CN107099315A - The separation method of water vapour and raw coke oven gas in low-order coal pyrolytic process - Google Patents
The separation method of water vapour and raw coke oven gas in low-order coal pyrolytic process Download PDFInfo
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- CN107099315A CN107099315A CN201710390154.XA CN201710390154A CN107099315A CN 107099315 A CN107099315 A CN 107099315A CN 201710390154 A CN201710390154 A CN 201710390154A CN 107099315 A CN107099315 A CN 107099315A
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- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 title claims abstract description 67
- 239000003245 coal Substances 0.000 title claims abstract description 63
- 239000000571 coke Substances 0.000 title claims abstract description 35
- 238000000034 method Methods 0.000 title claims abstract description 25
- 238000000926 separation method Methods 0.000 title claims abstract description 19
- 238000000197 pyrolysis Methods 0.000 claims abstract description 43
- 238000001816 cooling Methods 0.000 claims abstract description 13
- 239000000428 dust Substances 0.000 claims abstract description 8
- 239000012716 precipitator Substances 0.000 claims abstract description 7
- 239000002671 adjuvant Substances 0.000 claims abstract description 5
- 238000002485 combustion reaction Methods 0.000 claims abstract description 5
- 238000005086 pumping Methods 0.000 claims description 6
- 239000008235 industrial water Substances 0.000 claims description 4
- 239000003077 lignite Substances 0.000 claims description 4
- 238000010438 heat treatment Methods 0.000 claims description 3
- 239000002245 particle Substances 0.000 claims description 3
- 239000010865 sewage Substances 0.000 abstract description 5
- 238000005265 energy consumption Methods 0.000 abstract description 4
- 239000000284 extract Substances 0.000 abstract description 4
- 238000001035 drying Methods 0.000 description 3
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 2
- ISWSIDIOOBJBQZ-UHFFFAOYSA-N Phenol Chemical compound OC1=CC=CC=C1 ISWSIDIOOBJBQZ-UHFFFAOYSA-N 0.000 description 2
- 239000003034 coal gas Substances 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- JMANVNJQNLATNU-UHFFFAOYSA-N oxalonitrile Chemical compound N#CC#N JMANVNJQNLATNU-UHFFFAOYSA-N 0.000 description 2
- 238000010025 steaming Methods 0.000 description 2
- 238000010521 absorption reaction Methods 0.000 description 1
- 229910021529 ammonia Inorganic materials 0.000 description 1
- 239000002802 bituminous coal Substances 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 238000001514 detection method Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 239000002351 wastewater Substances 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B53/00—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form
- C10B53/04—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form of powdered coal
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B47/00—Destructive distillation of solid carbonaceous materials with indirect heating, e.g. by external combustion
- C10B47/18—Destructive distillation of solid carbonaceous materials with indirect heating, e.g. by external combustion with moving charge
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B47/00—Destructive distillation of solid carbonaceous materials with indirect heating, e.g. by external combustion
- C10B47/28—Other processes
- C10B47/30—Other processes in rotary ovens or retorts
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B57/00—Other carbonising or coking processes; Features of destructive distillation processes in general
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
- C10K1/00—Purifying combustible gases containing carbon monoxide
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
- C10K1/00—Purifying combustible gases containing carbon monoxide
- C10K1/02—Dust removal
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
- C10K1/00—Purifying combustible gases containing carbon monoxide
- C10K1/04—Purifying combustible gases containing carbon monoxide by cooling to condense non-gaseous materials
Landscapes
- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Combustion & Propulsion (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Organic Chemistry (AREA)
- Materials Engineering (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Coke Industry (AREA)
- Processing Of Solid Wastes (AREA)
Abstract
The present invention discloses the separation method of water vapour and raw coke oven gas in a kind of low-order coal pyrolytic process, its feed coal is admitted to revolution pyrolysis kiln by feed arrangement and is pyrolyzed, and the air-introduced machine that the kiln tail setting of kiln is pyrolyzed by turning round extracts the water vapour of the heated abjection of kiln tail section feed coal out；Most of feeding quickly cooling pond in the water vapour being extracted, makes the concurrent raw food of most of water vapor cooling solidifying, while the dust for carrying water vapour secretly is precipitated in quickly cooling pond, remainder uncondensed vapor feeding cooler is further condensed, and obtains steam condensate (SC)；Remainder in the water vapour being extracted is sent directly into hot-blast stove and used as combustion adjuvant；The raw coke oven gas that pyrolysis generation occurs for kiln hood section feed coal goes out after revolution pyrolysis kiln, carries out dedusting into hot precipitator, the high temperature raw coke oven gas after dedusting enters back into Leng Gu workshop sections, purified treatment is carried out to raw coke oven gas.The present invention can effectively reduce system energy consumption, reduce the sewage quantity that pyrolytic process is produced, and reduce cost of sewage disposal.
Description
Technical field
The invention belongs to low order pyrolytic process of coal technical field, more particularly, to water vapour in a kind of low-order coal pyrolytic process
With the separation method of raw coke oven gas.
Background technology
Coal is one of Chinese topmost fossil energy, and energy consumption structure of the China based on coal is longer in future
It will not change in one period.Low-order coal includes the bituminous coal of lignite and low metamorphic grade（Jet coal, dross coal and weakly caking coal）, its
Proved reserves account for 57% or so of national coal resources reserves, have become the important component of production of energy and supply.
Low-order coal moisture is higher, typically more than 20%, in pyrolytic process, can produce substantial amounts of pyrolysis water, and pyrolysis water contains greatly
The components such as phenol, ammonia, cyanogen, the oil of amount, composition is extremely complex, and COD, BOD value are at a relatively high, if without processing, can be caused sternly to environment
Heavily contaminated.But, pyrolysis waste water is because of complicated component, not only complex treatment process, and processing cost is very high；Water is pyrolyzed simultaneously to become
Into after vapor, substantial amounts of heat can be absorbed in pyrolytic process, increases system energy consumption.It is conventional at present to solve this problem
Method be that will be re-fed into pyrolysis oven after low-order coal drying and dehydrating to carry out pyrolytic reaction, but this method needs to increase extra drying
And other equipment, system investments cost is not only increased, technique is become increasingly complex.
The content of the invention
To solve the above problems, it is an object of the invention to provide water vapour in a kind of low-order coal pyrolytic process and raw coke oven gas
Separation method, its water vapour that can remove low order pyrolysis of coal early stage extracts revolution pyrolysis kiln out, so as to avoid water vapour
Lectotype selection into revolution pyrolysis kiln high temperature section absorption amount of heat and to follow-up raw coke oven gas quality-dividing system causes difficulty.
For achieving the above object, the present invention is adopted the following technical scheme that：
The separation method of water vapour and raw coke oven gas in a kind of low-order coal pyrolytic process, it comprises the following steps：
The fine-powdered feed coal of step 1, particle diameter less than 40mm is admitted to revolution pyrolysis kiln by feed arrangement and is pyrolyzed, and is pyrolyzed
Mode uses multitube rotary indirect heating type, and feed coal with the heat exchange of high-temperature gas heat carrier by absorbing heat, and feed coal is being returned
It is 30~90min to turn pyrolysis kiln residence time, and pyrolysis final temperature is 450~650 DEG C, is provided with and draws in the kiln tail of revolution pyrolysis kiln
Blower fan, is extracted out the water vapour for turning round the heated abjection of the kiln tail for being pyrolyzed kiln section feed coal by air-introduced machine, steam temperature is 100
~ 150 DEG C, pressure is -300 ~ -100Pa, and water vapour is 70~90% of Free water in feed coal；
Most of feeding quickly cooling pond in step 2, the water vapour being extracted, makes most of water vapor temperature be reduced to 50 ~ 80 DEG C
Concurrent raw food is solidifying, while the dust for carrying water vapour secretly is precipitated in quickly cooling pond, the water temperature in quickly cooling pond maintains 30 ~ 50 DEG C,
Remainder uncondensed vapor feeding cooler is further condensed, and obtains steam condensate (SC)；Residue in the water vapour being extracted
Part is sent directly into hot-blast stove, is used as combustion adjuvant；
The raw coke oven gas that pyrolysis generation occurs for step 3, kiln hood section feed coal goes out after revolution pyrolysis kiln, is removed into hot precipitator
Raw coke oven gas dust content is by 50 ~ 100g/Nm after dirt, dedusting3It is reduced to 20 ~ 100mg/Nm3, the operating temperature of hot precipitator is
300~500 DEG C, the high temperature raw coke oven gas after dedusting enters back into Leng Gu workshop sections, and purified treatment is carried out to raw coke oven gas.
Further, the feed arrangement in above-mentioned step 1 is inside and outside sleeve structure, and feed coal enters via inner cylinder to turn round
Kiln is pyrolyzed, steam flows through the annular space between outer barrel and inner cylinder, outer barrel is provided with steam pumping mouthful, passes through pipeline and kiln tail air-introduced machine
Connection, is extracted out the part water vapour turned round in pyrolysis kiln by kiln tail air-introduced machine.
Further, the N purged for the pipeline to steam pumping is additionally provided with above-mentioned step 12Blow device.
Further, the steam condensate (SC) obtained in above-mentioned step 2, can be used as situ industrial water after processing.
Further, the High Temperature Gas body heat that the hot blast of the hot-blast stove discharge in above-mentioned step 2 is pyrolyzed kiln as revolution is carried
Body.
Further, the kiln hood of above-mentioned revolution pyrolysis kiln is provided with air-introduced machine, by adjusting kiln hood air-introduced machine and kiln tail
Air-introduced machine, control kiln hood, the pressure difference of kiln tail, and realize the separation of kiln tail water vapour and kiln hood raw coke oven gas.
Further, above-mentioned low-order coal is at least one of lignite, jet coal, non caking coal.
Due to using technical scheme as described above, the present invention has following superiority：
The separation method of water vapour and raw coke oven gas during low order pyrolysis of coal, its technological process is simple, easy to operate, by inciting somebody to action
The water vapour of low order pyrolysis of coal early stage removing extracts revolution pyrolysis kiln out, so as to avoid water vapour from entering revolution pyrolysis kiln high temperature
Section absorbs amount of heat, while avoiding causing that equipment is huge, tar pyrolysis water separation is difficult greatly because of water vapour amount, at pyrolysis sewage
Reason amount is big, production cost is high etc. cause follow-up raw coke oven gas quality-dividing system lectotype selection it is difficult the problem of；Need not increase low-order coal
Pre-drying device, so as to greatly reduce the equipment investment of system；System energy consumption can be effectively reduced, while by the steaming after processing
Vapour condensed water is used as industrial water, alleviates the service water problem of arid area；The sewage quantity that pyrolytic process is produced effectively is reduced,
So as to effectively reduce cost of sewage disposal, the water vapour produced in low-order coal pyrolytic process is used as hot-blast stove combustion adjuvant, becomes useless
For treasured, economize on resources.
Brief description of the drawings
Fig. 1 is the process chart of the present invention.
Embodiment
Technical scheme is described in further detail with reference to the accompanying drawings and examples.
As shown in figure 1, during low order pyrolysis of coal water vapour and raw coke oven gas separation method, it comprises the following steps：
The fine-powdered feed coal of step 1, particle diameter less than 40mm is admitted to revolution pyrolysis kiln by feed arrangement and is pyrolyzed, and is pyrolyzed
Mode use multitube rotary indirect heating type, high-temperature gas heat carrier in heat exchanger tube, high-temperature gas heat carrier temperature be 900~
1000 DEG C, feed coal advances in kiln body, and feed coal absorbs substantial amounts of heat, raw material by being exchanged heat with high-temperature gas heat carrier
Coal is 30~90min in revolution pyrolysis kiln residence time, and pyrolysis final temperature is 450~650 DEG C, is set in the kiln tail of revolution pyrolysis kiln
Air-introduced machine is equipped with, is extracted out the water vapour for turning round the heated abjection of the kiln tail for being pyrolyzed kiln section feed coal by kiln tail air-introduced machine, water steams
Stripping temperature is 100 ~ 150 DEG C, and pressure is -300 ~ -100Pa, and water vapour is 70~90% of Free water in feed coal（Quality point
Number）；
Most of feeding quickly cooling pond in step 2, the water vapour being extracted, makes most of water vapor temperature be reduced to 50 ~ 80 DEG C
Concurrent raw food is solidifying, while the dust for carrying water vapour secretly is precipitated in quickly cooling pond, the water temperature in quickly cooling pond maintains 30 ~ 50 DEG C,
Remainder uncondensed vapor feeding cooler is further condensed, and obtains steam condensate (SC)；Residue in the water vapour being extracted
Part is sent directly into hot-blast stove, is used as combustion adjuvant；
The raw coke oven gas that pyrolysis generation occurs for step 3, kiln hood section feed coal goes out after revolution pyrolysis kiln, is removed into hot precipitator
Raw coke oven gas dust content is by 50 ~ 100g/Nm after dirt, dedusting3It is reduced to 20 ~ 100mg/Nm3, the operating temperature of hot precipitator is
300~500 DEG C, the high temperature raw coke oven gas after dedusting enters back into Leng Gu workshop sections, and purified treatment is carried out to raw coke oven gas.
Feed arrangement in above-mentioned step 1 is inside and outside sleeve structure, and feed coal enters revolution pyrolysis kiln via inner cylinder, steamed
Steam flow is provided with steam pumping mouthful in outer barrel, is connected, passed through with kiln tail air-introduced machine by pipeline through the annular space between outer barrel and inner cylinder
Kiln tail air-introduced machine extracts the part water vapour turned round in pyrolysis kiln out.
N is additionally provided with above-mentioned step 12Blow device, is periodically purged to the pipeline of steam pumping, prevents from taking out steaming
The dust that water vapour is carried secretly during vapour is by line clogging.
The water vapour sent into above-mentioned step 2 in quickly cooling pond is 70~80% in the water vapour being extracted, as excellent
Select scheme.
The steam condensate (SC) obtained in above-mentioned step 2, can be used as situ industrial water after processing.
The hot blast of hot-blast stove discharge in above-mentioned step 2 is pyrolyzed the high-temperature gas heat carrier of kiln as revolution.
The kiln hood of above-mentioned revolution pyrolysis kiln is provided with air-introduced machine, by adjusting kiln hood air-introduced machine and kiln tail air-introduced machine, control
The pressure difference of kiln hood processed, kiln tail, and realize the separation of kiln tail water vapour and kiln hood raw coke oven gas.
Kiln hood, the control of kiln tail pressure difference：The kiln tail of revolution pyrolysis kiln is provided with CO detection devices, when detecting CO volume contents
During less than 3%, illustrate that kiln hood, kiln tail pressure are in poised state, only minimal amount of coal gas flows to kiln tail end, when detecting CO
When volume content is more than 3%, illustrates that kiln hood, kiln tail pressure are in non-equilibrium state, there is a certain amount of coal gas to flow to kiln tail end, this
When can stop or reduce by kiln tail draw water steam, come realize kiln hood, kiln tail pressure balance.
Above-mentioned low-order coal is at least one of lignite, jet coal, non caking coal.
Presently preferred embodiments of the present invention, rather than limitation of the present invention are the foregoing is only, the essence of the present invention is not being departed from
In the case of refreshing and scope, all equivalent changes and modifications made according to scope of the present invention patent should all belong to the special of the present invention
Within sharp protection domain.
Claims (7)
1. the separation method of water vapour and raw coke oven gas in a kind of low-order coal pyrolytic process, it is characterized in that：It comprises the following steps：
The fine-powdered feed coal of step 1, particle diameter less than 40mm is admitted to revolution pyrolysis kiln by feed arrangement and is pyrolyzed, and is pyrolyzed
Mode uses multitube rotary indirect heating type, and feed coal with the heat exchange of high-temperature gas heat carrier by absorbing heat, and feed coal is being returned
It is 30~90min to turn pyrolysis kiln residence time, and pyrolysis final temperature is 450~650 DEG C, is provided with and draws in the kiln tail of revolution pyrolysis kiln
Blower fan, is extracted out the water vapour for turning round the heated abjection of the kiln tail for being pyrolyzed kiln section feed coal by air-introduced machine, steam temperature is 100
~150 DEG C, pressure is -300~-100Pa, and water vapour is 70~90% of Free water in feed coal；
Most of feeding quickly cooling pond in step 2, the water vapour being extracted, makes most of water vapor temperature be reduced to 50 ~ 80 DEG C
Concurrent raw food is solidifying, while the dust for carrying water vapour secretly is precipitated in quickly cooling pond, the water temperature in quickly cooling pond maintains 30 ~ 50 DEG C,
Remainder uncondensed vapor feeding cooler is further condensed, and obtains steam condensate (SC)；Residue in the water vapour being extracted
Part is sent directly into hot-blast stove, is used as combustion adjuvant；
The raw coke oven gas that pyrolysis generation occurs for step 3, kiln hood section feed coal goes out after revolution pyrolysis kiln, is removed into hot precipitator
Raw coke oven gas dust content is by 50 ~ 100g/Nm after dirt, dedusting3It is reduced to 20 ~ 100mg/Nm3, the operating temperature of hot precipitator is
300~500 DEG C, the high temperature raw coke oven gas after dedusting enters back into Leng Gu workshop sections, and purified treatment is carried out to raw coke oven gas.
2. the separation method of water vapour and raw coke oven gas in low-order coal pyrolytic process according to claim 1, it is characterized in that：Step
Feed arrangement in rapid 1 is inside and outside sleeve structure, and feed coal enters revolution pyrolysis kiln via inner cylinder, and steam flows through outer barrel and inner cylinder
Between annular space, outer barrel is provided with steam pumping mouthful, connect by pipeline with kiln tail air-introduced machine, by kiln tail air-introduced machine by revolution
The part water vapour being pyrolyzed in kiln is extracted out.
3. the separation method of water vapour and raw coke oven gas in low-order coal pyrolytic process according to claim 1, it is characterized in that：Step
The N purged for the pipeline to steam pumping is additionally provided with rapid 12Blow device.
4. the separation method of water vapour and raw coke oven gas in low-order coal pyrolytic process according to claim 1, it is characterized in that：Step
The steam condensate (SC) obtained in rapid 2, can be used as situ industrial water after processing.
5. the separation method of water vapour and raw coke oven gas in low-order coal pyrolytic process according to claim 1, it is characterized in that：Step
The hot blast of hot-blast stove discharge in rapid 2 is pyrolyzed the high-temperature gas heat carrier of kiln as revolution.
6. the separation method of water vapour and raw coke oven gas in low-order coal pyrolytic process according to claim 1, it is characterized in that：Its
The kiln hood of revolution pyrolysis kiln is provided with air-introduced machine, by adjusting kiln hood air-introduced machine and kiln tail air-introduced machine, control kiln hood, the pressure of kiln tail
Difference, and realize the separation of kiln tail water vapour and kiln hood raw coke oven gas.
7. the separation method of water vapour and raw coke oven gas in low-order coal pyrolytic process according to claim 1, it is characterized in that：Its
Low-order coal is at least one of lignite, jet coal, non caking coal.
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| CN201710390154.XA CN107099315B (en) | 2017-05-27 | 2017-05-27 | Method for separating water vapor and raw coke oven gas in low-rank coal pyrolysis process |
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| CN201710390154.XA CN107099315B (en) | 2017-05-27 | 2017-05-27 | Method for separating water vapor and raw coke oven gas in low-rank coal pyrolysis process |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107890732A (en) * | 2017-12-21 | 2018-04-10 | 中冶焦耐(大连)工程技术有限公司 | A vapor absorbing device used in a coke intermediate bin adding water, humidifying and dust-reducing system |
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| CN101676364A (en) * | 2008-09-16 | 2010-03-24 | 沈阳铝镁设计研究院 | Calcining process of petroleum cokes by using large rotary kiln and equipment thereof |
| CN104946279A (en) * | 2015-06-01 | 2015-09-30 | 农业部规划设计研究院 | Rotary sectional heating biomass continuous pyrolysis equipment |
| US9309465B2 (en) * | 2012-07-20 | 2016-04-12 | Nippon Steel & Sumitomo Metal Corporation | Coal reforming method and coal reforming apparatus |
| CN106106724A (en) * | 2016-08-25 | 2016-11-16 | 冷瑞卿 | A kind of walking evaporating water drying machine |
| CN206069777U (en) * | 2016-08-11 | 2017-04-05 | 中信重工机械股份有限公司 | A kind of low order low-temperature pyrolysis of coal horizontal revolving kiln |
-
2017
- 2017-05-27 CN CN201710390154.XA patent/CN107099315B/en active Active
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101676364A (en) * | 2008-09-16 | 2010-03-24 | 沈阳铝镁设计研究院 | Calcining process of petroleum cokes by using large rotary kiln and equipment thereof |
| US9309465B2 (en) * | 2012-07-20 | 2016-04-12 | Nippon Steel & Sumitomo Metal Corporation | Coal reforming method and coal reforming apparatus |
| CN104946279A (en) * | 2015-06-01 | 2015-09-30 | 农业部规划设计研究院 | Rotary sectional heating biomass continuous pyrolysis equipment |
| CN206069777U (en) * | 2016-08-11 | 2017-04-05 | 中信重工机械股份有限公司 | A kind of low order low-temperature pyrolysis of coal horizontal revolving kiln |
| CN106106724A (en) * | 2016-08-25 | 2016-11-16 | 冷瑞卿 | A kind of walking evaporating water drying machine |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107890732A (en) * | 2017-12-21 | 2018-04-10 | 中冶焦耐(大连)工程技术有限公司 | A vapor absorbing device used in a coke intermediate bin adding water, humidifying and dust-reducing system |
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