CN102010731A - Pyrolytic process of coal - Google Patents
Pyrolytic process of coal Download PDFInfo
- Publication number
- CN102010731A CN102010731A CN2010105596200A CN201010559620A CN102010731A CN 102010731 A CN102010731 A CN 102010731A CN 2010105596200 A CN2010105596200 A CN 2010105596200A CN 201010559620 A CN201010559620 A CN 201010559620A CN 102010731 A CN102010731 A CN 102010731A
- Authority
- CN
- China
- Prior art keywords
- coal
- pyrolysis
- pyrolytic process
- heating
- temperature
- 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.)
- Granted
Links
- 239000003245 coal Substances 0.000 title claims abstract description 82
- 238000000034 method Methods 0.000 title claims abstract description 16
- 238000000197 pyrolysis Methods 0.000 claims abstract description 33
- 238000010438 heat treatment Methods 0.000 claims abstract description 32
- 239000007789 gas Substances 0.000 claims abstract description 26
- 239000011280 coal tar Substances 0.000 claims abstract description 17
- 238000006243 chemical reaction Methods 0.000 claims abstract description 15
- 239000001257 hydrogen Substances 0.000 claims abstract description 10
- 229910052739 hydrogen Inorganic materials 0.000 claims abstract description 10
- 239000011449 brick Substances 0.000 claims description 9
- 239000003034 coal gas Substances 0.000 claims description 8
- 230000001186 cumulative effect Effects 0.000 claims description 7
- CPLXHLVBOLITMK-UHFFFAOYSA-N Magnesium oxide Chemical compound [Mg]=O CPLXHLVBOLITMK-UHFFFAOYSA-N 0.000 claims description 6
- NBIIXXVUZAFLBC-UHFFFAOYSA-N Phosphoric acid Chemical group OP(O)(O)=O NBIIXXVUZAFLBC-UHFFFAOYSA-N 0.000 claims description 6
- 239000000835 fiber Substances 0.000 claims description 6
- 239000003077 lignite Substances 0.000 claims description 6
- 239000007769 metal material Substances 0.000 claims description 4
- VYZAMTAEIAYCRO-UHFFFAOYSA-N Chromium Chemical compound [Cr] VYZAMTAEIAYCRO-UHFFFAOYSA-N 0.000 claims description 3
- RYGMFSIKBFXOCR-UHFFFAOYSA-N Copper Chemical compound [Cu] RYGMFSIKBFXOCR-UHFFFAOYSA-N 0.000 claims description 3
- YKTSYUJCYHOUJP-UHFFFAOYSA-N [O--].[Al+3].[Al+3].[O-][Si]([O-])([O-])[O-] Chemical compound [O--].[Al+3].[Al+3].[O-][Si]([O-])([O-])[O-] YKTSYUJCYHOUJP-UHFFFAOYSA-N 0.000 claims description 3
- 229910000147 aluminium phosphate Inorganic materials 0.000 claims description 3
- 239000000919 ceramic Substances 0.000 claims description 3
- 229910052802 copper Inorganic materials 0.000 claims description 3
- 239000010949 copper Substances 0.000 claims description 3
- 239000000395 magnesium oxide Substances 0.000 claims description 3
- 150000003839 salts Chemical class 0.000 claims description 3
- 229910001220 stainless steel Inorganic materials 0.000 claims description 3
- 239000010935 stainless steel Substances 0.000 claims description 3
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 claims 2
- 125000004435 hydrogen atom Chemical class [H]* 0.000 claims 1
- 229910052742 iron Inorganic materials 0.000 claims 1
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 abstract description 6
- 239000000463 material Substances 0.000 abstract description 3
- 238000004519 manufacturing process Methods 0.000 description 4
- 150000002431 hydrogen Chemical class 0.000 description 3
- 239000011269 tar Substances 0.000 description 3
- 238000002485 combustion reaction Methods 0.000 description 2
- 230000009466 transformation Effects 0.000 description 2
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 description 1
- 238000003763 carbonization Methods 0.000 description 1
- 239000000571 coke Substances 0.000 description 1
- 230000000052 comparative effect Effects 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 238000000354 decomposition reaction Methods 0.000 description 1
- 230000002950 deficient Effects 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 238000002309 gasification Methods 0.000 description 1
- 230000008676 import Effects 0.000 description 1
- 238000009434 installation Methods 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 238000006068 polycondensation reaction Methods 0.000 description 1
- 239000000843 powder Substances 0.000 description 1
- 238000001149 thermolysis Methods 0.000 description 1
Landscapes
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
- Muffle Furnaces And Rotary Kilns (AREA)
Abstract
一种煤的热解工艺，其特征在于包括如下步骤：首先选取原料煤，放入外热式回转炉，所述回转炉的炉体包括外壁和内壁两层，然后向所述外壁和内壁之间的空间通入循环煤气，通过控制所述循环煤气的通入量将升温速度控制为20-100℃/min，至炉内温度达到650℃-700℃，煤层在此温度下进行热解反应直至反应完全后收集热解产物，分离煤焦油和氢气后，将煤气循环至循环煤气入口处。A coal pyrolysis process, which is characterized in that it includes the following steps: first select raw coal, put it into an externally heated rotary furnace, the furnace body of the rotary furnace includes two layers of outer wall and inner wall, and then transfer the material between the outer wall and the inner wall Circulating gas is fed into the space between them, and the heating rate is controlled to 20-100°C/min by controlling the amount of circulating gas, until the temperature in the furnace reaches 650°C-700°C, and the coal seam undergoes pyrolysis reaction at this temperature After the reaction is complete, the pyrolysis products are collected, and after the coal tar and hydrogen are separated, the gas is recycled to the inlet of the circulating gas.
Description
Technical field
The present invention relates to a kind of pyrolytic process, relate in particular to a kind of pyrolysis of coal technology.
Background technology
The pyrolysis of coal also claims coal carbonization or thermolysis.The pyrolysis of coal is that coal is heated under the condition of secluding air as a kind of independent working method, and the complex process of series of physical variation and chemical reaction takes place under differing temps coal, and its product mainly is coal gas, tar, crude benzol and coke or semicoke.By the warm eventually difference of its heating, can be divided into: low temperature (500-700 ℃), middle temperature (700-1000 ℃) and high temperature (1000-1200 ℃) pyrolysis.
Compare with gasification with liquidation of coal, its processing conditions gentleness, less investment, production cost is low.The coal that is suitable for low temperature pyrogenation is generally low-rank coal, comprises the non caking coal of brown coal, long-flame coal and high volatile.The low-rank coal reserves of China are bigger, account for more than 42% of whole coals, and therefore, the low temperature pyrogenation technology can effectively be utilized the resource of China, and can reduce the environmental pollution that fire coal causes.
In the pyrolytic reaction process of coal, rate of heating and heat supply condition have very big influence to product yield and composition, and in addition, the lumpiness of coal also has certain influence to pyrolysis product, and the lumpiness of general coal increases, and tar yield reduces.Existing pyrolysis of coal technology generally adopts the vertical type stove, and it requires feed coal is lump coal, has limited the application of powder coal, and existing pyrolytic reaction, especially external-heat reaction, its heat generally needs the combustion chamber to supply with, increased the production cost of pyrolytic process virtually, and technology is comparatively complicated.
Summary of the invention
The object of the present invention is to provide a kind of pyrolytic process of coal, have that production cost is low, rate of heating is fast, transformation efficiency coal significantly improves, and the advantage of coal tar gain in yield.
Its concrete technical scheme is as follows:
A kind of pyrolytic process of coal, comprise the steps: at first to choose feed coal, put into the external-heating revolving stove, the body of heater of described rotary kiln comprises that outer wall and inwall are two-layer, space between described outer wall and inwall feeds circulating gas then, by the feeding amount of controlling described circulating gas heat-up rate is controlled to be 20-100 ℃/min, temperature reaches 650 ℃-700 ℃ to the stove, the coal seam is carried out pyrolytic reaction and is collected pyrolysis product until the back that reacts completely under this temperature, after separating coal tar and hydrogen, coal gas is circulated to the circulating gas ingress.
The amount of feed coal accounts for 1/5～1/3 of body of heater cumulative volume in the described body of heater, guarantees that feed coal can overturn in stove fully.
Described feed coal is brown coal, long-flame coal, non-caking coal or weakly caking coal.
Described furnace body outer wall can be selected any heat-resisting and thermal conductivity materials with smaller for use, constitute as light-weight refractory insulating brick or fully fibrous structure, guarantee that heat can not be dispersed into the body of heater outside, described light-weight refractory insulating brick can be phosphoric acid block salt, magnesia chrome brick etc., and described fully fibrous structure can be made of ceramic fiber, aluminum silicate fiber etc.; Described inwall can be selected any heat-resisting and material that thermal conductivity is higher for use, as pottery or various metallic substance, can be stainless steel, copper etc., guarantees the coal seam that heat can well be in inwall imports stove into.
At the pyrolysis of coal initial stage, promptly temperature is less than 300 ℃ the time, and described rate of heating is preferably 20-60 ℃/min; In pyrolysis of coal mid-term, promptly temperature is in the time of 300-450 ℃, and described rate of heating is preferably 50-70 ℃/min; In the pyrolysis of coal later stage, promptly temperature is in the time of 451-700 ℃, and described rate of heating is preferably 70-100 ℃/min.
Compared with prior art, pyrolysis of coal technology of the present invention has following characteristics:
1) adopt the rate of heating that changes, the initial stage rate of heating is slower, and ature of coal is long at the low-temperature range heated time, the selectivity of pyrolytic reaction is stronger, the initial stage pyrolysis disconnects key more weak in the coal molecule, and thermal polycondensation reaction parallel and order has taken place, and has formed the structure of Heat stability is good; At the hot stage decomposition of little, when adopting rapid heating, corresponding structure is decomposed many;
2) adopt the external-heating revolving stove as pyrolysis installation, overcome the defective that the vertical type stove only can pyrolysis lump coal, make the transformation efficiency of coal and tar yield significantly improve;
3) adopt circulating gas as heating medium, saved production cost greatly, and make technology obtain simplifying.
Embodiment
Below by embodiment technical scheme of the present invention is described in further detail, but is not limited to the content of present embodiment.
Embodiment 1
Choose Inner Mongol brown coal, put into the external-heating revolving stove, account for 1/5 of body of heater cumulative volume until the amount of feed coal, the body of heater of described rotary kiln comprises that outer wall and inwall are two-layer, space between described outer wall and inwall feeds circulating gas then, makes it carry out pyrolysis to the intravital coal of stove; By the feeding amount of controlling described circulating gas heat-up rate is controlled to be 30 ℃/min, when temperature rises to 300 ℃, adjusting rate of heating is 50 ℃/min, when temperature rises to 450 ℃, adjust rate of heating and be 100 ℃/min temperature to the stove and reach 650 ℃-700 ℃, the coal seam is carried out pyrolytic reaction and is collected pyrolysis product until the back that reacts completely under this temperature, separate coal tar and hydrogen after, coal gas is circulated to the circulating gas ingress, and wherein the coal tar productive rate is 20.8%.
Described furnace body outer wall is made of light-weight refractory insulating brick or fully fibrous structure, and described light-weight refractory insulating brick is phosphoric acid block salt, magnesia chrome brick etc., and described fully fibrous structure is made of ceramic fiber, aluminum silicate fiber etc.; Described inwall is selected pottery or various metallic substance for use, and it is stainless steel, copper etc.
Embodiment 2
Choose Datong District's weakly caking coal, put into the external-heating revolving stove, account for 1/3 of body of heater cumulative volume until the amount of feed coal, the body of heater of described rotary kiln comprises that outer wall and inwall are two-layer, space between described outer wall and inwall feeds circulating gas then, makes it carry out pyrolysis to the intravital coal of stove; By the feeding amount of controlling described circulating gas heat-up rate is controlled to be 20 ℃/min, when temperature rises to 300-450 ℃, adjusting rate of heating is 60 ℃/min, when temperature rises to more than 450 ℃, adjust rate of heating and be 80 ℃/min temperature to the stove and reach 650 ℃-700 ℃, the coal seam is carried out pyrolytic reaction and is collected pyrolysis product until the back that reacts completely under this temperature, separate coal tar and hydrogen after, coal gas is circulated to the circulating gas ingress, and wherein the coal tar productive rate is 21.5%.
All the other are with embodiment 1.
Embodiment 3
Choose refreshing mansion long-flame coal, put into the external-heating revolving stove, account for 1/3 of body of heater cumulative volume until the amount of feed coal, the body of heater of described rotary kiln comprises that outer wall and inwall are two-layer, space between described outer wall and inwall feeds circulating gas then, makes it carry out pyrolysis to the intravital coal of stove; By the feeding amount of controlling described circulating gas heat-up rate is controlled to be 60 ℃/min, when temperature rises to 300-450 ℃, adjusting rate of heating is 70 ℃/min, when temperature rises to more than 450 ℃, adjust rate of heating and be 90 ℃/min temperature to the stove and reach 650 ℃-700 ℃, the coal seam is carried out pyrolytic reaction and is collected pyrolysis product until the back that reacts completely under this temperature, separate coal tar and hydrogen after, coal gas is circulated to the circulating gas ingress, and wherein the coal tar productive rate is 22.0%.
All the other are with embodiment 1.
Embodiment 4
Choose Inner Mongol non-caking coal, put into the external-heating revolving stove, account for 1/4 of body of heater cumulative volume until the amount of feed coal, the body of heater of described rotary kiln comprises that outer wall and inwall are two-layer, space between described outer wall and inwall feeds circulating gas then, makes it carry out pyrolysis to the intravital coal of stove; By the feeding amount of controlling described circulating gas heat-up rate is controlled to be 40 ℃/min, when temperature rises to 300-450 ℃, adjusting rate of heating is 60 ℃/min, when temperature rises to more than 450 ℃, adjust rate of heating and be 70 ℃/min temperature to the stove and reach 650 ℃-700 ℃, the coal seam is carried out pyrolytic reaction and is collected pyrolysis product until the back that reacts completely under this temperature, separate coal tar and hydrogen after, coal gas is circulated to the circulating gas ingress, and wherein the coal tar productive rate is 20.3%.
All the other are with embodiment 1.
Embodiment 5
Choose Inner Mongol brown coal, put into the external-heating revolving stove, account for 1/4 of body of heater cumulative volume until the amount of feed coal, the body of heater of described rotary kiln comprises that outer wall and inwall are two-layer, space between described outer wall and inwall feeds circulating gas then, makes it carry out pyrolysis to the intravital coal of stove; By the feeding amount of controlling described circulating gas heat-up rate is controlled to be 50 ℃/min, when temperature rises to 300-450 ℃, adjusting rate of heating is 65 ℃/min, when temperature rises to more than 450 ℃, adjust rate of heating and be 85 ℃/min temperature to the stove and reach 650 ℃-700 ℃, the coal seam is carried out pyrolytic reaction and is collected pyrolysis product until the back that reacts completely under this temperature, separate coal tar and hydrogen after, coal gas is circulated to the circulating gas ingress, and wherein the coal tar productive rate is 21.2%.
All the other are with embodiment 1.
Comparative Examples
Choose Inner Mongol brown coal, put into the vertical type stove, the heat that produces by the combustion chamber heats pyrolysis to the coal seam, in temperature is 550 ℃, and normal pressure is reaction 85min down, generates coal tar and hydrogen, after the cooling, separate coal tar and hydrogen, wherein the coal tar productive rate is 15.6%.
Claims (8)
1. the pyrolytic process of a coal, it is characterized in that comprising the steps: at first choosing feed coal, put into the external-heating revolving stove, the body of heater of described rotary kiln comprises that outer wall and inwall are two-layer, space between described outer wall and inwall feeds circulating gas then, by the feeding amount of controlling described circulating gas heat-up rate is controlled to be 20-100 ℃/min, temperature reaches 650 ℃-700 ℃ to the stove, the coal seam is carried out pyrolytic reaction and is collected pyrolysis product until the back that reacts completely under this temperature, after separating coal tar and hydrogen, coal gas is circulated to the circulating gas ingress.
2. the pyrolytic process of coal according to claim 1 is characterized in that at the pyrolysis of coal initial stage, and promptly temperature is less than 300 ℃ the time, and described rate of heating is 20-60 ℃/min; In pyrolysis of coal mid-term, promptly temperature is in the time of 300-450 ℃, and described rate of heating is 50-70 ℃/min; In the pyrolysis of coal later stage, promptly temperature is in the time of 451-700 ℃, and described rate of heating is 70-100 ℃/min.
3. the pyrolytic process of coal according to claim 1 and 2 is characterized in that the amount of feed coal in the described body of heater accounts for 1/5～1/3 of body of heater cumulative volume.
4. the pyrolytic process of coal according to claim 1 and 2 is characterized in that described feed coal is brown coal, long-flame coal, non-caking coal or weakly caking coal.
5. the pyrolytic process of coal according to claim 1 and 2 is characterized in that described furnace body outer wall selects light-weight refractory insulating brick or fully fibrous structure for use, and described inwall is made of pottery or metallic substance.
6. the pyrolytic process of coal according to claim 5 is characterized in that described light-weight refractory insulating brick is phosphoric acid block salt or magnesia chrome brick.
7. the pyrolytic process of coal according to claim 5 is characterized in that described fully fibrous structure is made of ceramic fiber, aluminum silicate fiber.
8. the pyrolytic process of coal according to claim 5 is characterized in that described metallic substance comprises stainless steel, iron or copper.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201010559620 CN102010731B (en) | 2010-11-25 | 2010-11-25 | Pyrolytic process of coal |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201010559620 CN102010731B (en) | 2010-11-25 | 2010-11-25 | Pyrolytic process of coal |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN102010731A true CN102010731A (en) | 2011-04-13 |
| CN102010731B CN102010731B (en) | 2013-05-08 |
Family
ID=43841065
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 201010559620 Expired - Fee Related CN102010731B (en) | 2010-11-25 | 2010-11-25 | Pyrolytic process of coal |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN102010731B (en) |
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102358840A (en) * | 2011-09-13 | 2012-02-22 | 山东天力干燥股份有限公司 | Single-stage fine coal multi-pipe rotary low-temperature destructive distillation technology and system |
| CN104962306A (en) * | 2015-06-15 | 2015-10-07 | 天津天绿健科技有限公司 | Method of preparing fuel oil material by coal processing |
| CN104974769A (en) * | 2015-06-15 | 2015-10-14 | 天津天绿健科技有限公司 | Method for preparing fuel oil raw material by coal destructive distillation processing |
| CN105013496A (en) * | 2015-06-15 | 2015-11-04 | 天津天绿健科技有限公司 | Catalyst for using coal to prepare fuel feedstock and preparation thereof |
| CN118079792A (en) * | 2024-04-28 | 2024-05-28 | 河北飞天石化集团有限公司 | Environment-friendly oil sludge heat treatment pyrolysis device |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN201193205Y (en) * | 2008-02-24 | 2009-02-11 | 陈宝江 | Rotary furnace for producing active carbon |
| CN101805625A (en) * | 2010-04-22 | 2010-08-18 | 西安三瑞实业有限公司 | Method for preparing carbocoal by thermally cracking raw coal with external-heat horizontal rotary charring furnace |
-
2010
- 2010-11-25 CN CN 201010559620 patent/CN102010731B/en not_active Expired - Fee Related
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN201193205Y (en) * | 2008-02-24 | 2009-02-11 | 陈宝江 | Rotary furnace for producing active carbon |
| CN101805625A (en) * | 2010-04-22 | 2010-08-18 | 西安三瑞实业有限公司 | Method for preparing carbocoal by thermally cracking raw coal with external-heat horizontal rotary charring furnace |
Non-Patent Citations (1)
| Title |
|---|
| 韩永霞，姚昭章: "升温速度对煤热解动力学的影响", 《华东冶金学院学报》 * |
Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102358840A (en) * | 2011-09-13 | 2012-02-22 | 山东天力干燥股份有限公司 | Single-stage fine coal multi-pipe rotary low-temperature destructive distillation technology and system |
| CN102358840B (en) * | 2011-09-13 | 2013-05-01 | 山东天力干燥股份有限公司 | Single-stage fine coal multi-pipe rotary low-temperature destructive distillation technology and system |
| CN104962306A (en) * | 2015-06-15 | 2015-10-07 | 天津天绿健科技有限公司 | Method of preparing fuel oil material by coal processing |
| CN104974769A (en) * | 2015-06-15 | 2015-10-14 | 天津天绿健科技有限公司 | Method for preparing fuel oil raw material by coal destructive distillation processing |
| CN105013496A (en) * | 2015-06-15 | 2015-11-04 | 天津天绿健科技有限公司 | Catalyst for using coal to prepare fuel feedstock and preparation thereof |
| CN104962306B (en) * | 2015-06-15 | 2017-03-15 | 天津天绿健科技有限公司 | A kind of method that Coal dressing prepares hydrocarbon oil feedstock |
| CN107434976A (en) * | 2015-06-15 | 2017-12-05 | 天津天绿健科技有限公司 | A kind of method that coal destructive distillation processing prepares fuel oil raw material |
| CN118079792A (en) * | 2024-04-28 | 2024-05-28 | 河北飞天石化集团有限公司 | Environment-friendly oil sludge heat treatment pyrolysis device |
| CN118079792B (en) * | 2024-04-28 | 2024-12-10 | 河北飞天石化集团有限公司 | An environmentally friendly oil sludge thermal treatment cracking device |
Also Published As
| Publication number | Publication date |
|---|---|
| CN102010731B (en) | 2013-05-08 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN103708456B (en) | The method preparing carbide | |
| CN102295282B (en) | Carbonization-activation integral furnace | |
| CN101805625B (en) | Method for preparing carbocoal by thermally cracking raw coal with external-heat horizontal rotary charring furnace | |
| CN105858660B (en) | The system and method for preparing calcium carbide | |
| CN102010731A (en) | Pyrolytic process of coal | |
| CN101412915B (en) | Interior heating type method for continuously preparing coal gas by pyrolysis and gasification of biomass and pyrolysis gasification furnace | |
| CN101440290B (en) | A method of microwave rapid medium and low temperature carbonization of coal | |
| CN104073263B (en) | Heat accumulating type rotating bed low-temperature carbonization system and technique | |
| CN104342179A (en) | A mixed type coal pyrolysis method | |
| CN106977068A (en) | A kind of method for improving sludge carbon yield | |
| CN106916599A (en) | A kind of iron coke process units and method | |
| CN103468281B (en) | Method and device for low temperature carbonization and pyrolysis of low-rank coal and oil shale | |
| CN103333705B (en) | Zero-heat carrier powdered coal low-temperature dry distillation carbonization method | |
| CN105238421B (en) | A kind of tamping coking method for being incorporated biomass | |
| CN107353919A (en) | Production process for partially pure oxygen oxidation coke | |
| CN105694935A (en) | Dry distillation and activation integrated furnace for pulverized coal | |
| CN104910941B (en) | A kind of revolving bed coal is catalyzed method for pyrolysis | |
| CN103708460B (en) | The method preparing carbide | |
| CN105621410A (en) | Activated carbon production process | |
| CN102766476A (en) | Multi-layer upright tower type duff dust and oil shale distillation plant with stirring function and process | |
| CN105776208A (en) | Production method of active coke | |
| CN1640988A (en) | Method for preparing coal tar by coal pyrolysis | |
| CN103754870A (en) | Method for preparing coke-based formed activated carbon by using one-step activating method | |
| CN209536987U (en) | A kind of coal preparing active carbon system being pyrolyzed and activation is combined | |
| CN102784605A (en) | Method for preventing coal gas from being coked during preheating |
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 | ||
| ASS | Succession or assignment of patent right |
Owner name: BEIJING HUASHI UNITED ENERGY TECHNOLOGY AND DEVELO Free format text: FORMER OWNER: SHAO SUYING Effective date: 20150603 |
|
| C41 | Transfer of patent application or patent right or utility model | ||
| COR | Change of bibliographic data |
Free format text: CORRECT: ADDRESS; FROM: 100079 FENGTAI, BEIJING TO: 100101 CHAOYANG, BEIJING |
|
| TR01 | Transfer of patent right |
Effective date of registration: 20150603 Address after: 100101, 1612/1615, building 1, building 8, Beichen East Road, Chaoyang District, Beijing Patentee after: Beijing Huashi United Energy Technology and Development Co.,Ltd. Address before: 100079 Beijing City, Fengtai District, No. seven, No. 1603, room 9, No. 44 Patentee before: Shao Suying |
|
| CF01 | Termination of patent right due to non-payment of annual fee | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20130508 |