CN104130790A - Coal dry distillation technology employing indirect heat exchange - Google Patents
Coal dry distillation technology employing indirect heat exchange Download PDFInfo
- Publication number
- CN104130790A CN104130790A CN201410307533.4A CN201410307533A CN104130790A CN 104130790 A CN104130790 A CN 104130790A CN 201410307533 A CN201410307533 A CN 201410307533A CN 104130790 A CN104130790 A CN 104130790A
- Authority
- CN
- China
- Prior art keywords
- coal
- heat exchange
- gas
- indirect heat
- semicoke
- 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
Abstract
The invention provides a coal dry distillation technology employing indirect heat exchange. Glue gas subjected to heat exchange at a dry distillation stage is employed for direct heat exchange on raw coal at a drying stage, so that dewatering drying is realized. Then at the dry distillation stage, combustion of coal gas and air is realized and a high-temperature flue gas of 800-1200 DEG C is generated, and the high-temperature flue gas is used to perform indirect heat exchange on coal. After the dry distillation step is finished, cooling of semicoke employs direct spraying cooling at the upper part combined with indirect water cooling at the lower part, and indirect water cooling gives play to main effect, so that semicoke with relatively high quality is relatively easily obtained, and also no wastewater discharge is generated, water source is saved and environmental pollution is reduced. The coal dry distillation technology employing indirect heat exchange helps to improve the calorific value of coal gas, reduce the dust content in the coal gas and improve the tar yield, the prepared semicoke is high in quality, and the technology is applicable to both dry distillation of lump coal and small-granularity coal.
Description
Technical field
The present invention relates to a kind of coal carbonization technology of indirect heat exchange, belong to dry distillation of coal technical field.
Background technology
Destructive distillation is the reaction process of solid or organism thermal degradation under isolated air conditions.The result of destructive distillation is to generate various gas, steam and solid residue, and the mixture of gas and steam is divided into gas and liquid after cooling.Coal carbonization is one of important method of coal being carried out chemical process, and coal is after destructive distillation, and the composition of raw material and state of aggregation all will change, and solid-state in product, gaseous state and fluent meterial have, and can obtain semicoke, coal tar and coke-oven gas.
Destructive distillation is produced and is mostly adopted periodical operation, but destructive distillation device can be different and different with object because of raw material type, generally can be divided into external combustion type and internal combustion type two classes.External combustion type is that raw material is put into the airtight gas retort that metal or refractory materials are made, outside fuel combustion heat supply, this form of the many employings of existing destructive distillation device use.Internal combustion type is in destructive distillation, in gas retort, passes into a certain amount of air, makes the heat release of part destructive distillation material combusting, and raw material availability is lower, only in small-scale production, adopts.
Chinese patent literature CN101691493A discloses a kind of external combustion internally heated coal carbonization furnace, is followed successively by from top to bottom: be used for to the withering dryer section of feed coal, and in drying treatment, obtain cold flue gas; Be used for to the retort section of carrying out destructive distillation processing through the feed coal of drying treatment, feed coal forms destructive distillation product after destructive distillation is processed; By passing into described cold flue gas, be used for the destructive distillation product of output in described retort section to carry out the cooling section of cooling process; The described cold flue gas conducting that described dryer section is produced is to the cold flue gas pipeline of described cooling section.As can be seen here, above-mentioned external combustion internally heated coal carbonization furnace is by arranging preheating, dry, destructive distillation, cooling four segment structures, and the hot flue gas through cooling section is carried out to thermal pretreatment to the raw material coal cinder in preheating section, take full advantage of the preheating in flue gas, avoided the waste of heat energy.Yet above-mentioned external combustion internally heated coal carbonization furnace is only applicable to the particle diameter to be greater than the lump coal of 30mm carries out dry distillation charring, and while carrying out destructive distillation for the small grain size coal that particle diameter is less than 30mm, exist ventilation property poor, heat exchange efficiency is low, in coal gas, dust content is large, caloric power of gas is low, the series of problems such as tar yield is low, semicoke poor quality, thus this external combustion internally heated coal carbonization furnace can not be applicable to the charing of small grain size coal carbonization.
Real data shows, mining can a large amount of lump coal and the small particle size coal of output in producing, and for manual exploitation, lump coal accounts for 60%, and mixed coal accounts for 40%, and machine is when adopt, and lump coal only accounts for 40%, and mixed coal accounts for 60%; In mixed coal, the small particle size coal that particle diameter is less than 30mm accounts for 60% of mixed coal.In addition this year, because integration, the mechanical mining dynamics in little colliery strengthens, coal production scale increases, and the smalls amount of generation is very large, thereby present stage is found a kind of device and technique that is suitable for the smalls to carry out destructive distillation processing and just seems particularly important.
Summary of the invention
Technical problem to be solved by this invention is that external combustion internally heated coal carbonization furnace of the prior art can not be applicable to the charing of small grain size coal carbonization, thereby proposes a kind of coal carbonization technology that can simultaneously be applicable to the indirect heat exchange of lump coal and small grain size coal.
For solving the problems of the technologies described above, the technical scheme of employing of the present invention is:
A coal carbonization technology for indirect heat exchange, is characterized in that, comprises the following steps:
(1) coal is dried in dryer section;
(2) dried coal enters retort section, and the high-temperature flue gas producing with coal gas and air combustion in described retort section carries out indirect heat exchange, and described coal is carried out to pyrolysis;
(3) water is sprayed to pyrogenous origin raw gas, the described raw gas after spray is carried out to the separated of coal gas, tar and water;
(4) pyrogenous origin high temperature semicoke enters cooling section, at described cooling section, first makes water spray pyrogenous origin high temperature semicoke, and described high temperature semicoke is cooled to below 550 ℃;
Described high temperature semicoke after cooling carries out indirect heat exchange with recirculated cooling water again and obtains below semicoke until temperature is reduced to 100 ℃.
Described coal is that particle size range is the small grain size coal of 0-30mm.
Described dryer section, retort section and cooling section are vertically gone up from top to bottom and are set gradually.
The described high-temperature flue gas completing after indirect heat exchange with described small grain size coal in step (2) is sent into described dryer section, carry out direct heat exchange with described coal and be dried.
The temperature of described dryer section is 80-100 ℃; The high-temperature flue gas that in described step (2), coal gas and air combustion produce is 800-1200 ℃, and the pyrolysis temperature of described coal is 550-650 ℃.
The a part of coal gas that step (3) raw gas separation obtains produces high-temperature flue gas for step (2) and air combustion.
In step (4) with the heat exchange of described high temperature semicoke after recirculated cooling water and the air in step (2) carry out indirect heat exchange, it is cooling for described high temperature semicoke is carried out that recirculated cooling water after heat exchange comes back to cooling section, and the air after heat exchange and described coal gas burn and produces high-temperature flue gas.
In step (3), the described raw gas after spray is sent into tornado dust collector, direct-cooled washing tower, indirect horizontal cooler, spray catcher, electrical tar precipitator, gas compressor successively and carry out the separated of coal gas, tar and water.
Described retort section is provided with combustion chamber and coking chamber, and described combustion chamber is positioned at the peripheral of described coking chamber and around described coking chamber setting, described dried coal enters coking chamber, and described coal gas and air burn and produce high-temperature flue gas in described combustion chamber.
In described coking chamber, be provided with gas extractor, described gas extractor comprises:
Multilayer supervisor, every layer of described supervisor is provided with a plurality of and equal along continuous straight runs setting, and every layer of corresponding setting of described supervisor's in the vertical direction, forms a plurality of files;
Arm, along continuous straight runs setting, is communicated with described supervisor and distributes along described supervisor's zygomorphy, on described arm, is provided with air inlet port;
A plurality of upcasts, vertically arrange, and described in each, upcast is communicated with setting with supervisor described in a file, is communicated with and is provided with the transverse tube of giving vent to anger with the top of described a plurality of upcasts.
The coal carbonization technology of indirect heat exchange of the present invention, has the following advantages:
(1) coal carbonization technology of indirect heat exchange of the present invention, first adopts the flue gas after retort section heat exchange to carry out direct heat exchange to raw coal at described kiln, thereby realize, dehydrates, and has guaranteed to enter before retort section removing of part moisture in coal; In described retort section, realized the burning of coal gas and air and produced the high-temperature flue gas of 800-1200 ℃ afterwards, described high-temperature flue gas carries out indirect heat exchange to coal, and high-temperature flue gas and coal are by furnace wall indirect heat exchange, and flue gas does not mix with coal gas, obtains purer coal gas; After destructive distillation step completes, at described cooling section, first adopt spray water to carry out semicoke directly cooling, the steam producing forms elevated pressures between retort section and cooling section, effectively prevent that coal gas from entering cooling section, cooling water pipe being passed into recirculated water carries out indirectly cooling again to the semicoke in semicoke pipeline, thisly first adopt spraying cooling, then adopt the type of cooling of indirect water-cooling to be conducive to obtain the semicoke that quality is higher.And, mode due to the indirect water-cooling adopting, therefore can not produce discharge of wastewater, save water resources, reduce environmental pollution, thereby the coal carbonization technology of indirect heat exchange of the present invention, improve the calorific value of coal gas, reduced dust content in coal gas, improved tar yield, make semicoke quality high, can be applicable to lump coal and the charing of small grain size coal carbonization simultaneously.
(2) coal carbonization technology of indirect heat exchange of the present invention, further preferred described dryer section, retort section and cooling section are vertically gone up from top to bottom and are set gradually, by this setup, small particle size coal is descending gradually under self gravitation effect, thereby realizes whole retort process.And, the present invention arranges described dryer section, what retort section and cooling section were vertically arranged in order is also advantageous in that, due to distillation process of the present invention, after destructive distillation step completes, at described cooling section, first adopt spray water to carry out semicoke directly cooling, cooling water pipe being passed into recirculated water carries out indirectly cooling again to the green coke in green coke pipeline, to adopt spray water to carry out semicoke direct when cooling, the steam that spray water produces forms larger malleation on the top of cooling section, the coal gas that can hinder retort section enters cooling section, thereby prevent that coal gas from contacting with semicoke, make the quality of semicoke be able to further lifting.
(3) coal carbonization technology of indirect heat exchange of the present invention, in described coking chamber, be provided with multilayer gas extractor, thereby can realize, the raw gas in stove is carried out to multilayer gas collection, effectively avoiding that coal especially particle diameter is less than to 30mm small grain size coal carries out producing raw gas in the process rising after destructive distillation, bed resistance is larger, ventilation property is poor, multilayer gas extractor of the present invention, effectively reduce bed resistance, even also can realize even rising for the raw gas producing after the small grain size dry distillation of coal, good permeability, homogeneous heating, heat exchange efficiency is high.
Accompanying drawing explanation
For content of the present invention is more likely to be clearly understood, below according to a particular embodiment of the invention and by reference to the accompanying drawings, the present invention is further detailed explanation, wherein
Fig. 1 is for carrying out the schematic diagram of the gas retort of indirect heat exchange coal carbonization technology of the present invention;
Wherein, Reference numeral is expressed as:
1-furnace roof coal bunker, 2-dryer section, 3-retort section, 4-spray water-cooled section, 5-indirect water-cooling section, 6-flue, 7-the first spray equipment, the indirect horizontal cooler of 8-, 9-electrical tar precipitator, 10-gas compressor; 11-gas line; 12-air line; 13-interchanger; 14-air cooler; 15 water dust scrubbers; 16-induced draft fan.
Embodiment
Embodiment 1
In the present embodiment for carrying out the gas retort of the coal carbonization technology of indirect heat exchange, its structure comprises: furnace roof coal bunker 1, dryer section 2, retort section 3, cooling section and dumper along direction sets gradually are from top to bottom provided with push-pull valve between described furnace roof coal bunker 1 and dryer section 2; Wherein said retort section 3 is provided with combustion chamber and coking chamber, described combustion chamber is positioned at the peripheral of described coking chamber and around described coking chamber setting, described dried coal enters coking chamber and carries out pyrolysis, be connected with raw coke oven gas pipeline with described coking chamber, on described raw coke oven gas pipeline, be disposed with the first spray equipment 7, tornado dust collector, direct-cooled washing tower, indirect horizontal cooler 8, spray catcher, electrical tar precipitator 9 and gas compressor 10; The described raw coke oven gas pipeline that is positioned at described electrical tar precipitator 9 downstreams is communicated with setting by gas line 11 with described combustion chamber, also be communicated with and be provided with air line 12 and flue with described combustion chamber, on described flue, be provided with fly-ash separator 15 and induced draft fan 16, in addition, from combustion chamber, extremely described dryer section 2 is also provided with flue 6, for carrying out direct heat exchange with described coal; Upper part of cooling section described in the present embodiment, for spray water-cooled section 4, is provided with the second spray equipment in described spray water-cooled section 4, for spraying cooling water; The Lower Half of described cooling section is indirect water-cooling section 5, in described indirect water-cooling section 5, is provided with indirect water-cooling pipeline.
The small grain size coal that the coal carbonization technology that adopts described indirect heat exchange in the present embodiment is 0-30mm to particle size range carries out destructive distillation, and step comprises:
(1) open slide valve, small grain size coal enters dryer section 2 by furnace roof coal bunker 1, and the inlet amount of described small grain size coal is 125 tons/h; It is dry that the flue gas of described small grain size coal in dryer section 2 and flue 6 carries out direct heat exchange, and the temperature of described dryer section 2 is 80 ℃;
(2) under dried small grain size coal, be advanced into retort section 3, in described retort section 3 with combustion chamber in the high-temperature flue gas of 800 ℃ that produces of coal gas and air combustion carry out indirect heat exchange, described small grain size coal is heated to 550 ℃ and carries out pyrolysis; Send into described dryer section 2 with the described high-temperature flue gas that described small grain size coal completes after indirect heat exchange, to carry out direct heat exchange dry with described small grain size coal, with described small grain size coal carry out the dried flue gas of direct heat exchange through water dust scrubber 15 dedustings by being discharged by induced draft fan 16.
(3) pyrogenous origin raw gas enters raw coke oven gas pipeline, the first spray equipment 7 spray waters spray pyrogenous origin raw gas, described raw gas after spray is sent into tornado dust collector, direct-cooled washing tower, indirect horizontal cooler 8, spray catcher, electrical tar precipitator 9 and gas compressor 10 more successively, carry out the separated of coal gas, tar and water, a part in the coal gas that separation is obtained passes in described combustion chamber by gas line, for step (2) and air combustion, produces high-temperature flue gas;
(4) under pyrogenous origin high temperature semicoke, be advanced into cooling section, the second spray equipment, by pyrogenous origin high temperature semicoke spray water, is cooled to described high temperature semicoke below 550 ℃;
Semicoke after cooling continues descending, in indirect water-cooling section 5 and described indirect water-cooling tube contacts, carries out indirect heat exchange until temperature is reduced to 100 ℃ and obtains below semicoke product; Described semicoke product is discharged in stove by dumper, and the output of semicoke described in the present embodiment is 72.25 tons/h.
Embodiment 2
In the present embodiment for carry out indirect heat exchange coal carbonization technology gas retort as shown in Figure 1, its structure comprises: along furnace roof coal bunker 1, dryer section 2, retort section 3, cooling section and the dumper that direction sets gradually from top to bottom, between described furnace roof coal bunker 1 and dryer section 2, be provided with push-pull valve, wherein said retort section 3 is provided with combustion chamber and coking chamber, described combustion chamber is positioned at the peripheral of described coking chamber and around described coking chamber setting, described dried coal enters coking chamber and carries out pyrolysis;
Gas retort described in the present embodiment is also provided with gas extractor in described coking chamber, and described gas extractor comprises: multilayer supervisor, arm and a plurality of upcast; Wherein every layer of described supervisor is provided with a plurality of and equal along continuous straight runs setting, and every layer of corresponding setting of described supervisor's in the vertical direction, forms a plurality of files; Described arm along continuous straight runs arranges, and described arm is communicated with described supervisor and along described supervisor's zygomorphy distribution, on described arm, is provided with air inlet port; Described a plurality of upcast vertically arranges, described in each, upcast is communicated with setting with supervisor described in a file, be communicated with and be provided with the transverse tube of giving vent to anger with the top of described a plurality of upcasts, with described give vent to anger to traverse to be communicated be provided with raw coke oven gas pipeline, on described raw coke oven gas pipeline, be disposed with the first spray equipment 7, indirect horizontal cooler 8, electrical tar precipitator 9 and gas compressor 10; The described raw coke oven gas pipeline that is positioned at described electrical tar precipitator 9 downstreams is communicated with setting by gas line 11 with described combustion chamber; Also be communicated with and be provided with air line 12 and flue with described combustion chamber, be provided with fly-ash separator 15 and induced draft fan 16 on described flue, in addition, from combustion chamber, extremely described dryer section 2 is also provided with flue 6, for carrying out direct heat exchange with described coal;
Upper part of described cooling section in the present embodiment, for spray water-cooled section 4, is provided with the second spray equipment in described spray water-cooled section 4, for spraying cooling water; The Lower Half of described cooling section is indirect water-cooling section 5, in described indirect water-cooling section 5, is provided with indirect water-cooling pipeline.Be connected with interchanger 13 with described indirect water-cooling pipeline, described interchanger 13 is suitable for air and carries out heat exchange, and the air after heat exchange enters described burning zone and described coal gas through air line 12 and burns and produce high-temperature flue gas; On the indirect water-cooling pipeline that is positioned at described interchanger 13 downstreams, be also provided with air cooler 14.
The present embodiment adopts the small grain size coal that the coal carbonization technology of described indirect heat exchange is 0-30mm to particle size range to carry out destructive distillation, comprises the following steps:
(1) open slide valve, small grain size coal enters dryer section 2 by furnace roof coal bunker 1, and the inlet amount of described small grain size coal is 125 tons/h; The temperature of described dryer section 2 is 100 ℃;
(2) under dried small grain size coal, be advanced into retort section 3, the high-temperature flue gas of 1000 ℃ producing with coal gas and air combustion in described retort section 3 carries out indirect heat exchange, described small grain size coal is heated to 650 ℃ and carries out pyrolysis; Send into described dryer section 2 with the described high-temperature flue gas that described small grain size coal completes after indirect heat exchange, to carry out direct heat exchange dry with described small grain size coal, with described small grain size coal carry out the dried flue gas of direct heat exchange through water dust scrubber 15 dedustings by being discharged by induced draft fan 16;
(3) pyrogenous origin raw gas enters raw coke oven gas pipeline, the first spray equipment 7 spray waters spray pyrogenous origin raw gas, described raw gas after spray is sent into transverse tube inter cooler 8, electrical tar precipitator 9 and gas compressor 10 successively, carry out the separated of coal gas, tar and water, a part in the coal gas that separation is obtained passes in described combustion chamber by gas line, for step (2) and air combustion, produces high-temperature flue gas;
(4) under pyrogenous origin high temperature semicoke, be advanced into cooling section, the second spray equipment, by pyrogenous origin high temperature semicoke spray water, is cooled to described high temperature semicoke below 550 ℃;
Semicoke after cooling continues descending, with described indirect water-cooling tube contacts, carries out indirect heat exchange until temperature is reduced to 100 ℃ and obtains below semicoke product; Described semicoke product is discharged in stove by dumper, and the output of semicoke described in the present embodiment is 72.25 tons/h.
In the step of the present embodiment (4), carry out indirect heat exchange with recirculated cooling water after the heat exchange of described high temperature semicoke and the air in step (2), it is cooling for described high temperature semicoke is carried out that recirculated cooling water after heat exchange comes back to cooling section, and the air after heat exchange enters described burning zone and described coal gas through air line 12 and burns and produce high-temperature flue gas.
Obviously, above-described embodiment is only for example is clearly described, and the not restriction to embodiment.For those of ordinary skill in the field, can also make other changes in different forms on the basis of the above description.Here exhaustive without also giving all embodiments.And the apparent variation of being extended out thus or change are still among the protection domain in the invention.
Claims (10)
1. a coal carbonization technology for indirect heat exchange, is characterized in that, comprises the following steps:
(1) coal is dried in dryer section;
(2) dried coal enters retort section, and the high-temperature flue gas producing with coal gas and air combustion in described retort section carries out indirect heat exchange, and described coal is carried out to pyrolysis;
(3) water is sprayed to pyrogenous origin raw gas, the described raw gas after spray is carried out to the separated of coal gas, tar and water;
(4) pyrogenous origin high temperature semicoke enters cooling section, at described cooling section, first makes water spray pyrogenous origin high temperature semicoke, and described high temperature semicoke is cooled to below 550 ℃;
Described high temperature semicoke after cooling carries out indirect heat exchange with recirculated cooling water again and obtains below semicoke until temperature is reduced to 100 ℃.
2. the coal carbonization technology of indirect heat exchange according to claim 1, is characterized in that, described coal is that particle size range is the small grain size coal of 0-30mm.
3. the coal carbonization technology of indirect heat exchange according to claim 1 and 2, is characterized in that, described dryer section, retort section and cooling section are vertically gone up from top to bottom and set gradually.
4. according to the coal carbonization technology of the arbitrary described indirect heat exchange of claim 1-3, it is characterized in that, the described high-temperature flue gas completing after indirect heat exchange with described small grain size coal in step (2) is sent into described dryer section, carry out direct heat exchange with described coal and be dried.
5. according to the coal carbonization technology of the arbitrary described indirect heat exchange of claim 1-4, it is characterized in that, the temperature of described dryer section is 80-100 ℃; The high-temperature flue gas that in described step (2), coal gas and air combustion produce is 800-1200 ℃, and the pyrolysis temperature of described coal is 550-650 ℃.
6. according to the coal carbonization technology of the arbitrary described indirect heat exchange of claim 1-5, it is characterized in that, a part of coal gas that step (3) raw gas separation obtains produces high-temperature flue gas for step (2) and air combustion.
7. according to the coal carbonization technology of the arbitrary described indirect heat exchange of claim 1-6, it is characterized in that, in step (4) with the heat exchange of described high temperature semicoke after recirculated cooling water and the air in step (2) carry out indirect heat exchange, it is cooling for described high temperature semicoke is carried out that recirculated cooling water after heat exchange comes back to cooling section, and the air after heat exchange and described coal gas burn and produces high-temperature flue gas.
8. according to the coal carbonization technology of the arbitrary described indirect heat exchange of claim 1-7, it is characterized in that, in step (3), the described raw gas after spray is sent into tornado dust collector, direct-cooled washing tower, indirect horizontal cooler, spray catcher, electrical tar precipitator, gas compressor successively and carry out the separated of coal gas, tar and water.
9. according to the coal carbonization technology of the arbitrary described indirect heat exchange of claim 1-8, it is characterized in that, described retort section is provided with combustion chamber and coking chamber, described combustion chamber is positioned at the peripheral of described coking chamber and around described coking chamber setting, described dried coal enters coking chamber, and described coal gas and air burn and produce high-temperature flue gas in described combustion chamber.
10. according to the arbitrary described distillation process for small grain size coal indirect heat exchange of claim 1-9, it is characterized in that, in described coking chamber, be provided with gas extractor, described gas extractor comprises:
Multilayer supervisor, every layer of described supervisor is provided with a plurality of and equal along continuous straight runs setting, and every layer of corresponding setting of described supervisor's in the vertical direction, forms a plurality of files;
Arm, along continuous straight runs setting, is communicated with described supervisor and distributes along described supervisor's zygomorphy, on described arm, is provided with air inlet port;
A plurality of upcasts, vertically arrange, and described in each, upcast is communicated with setting with supervisor described in a file, is communicated with and is provided with the transverse tube of giving vent to anger with the top of described a plurality of upcasts.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410307533.4A CN104130790B (en) | 2014-06-30 | 2014-06-30 | A kind of coal carbonization technology of indirect heat exchange |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410307533.4A CN104130790B (en) | 2014-06-30 | 2014-06-30 | A kind of coal carbonization technology of indirect heat exchange |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN104130790A true CN104130790A (en) | 2014-11-05 |
| CN104130790B CN104130790B (en) | 2018-12-07 |
Family
ID=51803651
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201410307533.4A Active CN104130790B (en) | 2014-06-30 | 2014-06-30 | A kind of coal carbonization technology of indirect heat exchange |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN104130790B (en) |
Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105062533A (en) * | 2015-08-03 | 2015-11-18 | 中冶焦耐工程技术有限公司 | Drying pre-heating apparatus for coal material entering furnace |
| CN105885893A (en) * | 2016-06-02 | 2016-08-24 | 华电重工股份有限公司 | Internal and external heating coal dry distillation device and dry distillation method thereof |
| CN106590699A (en) * | 2015-10-20 | 2017-04-26 | 晏廷书 | Coke quenching technology |
| CN107619670A (en) * | 2017-10-20 | 2018-01-23 | 北京神雾电力科技有限公司 | A kind of pyrolysis oven and method for pyrolysis |
| CN108410489A (en) * | 2017-02-10 | 2018-08-17 | 中国神华能源股份有限公司 | Clean coal production system and production method |
| CN108410487A (en) * | 2017-02-10 | 2018-08-17 | 中国神华能源股份有限公司 | Clean coal polygenerations systeme and Poly-generation method |
| CN110041949A (en) * | 2019-05-09 | 2019-07-23 | 重庆富燃科技股份有限公司 | A kind of device and method of pair of powdery (or graininess) solid matter recycling treatment |
| CN110184083A (en) * | 2019-05-29 | 2019-08-30 | 中国成达工程有限公司 | A kind of coal oil residue treatment technique and processing unit |
| CN110699102A (en) * | 2019-11-05 | 2020-01-17 | 西安热工研究院有限公司 | Drying and pyrolyzing furnace and drying and pyrolyzing method for municipal domestic garbage |
Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE2633789A1 (en) * | 1976-07-28 | 1978-02-09 | Wintershall Ag | PROCESS FOR THE PRODUCTION OF PETROL LOCAL CALCINATE |
| CN101691493A (en) * | 2009-09-15 | 2010-04-07 | 北京国电富通科技发展有限责任公司 | External combustion internally heated coal carbonization furnace |
| CN201574140U (en) * | 2009-12-04 | 2010-09-08 | 北京中能华源投资有限公司 | Gas collecting device for coal dry distillation furnace |
| CN201770652U (en) * | 2010-08-16 | 2011-03-23 | 王东辉 | Semi-coke dry quenching system |
| US20120017499A1 (en) * | 2011-08-23 | 2012-01-26 | Advanced Torrefaction Systems, Inc. | Torrefaction Systems and Methods Including Catalytic Oxidation and/or Reuse of Combustion Gases Directly in a Torrefaction Reactor, Cooler, and/or Dryer/Preheater |
| CN102492432A (en) * | 2011-12-09 | 2012-06-13 | 新疆美特镁业有限公司 | Pulverized coal coking equipment and method |
| CN202671496U (en) * | 2012-01-06 | 2013-01-16 | 吴植仁 | Vertical low temperature retort furnace |
| CN203462003U (en) * | 2013-08-08 | 2014-03-05 | 宁波互联聚能环保技术有限公司 | Direct-indirect combining heat granule shale low temperature dry distillation furnace |
-
2014
- 2014-06-30 CN CN201410307533.4A patent/CN104130790B/en active Active
Patent Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE2633789A1 (en) * | 1976-07-28 | 1978-02-09 | Wintershall Ag | PROCESS FOR THE PRODUCTION OF PETROL LOCAL CALCINATE |
| CN101691493A (en) * | 2009-09-15 | 2010-04-07 | 北京国电富通科技发展有限责任公司 | External combustion internally heated coal carbonization furnace |
| CN201574140U (en) * | 2009-12-04 | 2010-09-08 | 北京中能华源投资有限公司 | Gas collecting device for coal dry distillation furnace |
| CN201770652U (en) * | 2010-08-16 | 2011-03-23 | 王东辉 | Semi-coke dry quenching system |
| US20120017499A1 (en) * | 2011-08-23 | 2012-01-26 | Advanced Torrefaction Systems, Inc. | Torrefaction Systems and Methods Including Catalytic Oxidation and/or Reuse of Combustion Gases Directly in a Torrefaction Reactor, Cooler, and/or Dryer/Preheater |
| CN102492432A (en) * | 2011-12-09 | 2012-06-13 | 新疆美特镁业有限公司 | Pulverized coal coking equipment and method |
| CN202671496U (en) * | 2012-01-06 | 2013-01-16 | 吴植仁 | Vertical low temperature retort furnace |
| CN203462003U (en) * | 2013-08-08 | 2014-03-05 | 宁波互联聚能环保技术有限公司 | Direct-indirect combining heat granule shale low temperature dry distillation furnace |
Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105062533A (en) * | 2015-08-03 | 2015-11-18 | 中冶焦耐工程技术有限公司 | Drying pre-heating apparatus for coal material entering furnace |
| CN106590699A (en) * | 2015-10-20 | 2017-04-26 | 晏廷书 | Coke quenching technology |
| CN105885893A (en) * | 2016-06-02 | 2016-08-24 | 华电重工股份有限公司 | Internal and external heating coal dry distillation device and dry distillation method thereof |
| CN108410489A (en) * | 2017-02-10 | 2018-08-17 | 中国神华能源股份有限公司 | Clean coal production system and production method |
| CN108410487A (en) * | 2017-02-10 | 2018-08-17 | 中国神华能源股份有限公司 | Clean coal polygenerations systeme and Poly-generation method |
| CN107619670A (en) * | 2017-10-20 | 2018-01-23 | 北京神雾电力科技有限公司 | A kind of pyrolysis oven and method for pyrolysis |
| CN110041949A (en) * | 2019-05-09 | 2019-07-23 | 重庆富燃科技股份有限公司 | A kind of device and method of pair of powdery (or graininess) solid matter recycling treatment |
| CN110184083A (en) * | 2019-05-29 | 2019-08-30 | 中国成达工程有限公司 | A kind of coal oil residue treatment technique and processing unit |
| CN110699102A (en) * | 2019-11-05 | 2020-01-17 | 西安热工研究院有限公司 | Drying and pyrolyzing furnace and drying and pyrolyzing method for municipal domestic garbage |
Also Published As
| Publication number | Publication date |
|---|---|
| CN104130790B (en) | 2018-12-07 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN104130790A (en) | Coal dry distillation technology employing indirect heat exchange | |
| CN101514291B (en) | Method for dry quenching by internal heat and low temperature carbonization of coal | |
| JP5756814B2 (en) | Coal substance decomposition equipment | |
| CN101691493B (en) | External combustion internally heated coal carbonization furnace | |
| CN104531187A (en) | Method for preparing tar, coal gas and semi-coke by virtue of pyrolysis of bituminous coal | |
| CN102732274A (en) | Brown coal dry-distillation method using coal hot air furnace to supply heat | |
| CN101250419B (en) | Low-temperature dry distillation process with coal gas internal heat | |
| CA2806493C (en) | Electrical-heating coal material decomposition device | |
| CN204237743U (en) | A kind of New type coal gas retort | |
| CN104789244A (en) | Gas-circulating method for pyrolysis production of anthracite in coal powder rotary furnace | |
| US20130126330A1 (en) | Vertical pyrolysis equipment for coal material | |
| CN101402870B (en) | Complete alternation gas retort for treating 300 tons of wax shale mash gas a day | |
| CN105621410A (en) | Activated carbon production process | |
| CN103435028B (en) | Method and device for producing semi coke | |
| CN104263394B (en) | A kind of brown coal low temperature distillation method for pyrolysis | |
| CN103980920A (en) | Low-quality fuel pyrolysis process | |
| CN105776208A (en) | Production method of active coke | |
| CN202124594U (en) | Heat accumulating type external heating medium-temperature and low-temperature coal pyrolyzing furnace | |
| CN105907413B (en) | The low temperature distillation technique of low order fine coal | |
| CN201520746U (en) | External-combustion internal-heating-type coal dry distillation furnace | |
| CN101691492A (en) | Coal carbonization technology | |
| CN106010607A (en) | Coal pyrolysis and gasification coupling technology and device | |
| CN102786965B (en) | Automatic control device for thermal cycle continuous coal pyrolyzing furnace | |
| CN204848755U (en) | Belt pyrolysis oven | |
| CN205313462U (en) | System for be arranged in low temperature dry distillation of coal |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |