer (12), hermetic seal between the burnt pyrolyzer tubulation shell of lower collection chamber (21) three and carbon (13), collection chamber (15) top is provided with high-temperature flue gas import (11) on the burnt pyrolyzer of carbon, collection chamber (21) communicates with collection chamber (20) under the Gas-making Furnace by high-temperature flue gas pipeline (18) under the burnt pyrolyzer of carbon, and is provided with ash bucket (19) in the middle of high-temperature flue gas pipeline (18); The burnt pyrolyzer tubulation shell (13) of carbon top is provided with water vapour import (10); The burnt pyrolyzer tubulation shell (13) of carbon top communicates with Gas-making Furnace tubulation shell (4) top by tar gas pipeline (9); The burnt pyrolyzer tubulation shell (13) of carbon bottom is provided with air outlet (14).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201110173914 CN102260538B (en) | 2011-06-24 | 2011-06-24 | Method and device for air-floatation flow-state high-temperature heat-transfer gasification of biomass |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201110173914 CN102260538B (en) | 2011-06-24 | 2011-06-24 | Method and device for air-floatation flow-state high-temperature heat-transfer gasification of biomass |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN102260538A CN102260538A (en) | 2011-11-30 |
| CN102260538B true CN102260538B (en) | 2013-04-17 |
Family
ID=45007388
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 201110173914 Expired - Fee Related CN102260538B (en) | 2011-06-24 | 2011-06-24 | Method and device for air-floatation flow-state high-temperature heat-transfer gasification of biomass |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN102260538B (en) |
Families Citing this family (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102899091B (en) * | 2012-11-14 | 2014-03-19 | 程培胜 | Method for preparing coal gas by cracking biomasses and municipal wastes by using system self heat source |
| CN105299622A (en) * | 2014-05-27 | 2016-02-03 | 上海毅知实业有限公司 | Method for combusting biomass synthetic fuel |
| CN110066692A (en) * | 2019-03-22 | 2019-07-30 | 张英华 | Coal hydrogen equipment and control method |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1603388A (en) * | 2004-09-03 | 2005-04-06 | 南京工业大学 | Process and device for preparing coal gas by using fluffy biomass raw material |
| CN1831094A (en) * | 2006-04-21 | 2006-09-13 | 江苏大学 | Process and equipment for co-gasification of biomass and coal |
| CN202401035U (en) * | 2011-11-15 | 2012-08-29 | 华中科技大学 | Biomass air-floatation flow-state high-temperature heat-exchange gasifying device |
Family Cites Families (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE102005043212A1 (en) * | 2005-09-09 | 2007-03-15 | Future Energy Gmbh | Solid fuel, e.g. anthracite or gasification, for e.g. fluidized bed reactor, involves taking water-washed raw gas for deposition of particulate matters of partial condensation, where raw gas is indirectly cooled at preset temperature |
-
2011
- 2011-06-24 CN CN 201110173914 patent/CN102260538B/en not_active Expired - Fee Related
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1603388A (en) * | 2004-09-03 | 2005-04-06 | 南京工业大学 | Process and device for preparing coal gas by using fluffy biomass raw material |
| CN1831094A (en) * | 2006-04-21 | 2006-09-13 | 江苏大学 | Process and equipment for co-gasification of biomass and coal |
| CN202401035U (en) * | 2011-11-15 | 2012-08-29 | 华中科技大学 | Biomass air-floatation flow-state high-temperature heat-exchange gasifying device |
Also Published As
| Publication number | Publication date |
|---|---|
| CN102260538A (en) | 2011-11-30 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| WO2015143955A1 (en) | Solid fuel staged gasification-combustion dual-bed polygeneration system and method | |
| CN102517065B (en) | Self-heating type biomass fast pyrolysis liquefying device | |
| CN101024782B (en) | Dense-phase conveying-bed coal pressurizing gasifying apparatus and method | |
| CN206531067U (en) | A kind of system of refuse pyrolysis gasification and melting | |
| CN102071042B (en) | Intelligentized continuous quick microwave cracking device for biomass and waste of biomass | |
| CN1888017B (en) | Cracking and gasifying reforming furnace | |
| CN102226107A (en) | Technology and equipment for preparation of synthetic gas by two-stage high temperature biomass gasification | |
| CN101250419B (en) | Low-temperature dry distillation process with coal gas internal heat | |
| CN101955803A (en) | Low-rank coal carbonization method | |
| CN107189821A (en) | A kind of dry pulverized coal coupled biological matter gasifies descending Quench gasification furnace altogether | |
| CN102146301A (en) | Method for two-stage coal gasification on composite external heat fixed bed and gas furnace | |
| CN106500107A (en) | A kind of system and method for refuse pyrolysis gasification and melting | |
| CN103740409A (en) | Multi-stage gas distribution high-temperature coal gasification device and method | |
| CN110903855A (en) | Material pyrolysis gasification process, system and application | |
| CN201343520Y (en) | Flash dry distillation technology device of oil shale | |
| CN102260536A (en) | Internal circulation external heating type gasification device | |
| CN204058390U (en) | Solid fuel classification gasification-burning double bed polygenerations systeme | |
| CN102260538B (en) | Method and device for air-floatation flow-state high-temperature heat-transfer gasification of biomass | |
| CN102517079B (en) | Biomass gasifying device with function of catalytically cracking inner circulation tar | |
| CN202401035U (en) | Biomass air-floatation flow-state high-temperature heat-exchange gasifying device | |
| CN108504396B (en) | Sectional biomass gasification method and special equipment thereof | |
| CN202322754U (en) | External heat type gasifier | |
| CN202440467U (en) | Self-heating biomass flash pyrolysis liquefying device | |
| CN205258385U (en) | Fixed bed biological matter gasification - pyrolysis of coal coupling poly -generation device | |
| CN102010758B (en) | Method for preparing feed gas by utilizing rubbish and biomass |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20130417 |
|
| CF01 | Termination of patent right due to non-payment of annual fee |