CN103361085A - Cleaner production system of carbonization furnace group - Google Patents
Cleaner production system of carbonization furnace group Download PDFInfo
- Publication number
- CN103361085A CN103361085A CN2012100876261A CN201210087626A CN103361085A CN 103361085 A CN103361085 A CN 103361085A CN 2012100876261 A CN2012100876261 A CN 2012100876261A CN 201210087626 A CN201210087626 A CN 201210087626A CN 103361085 A CN103361085 A CN 103361085A
- Authority
- CN
- China
- Prior art keywords
- heat
- gas
- oil
- heat transfer
- oil gas
- 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
- Processing Of Solid Wastes (AREA)
Abstract
The invention discloses a cleaner production system (figure 1) for intermittent carbonization furnaces, which realizes mass transfer and heat transfer between the carbonization furnaces and colony using of the carbonization furnaces. The system adopts the technical scheme that hot air and oil-gas can be transferred to a plurality of following carbonization furnaces (B, C and D) which are not ignited from a current heating (spontaneous combustion or furnace chamber heating) carbonization furnace A through inter-furnace mass transfer and heat transfer passages, so as to progressively realize preheating, drying or preliminary thermal cracking of the carbonization furnaces (B, C and D), which in turn shortens the preparation time of ignition and thermal cracking and facilitates quick temperature reduction after the completion of thermal cracking. The cleaner production system adopting the working mode is conducive to improving the production efficiency, speed and benefits. Moreover, the whole production process is very clean and energy is saved, as the flue gas generated during combustion heating and the oil-gas generated during thermal cracking are processed respectively, the flue gas is directly used for drying biomass materials, the oil-gas enters into a special oil-gas separating tower for processing after being subjected to tunnel cooling (the exchanged heat can be used for geothermal energy of raw materials yards), collected noncondensable gas, namely wood gas, serves as a thermal cracking fuel, and condensed fluid serves as an important by-product of the production.
Description
Affiliated technical field
The biomass carbonization technology that belongs to the clean energy field.Be particularly suitable for biomass are made charcoal fuel, wood gas, wood tar oil, wood vinegar as raw material.
Background technology
The thermal cracking processes of biomass can be divided into four-stage:
Pre-heating stage: (room temperature-100 degree) heats biomass from room temperature, in biomass-based variation of only having temperature of this one-phase.
Water smoking: physical change just occurs in these one-phase biomass in (100-160 degree), mainly dries out.
The thermo-cracking stage: in these one-phase biomass decomposes under anoxia condition, along with the continuous rising of temperature, various volatile matters are corresponding separates out (160-500 degree), and most mass loss occurs raw material.
Calcination stage: (＞500 degree) are very slow in the decomposition that this one-phase occurs, and the mass loss of generation is more much smaller than subordinate phase, usually are considered to that the further cracking of C-C key and c h bond causes this stage.Calcining can improve the intensity of charcoal.
So that the biomass through pyrolysis of fuel as purpose to be provided, generally do not need to calcine, the production cycle be can shorten like this, volatile matter and hydrogen content improved, also be convenient to the mechanical deep processing of charcoal.
Take the timber biological raw material as example: begin violent heat scission reaction after temperature is higher than 160 degree, hemicellulose begins thermopositive reaction about 220 degree, and Mierocrystalline cellulose begins thermopositive reaction about 275 degree, and xylogen is in 310 degree beginning thermopositive reaction.
Biomass through pyrolysis can be divided at a slow speed thermo-cracking, conventional thermo-cracking, fast pyrolysis, flash pyrolysis according to heat-up rate and final carbonization temperature.The thermo-cracking main purpose is to produce charcoal (30% quality output) at a slow speed, the fast pyrolysis main purpose is produce oil (the highest 80% quality output), the flash pyrolysis main purpose is aerogenesis (the highest 80% quality output), and conventional thermo-cracking then charcoal, oil, gas is all produced (each 1/3rd quality output).Fast pyrolysis, flash pyrolysis generally need outer heat to heat up and could regulate heat-up rate.
Be lower than (0.1～1 ℃/s) thermo-cracking of 600 ℃ moderate temperature and medium speed of reaction, be conventional thermo-cracking, can be made into gas, liquid and the solid phase prod of same ratio, namely 3 tons of biomass dry-matteies can be produced 1 ton of combustible gas, 1 ton of bio oil and 1 ton of charcoal.
The conventional mode of production has two kinds of continous way and intermittent types, and heat-supplying mode has two kinds of internal heat type and external-heats.Continuous process is general with reference to ripe fluidized-bed process and (two) tower process, is characterized in that the waste heat in continuously feeding and discharging, the production process can rationally utilize.But for biomass through pyrolysis, utilizing thermal cracking products if will reach direct circulation----not condensable inflammable gas can only adopt external-heat or mix heat supply, otherwise the continuous accumulation of carbon dioxide will make the inflammable gas of recovery lose utility value.The continous way investment of production is generally larger, also is unfavorable for small-scale production.
Traditional charcoal kiln, modern independently charring furnace are exactly the Typical Representative of batch production, and its deficiency is to fully utilize heat energy, and productivity is not high, and environment is had certain disadvantageous effect, generally only obtain the charcoal product and can not obtain bio oil and combustible gas product.Its advantage is to be convenient to low cost construction, to produce, copy.
As seen: low investment and production cost, comprehensive cyclic utilization heat energy, all reclaiming the clearer production technology of thermal cracking products, is exactly pursuing a goal of biomass through pyrolysis.
Summary of the invention:
The invention solves the problem that the intermittent type charring furnace generally can not carry out mass transfer and heat transfer between stove, with charring furnace group cooperative work mode, by the organic connections of mass-and heat-transfer between the intermittent type charring furnace, realize High-efficient Production.Utilize the wood gas that produces in producing to realize the burner hearth heat supply, and flue gas and pyrolysis oil gas are processed respectively, fully utilize whole pyrolysis products, improve thermo-efficiency, improve profit for output value, also realize cleaner production.
Description of drawings:
Fig. 1 has described charring furnace all living creatures production art relation, wherein: 1. being coking chamber, 2. is the air intlet switch, 3. goes out air cock for burner hearth flue gas and coking chamber flue gas, 4. be coking chamber pyrolysis oil gas gate out switch, 5. being multistage oil gas condensation tower, 6. being condensable gases supercharging device (such as the jet flow pressurizing pump) not, 7. is the wood gas storage tank, 8. be the burner hearth ignition switch, 9. being vacuum fan, 10. is the coking chamber temperature indicating device
Be mass transfer channel switch between stove,
Be heat transfer path switch between stove,
Be material storage yard,
Lead to liquid sump,
Be condensable gases not,
Be the flue gas main pipe line,
Be oil gas master tunnel
Fig. 2 is the coking chamber section of structure that furnace bottom arranges burner hearth, wherein: 1. sealing plate, 2. 3. the air blast inlet is coking chamber, 4. be the charing cage, 5. being the wood gas pipeline opening, 6. is the metal furnaces plate, 7. is refractory heat isolating plate, 8. be refractory brick marshalling, 9. being heat transfer pipe, 10. is ir radiation an electrical ignition element stove
Be by heat transfer plate in the charing cage (charing cage hour do not install),
Be the heat-transfer pipe protective shield.
Fig. 3 is the charring furnace left side sectional view, and wherein: 1. being the mass transfer channel switch, 2. is the oil gas internal passages, 3. is the oil gas outlet at bottom, 4. is burner hearth.
Fig. 4 is the charring furnace right side sectional view, and wherein: 1. being the mass transfer channel switch, 2. is the oil gas internal passages, 3. is the oil gas top inlet, 4. is burner hearth.
Fig. 5 is the switch junctions composition, and wherein: 1. being sealing liquid, 2. is gas port, 3. sealing groove, 4. switch cover plate, 5. suspension ring (can be designed to movable).
Fig. 6 mass transfer gas channel schematic diagram, wherein: 6. be the gather qi together passage, 7. be air inlet or production well.
Fig. 7 is the two channel switch schematic diagram, and the switch on the passage one is taken out, and then passage one and passage two are communicated with, and wherein: 8. being sealing liquid, 9. is passage one, 10. is passage two.
Fig. 8 is refractory heat isolating plate, when the coking chamber topside area is little, can not establish air switch on the refractory heat isolating plate, also can only use a whole plate.Wherein, 1. be the air intlet switch, 2. refractory heat-insulating divides plate.
Fig. 9 is seal cover board, according to coking chamber topside area size, uses 1,2 or polylith, will guarantee its sealing effectiveness during technological design.Wherein: 1. be sealing minute plate, 2. heat-insulating and sealing groove.
Coking chamber vertical view when Figure 10 is the burner hearth side, 1. sealing plate wherein, 2. 3. the air blast inlet is burner hearth and coking chamber exhanst gas outlet switch, 4. is coking chamber oil gas vent switch, 5. be ir radiation an electrical ignition element stove, 6. 7. the mass transfer channel switch is the heat transfer path switch, 8. is temperature indicating device, 9. being the burner hearth ignition switch, 10. is burner hearth metal heat transfer plate.
Coking chamber sectional view when Figure 11 is the burner hearth side, wherein: 1. sealing plate, 2. 3. the air blast inlet is ir radiation an electrical ignition element stove, 4. be coking chamber, 5. be burner hearth metal heat transfer plate, 6. 7. the charing cage is the burner hearth blast tube, 8. refractory heat isolating plate, 9. be mass transfer, heat transfer path and switch, 10. heat transfer pipe
Be refractory brick marshalling,
Be the heat-transfer pipe protective shield,
Charing cage heat transfer plate.
Figure 12 is oil gas master tunnel vertical view, and wherein: 1. being oil and gas import, 2. is the maintenance bypass mouth, 3. is condensate pipe.
Figure 13 is oil gas master tunnel sectional view, and wherein: 1. being sealing cover, 2. is condensate pipe.
Embodiment:
The pyrolysis oven of this patent design belongs to the batch production pyrolysis oven, but works its main production process following (Fig. 1) in stove group's mode:
Coking chamber (ABCD) 1. in the inner biomass that install of charing cage (Fig. 2), with A coking chamber air blast inlet 2. (Fig. 5) open (then must not close 2. when not needing the spontaneous combustion heat supply), with mass transfer between stove
Conduct heat
Passage (Fig. 3, Fig. 4, Fig. 6, Fig. 7) is communicated with, close straight-through export 3. (Fig. 5) of flue gas, oil gas of burner hearth and coking chamber, start vacuum fan 9., the hearth combustion device is lighted or lighted to biomass in the charing cage, build ABCD coking chamber cover plate (Fig. 8, Fig. 9) 1..2. same at present 3 roads (BCD) operation charring furnace closes blast inlet, the outlet that the charring furnace in lower 2 roads (BC) is closed all straight-through flue gases, oil gas 3., only open mass-and heat-transfer passage between stove, and the charring furnace of lower the 3rd road (D) operation will be opposite, close and the stove of lower road (E) operation between the mass-and heat-transfer passage, open flue gas, the straight-through outlet of oil gas 3..Along with the intensification of coking chamber A, realize conducting heat by the mass-and heat-transfer passage, make biomass in B, C, three coking chambers of D, as continous way is produced, progressively realize preheating, dehydration, preliminary thermo-cracking.By the apparent survey of monitoring temperature, (310～500 sufficiently long times of degree of carbonization temperature are kept in the thermo-cracking heat release to machine in due course, determined by biomass kind and bore thickness), stop spontaneous combustion heat supply (closing the blast inlet of A) or burner hearth heat supply (after certain hour is carried out in production, after 7. the wood gas holding tank stores enough combustion gas, can not carry out the spontaneous combustion heat supply, and all adopt the burner hearth gas heating), machine is lighted the heat supply of B charring furnace and is entered main thermo-cracking when appropriate, when B coking chamber temperature is higher than the A chambers temp, open first the straight-through outlet of oil gas of A 3., close again the mass-and heat-transfer passage between AB; Then open mass-and heat-transfer passage between the stove between DE, close mass-and heat-transfer passage between the stove between EF, open the straight-through outlet of flue gas, oil gas of E 3., close the straight-through outlet of flue gas, oil gas of D 3..So therefore continuous circulation requires production line necessary end to end, links to each other such as annulus arrangement or biserial.
When the A chambers temp is reduced to oil gas and the straight-through outlet of flue gas that 70 degree are closed A when following, the charing cage is lifted out, the transfer charcoal is further lowered the temperature the charing cage of packing into and installing biomass in A.When A stops thermo-cracking and enters the process of cooling, can take to open the straight-through outlet of burner hearth flue gas and accelerate cooling, also can use the flowing water cooling at the coking chamber cover plate.
The coking chamber installation form has three kinds: pile up formula on the ground, half piles up formula on the ground, and formula is built in underground hole.Ground type generally takes to divide into burner hearth, and half ground or underground type are generally taked side burner hearth (Figure 10, Figure 11) design, save metal consumption, avoid the boiler face load-bearing, increase the service life, and reduce maintenance cost.
The hearth combustion device is with biomass infrared gas electronic oven best results, and efficient is high, quick heating and convenient control.
Oil gas master tunnel (Figure 12, Figure 13) can be on top, tunnel and the default water pipe cooling in side (realize the one-level gas-oil separation, improve gas and oil separating plant efficient 5.), can arrange in the side safeguard with observation near coal-mine.With the vacuum fan place that communicates, select about designing so that oil gas stroke in the circular channel is long, good cooling effect.
Flue both can adopt the tunnel, also can buy large diameter pipeline and install, and general exhanst gas outlet can design in the biomass stockyard, utilizes the waste heat dried biomass, also can directly be communicated with the rear discharging of pond cooling.
6. the wood gas supercharging device is generally the jet flow pressurizing pump.Wood gas holding tank device pressure setting 7. generally will meet the requirement of stove and accessory.
Coking chamber is two layers of cover plate of upper design 1., the cover plate of the superiors is the heat insulation cover plate of light sealing (Fig. 9) (generally being designed to integral slab or quarter stuff), mainly play sealing heat insulation, seal means recommends to take fluid-tight (such as water seal), and lower floor's cover plate (Fig. 8) mainly satisfies fire-resistant requirement, is generally metal sheet, can be designed to polylith according to surface size, with handled easily, when lowering the temperature, should satisfy by needs the needs of flowing water cooling.When coking chamber plane 1. is long-pending little, can not design ventilation opening on the refractory heat-insulating cover plate.
Charing cage key points in design is (Fig. 2): the mobile needs of lifting are satisfied in the theory of structures design, the all-metal framework satisfies the heat transfer needs, upper opening satisfies filling material needs, bottom metal can not wide-bore, the side metal plate can be slotted or the cloth hole, so that pyrolysis mass transfer (steam or oil gas).Heat transfer plate can be designed in the cage middle part, and the enhance heat transfer ability also can play the effect that strengthens structure, but filling material and discharging are had certain influence.The charing cage also is the charring furnace inner bag.
In the time of in carbonization temperature 500 degree, the wood gas of system can satisfy need of production fully.If native system is mainly used in produce oil, then want the rational deployment coking chamber, arrange enough coking chamber aerogenesis, want science to calculate wood gas holding tank capacity 7. simultaneously.
The coking chamber blast inlet is designed to odd number, is control temperature and heat-up rate when making things convenient for spontaneous combustion.Standard-sized sheet during beginning, oxygen-supplying amount is large, begins to reduce air intake after temperature rises to 160 degree, particularly after temperature rises to 300 degree, generally only stays an air port just to close after for some time, enters the anaerobic charing.When system's wood gas is sufficient, do not carry out the spontaneous combustion heat supply, all blast inlet whole process are closed.
Mass transfer channel between stove: last oven carbonization chamber right upper portion (Fig. 4) is opened oil gas vent, related with the oil and gas import in this oven carbonization chamber left side by mass transfer channel switch between stove, the outlet of oil and gas import is beneficial to increase the heat transfer stroke in the bottom of coking chamber, strengthens heat-transfer effect.
Heat transfer path between stove: heat transfer pipe adopts bend pipe, the vertical or horizontal coking chamber periphery (Fig. 2, Figure 11) that is arranged at, import is at burner hearth, exports a heat transfer path between stove (opening during heat transfer), one flue gas main pipe line (opening during cooling).Recommend to install protective shield protection heat transfer pipe.
Chamber design requires: biomass ir radiation an electrical ignition element stove and accessory, in the quantity of burner hearth layout, should determine according to the production technique needs.General requirement can be regulated firepower by automatic or manual, and the highest furnace temperature generally can not be higher than 1000 degree.The steam line size is according to the air supply requirement calculative determination, and is relevant with the burner hearth quantity that the maximum air demand of single burner hearth and stove group work simultaneously.Size and the thickness of burner hearth metal heat transfer face can calculate according to the highest heat-up rate of system's heat transfer, furnace temperature.
The vacuum fan design requirements: steam or oil gas always lead to the low outlet of pressure in the coking chamber, and general requirement axially produces enough negative pressure, make pyrolysis gas gas phase retention time within the scope of processing requirement.The gas phase retention time is also relevant with the windage of wind path, must integrated design.
In design, construction and producing, guarantee the realization of anaerobic charing environment, note sealing.
For accelerating charing rate, reduce the production cycle, also can take other process meanses such as biomass are chipped, correct layout biomass.
Claims (10)
1. the system of the energy intermittent type charring furnace cleaner production charcoal fuel that mass transfer, heat transfer, cluster use between charring furnace and wood vinegar, wood tar oil.It is characterized in that: charring furnace is with stove group's mode work (Fig. 1), namely when working by the charring furnace of spontaneous combustion or burner hearth ignition, open follow-up not several charring furnaces of igniting with mass-and heat-transfer switch between stove, with mass transfer channel mass-and heat-transfer simultaneously, progressively realize being opened biomass preheating in the follow-up charring furnace of contact, drying or tentatively pyrolysis when conducting heat with heat transfer path.System carries out separating treatment with oil gas, can not provide burner hearth to act as a fuel as combustion gas by the condensation composition, and the condensation composition is as byproduct.
2. according to claim 1 being characterised in that: charring furnace both can obtain heat energy (2. Fig. 1 blast inlet advances oxygen) by heat in the spontaneous combustion, also can pass through burner hearth heat supply (Fig. 2, Figure 10, Figure 11).The used combustion gas of hearth combustion derives from the wood gas (Fig. 1 device 6., 7.) of systematic collection.The production initial stage finishes after the production of 3～5 stoves take the spontaneous combustion heat supply as main, can use the burner hearth heat supply instead.
3. according to claim 1 being characterised in that: the charring furnace group processes respectively (the flue gas main pipe line among Fig. 1 with the flue gas that spontaneous combustion, hearth combustion produce with the oil gas of pyrolysis generation
Oil gas master tunnel
The flue gas that the production initial stage can produce spontaneous combustion almost do not have dust emissions, and after taking the burner hearth heat supply, dust is just fewer, can reach in line requirement fully through filtration, the absorption of follow-up a plurality of coking chambers, and flue gas can be directly used in the dried biomass raw material.Oil gas enters the gas-oil separation tower after through tunnel oil gas groove water-cooled again and processes, except 7. defocused can not the condensation composition acting as a fuel be collected in device, for hearth combustion.
4. according to claim 1 being characterised in that: mass transfer, heat transfer path (mass transfer switch between Fig. 1 stove have been installed between adjacent charring furnace
The heat transfer switch
Fig. 2, Fig. 3, Fig. 4, Fig. 5, Fig. 6, Fig. 7).Heat transfer path only conducts heat with thermal conduction, thermal radiation mode by warm air, and mass transfer channel reaches the purpose of heat transfer by the oil gas transmission.
5. according to claim 1 being characterised in that: but charring furnace both built on the ground, also semi-underground building also can be selected in full hypogee.Generally take side chamber design (Figure 10, Figure 11) during full hypogee, generally take furnace bottom that burner hearth (Fig. 2) is set during surface structures, and semi-underground building burner hearth both can be arranged at furnace bottom and also can be arranged at the side.
6. according to claim 1 being characterised in that: owing to adopting hearth combustion heat supply (external-heat), can control as required heat-up rate, not only adapt to conventional thermo-cracking, also can carry out fast pyrolysis or flash pyrolysis, satisfy different need of productions.
7. according to claim 1 being characterised in that: heat transfer path conducts heat in pyrolytic process, and the heat transfer after pyrolysis finishes can help the coking chamber fast cooling (to close between stove and conduct heat
Opening the flue gas main pipe line 3. conducts heat).
8. according to claim 1 being characterised in that: oil gas master tunnel (Figure 12, Figure 13) facility, can effectively carry out the one-level condensation to oil gas, but science control oil gas condensation path length.The tunnel is designed with the service port (Figure 13) of bypass, is convenient to clear up the tar of poor fluidity, prevents that the tunnel from stopping up, and also is convenient to clear up the tar on the condensate pipe, ensures condensation effect.
9. according to claim 1 being characterised in that: after the oil gas master tunnel condensation, oil gas passes through multi-grade oil gas disposal tower (device 5. among Fig. 1) (being not limited to three grades) again, can effectively collect tar and wood vinegar.
10. according to claim 1 being characterised in that: heat transfer pipe can adopt bend pipe (Fig. 2, Figure 11), and horizontal or vertical layout is at coking chamber, and the bend pipe outside can increase protection metal sheet (with holes) and protect.The heat transfer pipe import is at burner hearth, outlet heat transfer path (Fig. 1) between stove, and an outlet is at flue gas main pipe line (Fig. 1).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2012100876261A CN103361085A (en) | 2012-03-29 | 2012-03-29 | Cleaner production system of carbonization furnace group |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2012100876261A CN103361085A (en) | 2012-03-29 | 2012-03-29 | Cleaner production system of carbonization furnace group |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN103361085A true CN103361085A (en) | 2013-10-23 |
Family
ID=49363366
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2012100876261A Pending CN103361085A (en) | 2012-03-29 | 2012-03-29 | Cleaner production system of carbonization furnace group |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN103361085A (en) |
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105131977A (en) * | 2014-06-04 | 2015-12-09 | 袁承世 | Linear mobile continuous destructive distillation kettle carbonization furnace |
| CN105154116A (en) * | 2015-09-24 | 2015-12-16 | 蓝山县鑫旺竹业有限公司 | Method and system for recycling bamboo dust and application of obtained product |
| CN105423316A (en) * | 2015-11-30 | 2016-03-23 | 桃江县金杰生物能源有限公司 | Smoke purifying device |
| CN106883869A (en) * | 2017-03-21 | 2017-06-23 | 张成礼 | A kind of environment-friendly biomass burner |
| CN115648373A (en) * | 2022-11-07 | 2023-01-31 | 哈尔滨师范大学 | Ecological slope anti-corrosion timber pile and treatment device and treatment method thereof |
Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB563461A (en) * | 1943-01-05 | 1944-08-15 | Oswald Heller | Improvements relating to the manufacture of charcoal |
| CN2038907U (en) * | 1988-07-26 | 1989-06-07 | 李柏寿 | Combined device for coking and metal ball |
| CN2203302Y (en) * | 1994-12-08 | 1995-07-12 | 王长生 | Small heat-exchange type continuous coke furnace |
| CN2585861Y (en) * | 2002-12-06 | 2003-11-12 | 刘英旺 | Wholly enclosed twin and specially-made shape coke continuous coke discharge over |
| JP2004239162A (en) * | 2003-02-06 | 2004-08-26 | Cyc:Kk | Biomass power generation system |
| CN101519598A (en) * | 2009-02-09 | 2009-09-02 | 李观德 | Method and system for waste therophyte high-efficiency clean environment-protective cycled comprehensive utilization |
| CN101979463A (en) * | 2010-10-26 | 2011-02-23 | 山西省化工设计院 | Clean heat reclamation tamping type coke furnace |
-
2012
- 2012-03-29 CN CN2012100876261A patent/CN103361085A/en active Pending
Patent Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB563461A (en) * | 1943-01-05 | 1944-08-15 | Oswald Heller | Improvements relating to the manufacture of charcoal |
| CN2038907U (en) * | 1988-07-26 | 1989-06-07 | 李柏寿 | Combined device for coking and metal ball |
| CN2203302Y (en) * | 1994-12-08 | 1995-07-12 | 王长生 | Small heat-exchange type continuous coke furnace |
| CN2585861Y (en) * | 2002-12-06 | 2003-11-12 | 刘英旺 | Wholly enclosed twin and specially-made shape coke continuous coke discharge over |
| JP2004239162A (en) * | 2003-02-06 | 2004-08-26 | Cyc:Kk | Biomass power generation system |
| CN101519598A (en) * | 2009-02-09 | 2009-09-02 | 李观德 | Method and system for waste therophyte high-efficiency clean environment-protective cycled comprehensive utilization |
| CN101979463A (en) * | 2010-10-26 | 2011-02-23 | 山西省化工设计院 | Clean heat reclamation tamping type coke furnace |
Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105131977A (en) * | 2014-06-04 | 2015-12-09 | 袁承世 | Linear mobile continuous destructive distillation kettle carbonization furnace |
| CN105154116A (en) * | 2015-09-24 | 2015-12-16 | 蓝山县鑫旺竹业有限公司 | Method and system for recycling bamboo dust and application of obtained product |
| CN105154116B (en) * | 2015-09-24 | 2018-05-29 | 蓝山县鑫旺竹业有限公司 | A kind of application of the reuse method of bamboo scraps, system and products therefrom |
| CN105423316A (en) * | 2015-11-30 | 2016-03-23 | 桃江县金杰生物能源有限公司 | Smoke purifying device |
| CN105423316B (en) * | 2015-11-30 | 2019-04-12 | 桃江县金杰生物能源有限公司 | A kind of flue gas purification device |
| CN106883869A (en) * | 2017-03-21 | 2017-06-23 | 张成礼 | A kind of environment-friendly biomass burner |
| CN115648373A (en) * | 2022-11-07 | 2023-01-31 | 哈尔滨师范大学 | Ecological slope anti-corrosion timber pile and treatment device and treatment method thereof |
| CN115648373B (en) * | 2022-11-07 | 2023-08-04 | 哈尔滨师范大学 | Ecological side slope anti-corrosion wood pile and processing device and processing method thereof |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN102776007A (en) | Continuous biomass pyrolytic carbon gas-oil poly-generation system | |
| CN103361085A (en) | Cleaner production system of carbonization furnace group | |
| CN105062521A (en) | Rotary-type continuous pyrolyzing straw carbonizing furnace | |
| CN102766476B (en) | Multi-layer upright tower type duff dust and oil shale distillation plant with stirring function and process | |
| CN203487080U (en) | Internal heated vertical retort | |
| CN102964884B (en) | Hot cracking method process for preparing carbon black by using co-production of tail gas | |
| CN102925180B (en) | Oil shale external heat radiation type retort | |
| CN204939394U (en) | Rotary type continuous pyrolysis stalk coke oven | |
| CN202482249U (en) | Coal pyrolysis furnace | |
| CN107022363A (en) | A kind of continuous biomass pyrolysis gas is reversely flowd back towards with charcoal gas cogeneration facility | |
| CN207738699U (en) | A kind of gas complete alternation distillation system for the long flame dry distillation of coal | |
| CN105482837B (en) | A kind of bamboo material continuous carbonization furnace | |
| CN102994104B (en) | Coal pyrolysis furnace | |
| CN205560759U (en) | Mechanical stoker formula waste gasification burns dual -boiler power generation system | |
| CN104804752A (en) | Timber continuous carbonization and gasification method and device | |
| CN202849331U (en) | Multi-layer vertical tower fine coal and oil shale destructive distillation production device with stirring | |
| CN205473575U (en) | Continuous retort of bamboo material | |
| CN105464727A (en) | Boiler power generation system utilizing rubbish gasification and incineration synthesis gas | |
| CN205560769U (en) | Mechanical stoker formula waste gasification burns dual -boiler energy -saving power generation system | |
| CN205560768U (en) | Mechanical stoker formula waste gasification incineration boiler power generation system | |
| CN205560758U (en) | Double -deck mechanical stoker formula waste gasification incineration boiler power generation system | |
| CN105588131A (en) | Mechanical fire grate type rubbish gasification incinerator and dual-boiler energy-saving power generation system thereof | |
| CN205560767U (en) | Double -deck mechanical stoker formula waste gasification burns dual -boiler power generation system | |
| CN105465789A (en) | Dual-layer mechanical grate type garbage gasifying incinerator and dual-boiler power generation system thereof | |
| CN205558990U (en) | Utilize waste gasification to burn boiler power generation system of synthetic gas |
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: 20131023 |