CN103740389B - The multi-production process of low-rank coal cascade utilization - Google Patents

The multi-production process of low-rank coal cascade utilization Download PDF

Info

Publication number
CN103740389B
CN103740389B CN201410029216.0A CN201410029216A CN103740389B CN 103740389 B CN103740389 B CN 103740389B CN 201410029216 A CN201410029216 A CN 201410029216A CN 103740389 B CN103740389 B CN 103740389B
Authority
CN
China
Prior art keywords
gas
coal
enters
heat
gasification
Prior art date
Application number
CN201410029216.0A
Other languages
Chinese (zh)
Other versions
CN103740389A (en
Inventor
蒙爱红
吴洪肖
蒋景沛
Original Assignee
北京立化科技有限公司
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Application filed by 北京立化科技有限公司 filed Critical 北京立化科技有限公司
Priority to CN201410029216.0A priority Critical patent/CN103740389B/en
Publication of CN103740389A publication Critical patent/CN103740389A/en
Application granted granted Critical
Publication of CN103740389B publication Critical patent/CN103740389B/en

Links

Abstract

The multi-production process of low-rank coal cascade utilization, with circulation fluidized-bed combustion boiler, circulating fluidized bed dry distillation reactor device, circulating fluidized bed gasifying reactor for core, power generation cascade device realizes the recycle of low-disintegration coal step.Low-rank coal is through fragmentation, first montanin wax extraction is carried out after drying, then brown coal pyrolysis reactor is entered, adopt the raw gas of gasifying reactor as fluidizing medium, tar is obtained after destructive distillation, raw gas, semicoke enters gasifying reactor and carries out partial gasification, generating portion coal gas is as the fluidizing medium of dry distillation reactor device, the semicoke be not gasified totally enters burning boiler as fuel, produce heat by burning and produce steam for generating, by-product low-pressure steam can be used as gasifying reactor raw material, burning gained high-temperature semi-coke and hot ash enter dry distillation reactor device and gasifying reactor as thermal barrier, thus complete a circulation.The present invention can significantly improve the economic worth of low-rank coal, and step recycle significantly can reduce the discharge of pollutent, safe and reliable.

Description

The multi-production process of low-rank coal cascade utilization

Technical field

The present invention relates to a kind of low order cascade utilization multi-production process, can be used for the inferior coal comprehensive high-efficiencies such as brown coal and utilize technical field, particularly with the technique of brown coal step recycle coproduction electricity, steam, coal gas, tar and semicoke.

Background technology

China take coal as main energy sources resource, in recent years, in Inner Mongol, Yunnan, the ground such as Xinjiang found extensive coalfield continuously, main based on low-rank coal (brown coal account for the overwhelming majority), the coals such as brown coal, because moisture is high, ash content is high, volatile matter is high, calorific value is low, are often regarded inferior fuel steam coal; In addition oxidizable and spontaneous combustion, should not transport for long-distance, and therefore becomes the coal resource being difficult to strange land processing and utilization.How these resources of efficiency utilization, alleviate the pollution to environment simultaneously to greatest extent, day by day cause the concern of numerous experts and scholars.

The utilization of current coal resources in China, major part is based on the extremely low direct burning of the utilising efficiency of single production process, and other gasifications, liquefaction are also based on single process.Higher transformation efficiency is obtained in order to make conversion process, often need complicated technique and higher operational conditions, thus cause conversing technology complicated, equipment is huge, investment and production cost high, even if obtain high-level efficiency in single production technique, the overall utilising efficiency of its energy also can not be very high.In addition, single production process often causes the very large waste of resource.The direct burning of coal is exactly that the various components contained by coal are all utilized as fuel, and does not utilize the component wherein with higher utility value, as volatilization grades.So if the multiple production technique taking coal as resource are considered as a system, i.e. the polygenerations systeme of coal, improves coal resources utilization ratio from the angle of whole utilization efficiency, can solve faced resource and environment problem better.

The major technique direction of current Poly-generation can be divided into 3 classes: the thermoelectricity gas Poly-generation technology 1. based on pyrolysis of coal; 2. the thermoelectricity gas Poly-generation technology based on coal partial gasification; 3. the thermoelectricity gas Poly-generation technology based on coal is gasified totally.

According to the difference of reaction unit, thermal barrier character, this technology mainly can be divided at present: the thermoelectricity gas Poly-generation technology 1. based on fluidized bed coal pyrolysis; 2. the thermoelectricity gas Poly-generation technology based on moving-bed pyrolysis of coal; 3. the thermoelectricity gas Poly-generation technology based on burnt thermal barrier pyrolysis of coal.

Current multi-production process mainly biases toward the thermoelectricity gas coproduction of coal gasification/burning, or the thermoelectricity gas coproduction of destructive distillation/burning combination, does not often have the cogeneration of destructive distillation/gasification/burn combination.

Summary of the invention

The object of the invention is to the shortcoming overcoming existing brown coal Poly-generation technology, the multi-production process of a kind of heat based on brown coal cascade utilization, electricity, gas, tar and semicoke is provided, realize the cascade utilization of brown coal, have that energy consumption is low, reduced investment, brown coal utilization ratio are high, entire system thermal utilization advantages of higher.

The technical solution used in the present invention is:

Low-rank coal cascade utilization multi-production process, comprises raw coal pretreatment system, montanin wax extraction system, distillation system, gasification system, firing system, power generation system and dust-removal system; Described raw coal pretreatment system comprises crushing and screening device, drying installation; Distillation system comprises fluidized bed dry distillation device, carbonization gas solid separation device and charred ashes tripping device, it is characterized in that:

1) when starting, after the fragmentation in raw coal pretreatment system of low order feed coal, screening, particle diameter enters firing system burning at the feed coal of 0 ~ 20mm, the heat ash produced enters burning bed cyclonic separator with gas elutriation, and the heat ash under cyclonic separator is separated delivers to fluidized bed dry distillation device as thermal barrier; Heat smoke after cyclonic separator is separated and the heat exchange unit heat exchange of fluidized-bed combustion boiler, water in heat exchange unit is added thermogenesis water vapour, heat smoke after cooling enters into the feed coal after the dry crushing and screening of drying installation, then discharges after dust-removal system dedusting;

2), when normally running, low order feed coal is broken in raw coal pretreatment system and after sieving, granularity enters drying installation at the feed coal of 0 ~ 20mm, utilizes the heat smoke from firing system to carry out drying; Dried low-rank coal enters montanin wax extraction system, after extracting product montanin wax, enters fluidized bed dry distillation device and carries out the quick destructive distillation of low temperature (500 ~ 650 DEG C); Fluidized bed dry distillation device is using heat ash as thermophore, and the solid semicoke after destructive distillation and heat ash mixture enter charred ashes tripping device, and the semicoke under charred ashes tripping device is separated directly sends into gasification system, and the hot ash of destructive distillation enters ash silo; Gas-solid mixture after destructive distillation enters carbonization gas solid separation device, and the dust separated enters ash silo; Gas after carbonization gas solid separation device is separated enters tar condensing retrieving arrangement and reclaims tar, the raw gas part continuation circulation of discharging from tar condensing retrieving arrangement enters as fluidizing medium in fluidized bed dry distillation device, and another part is sent to the storage of raw gas gas-holder after purification;

3) the semicoke part entering gasification system is reacted with water vapor, oxygen generating gasification, gasification product coal gas is discharged from top of gasification furnace and is entered gasification section gas change heater, water in interchanger absorbs heat and produces water vapour, after heat exchange, gas temperature reduction enters gas recovery system for oil, and the coal gas after purifying treatment is sent to gas-holder storage; Another part semicoke endothermic temperature in gasification system raises further, and high-temperature semi-coke is discharged gasification system and entered firing system burning;

4) firing system comprises fluidized-bed combustion boiler, burning bed cyclonic separator and heat exchange unit, ash in ash silo sends into fluidized-bed combustion boiler, the heat that high-temperature semi-coke combustion processes produces heats this part ash and forms heat ash, the flue gas that burning produces carries hot ash and enters burning bed cyclonic separator, and the heat ash under cyclonic separator is separated sends fluidized bed dry distillation device back to as thermal barrier; Heat smoke after cyclonic separator is separated and the heat exchange unit heat exchange of fluidized-bed combustion boiler, add thermogenesis water vapour by the water in heat exchange unit, and the heat smoke after cooling enters the coal sample after the dry fragmentation of drying installation, then discharges through dust-removal system dedusting.

In technique scheme, from the raw gas that the tar condensing retrieving arrangement of distillation system is discharged, circulation enter fluidized bed dry distillation device as fluidizing medium before, first through gas preheater heat exchange, raw gas is preheating to 200-350 DEG C, then sends into fluidized bed dry distillation device.

In technique scheme, the high pressure steam that heat exchange unit produces is used for power generation system generating, and low-pressure steam delivers to gasification system as vaporized chemical, and the flue gas recirculation that gasification system produces gets back to drying installation as the coal sample after the dry crushing and screening of thermal source.

The present invention compared with prior art, has the following advantages and beneficial effect: low-rank coal cascade development uses by the present invention, substantially increases the added value of low-rank coal; Be coupled fluidized bed dry distillation, gasification technology, solid heat-carrying technology and Combustion technology of circulating fluidized, and entire system efficiency of utilization is higher, pollutant emission is less; Low-rank coal is carried out cascade development by this technique simultaneously, lower to each technique unit equipment requirements, and production operation is simple, has good economic benefit.

Accompanying drawing explanation

Fig. 1 is the multi-production process schema of a kind of heat based on brown coal cascade utilization, electricity, gas, tar and semicoke.

In figure: 1 – raw coal pretreatment system; 2 – montanin wax extraction systems; 3 – distillation systems; 4 – gasification systems; 5 – firing systems; 6 – crushing and screening devices; 7 – drying installations; 8 – fluidized bed dry distillation devices; 9 – carbonization gas solid separation devices; 10 – charred ashes tripping devices; 11 – tar condensing retrieving arrangements; 12 – gasification section gas change heaters; 13 – burning bed cyclonic separators; 14 – fluidized-bed combustion boilers; 15 – heat exchange units; 16 – power generation systems; 17 – dust-removal systems; 18 – ash silos; 19 – raw gas gas-holder; 20 – gas recovery system for oil.

Embodiment

Concrete technology of the present invention and operational scheme is described in detail below in conjunction with accompanying drawing:

Low-rank coal cascade utilization multi-production process, comprises raw coal pretreatment system 1, montanin wax extraction system 2, distillation system 3, gasification system 4, firing system 5, power generation system 16 and dust-removal system 17.Raw coal pretreatment system 1 comprises crushing and screening device 6, drying installation 7.Distillation system 3 comprises fluidized bed dry distillation device 8, carbonization gas solid separation device 9 and charred ashes tripping device 10.Low-rank coal cascade utilization multi-production process comprises the steps:

During startup, after the fragmentation in raw coal pretreatment system of low order feed coal, screening, particle diameter enters firing system 5 at the feed coal of 0 ~ 20mm and burns, the heat ash produced enters burning bed cyclonic separator 13 with gas elutriation, and the heat ash under cyclonic separator is separated delivers to fluidized bed dry distillation device 8 as thermal barrier; Heat smoke after cyclonic separator is separated and heat exchange unit 15 heat exchange of fluidized-bed combustion boiler, water in heat exchange unit 15 is added thermogenesis water vapour, heat smoke after cooling enters into the feed coal after the dry crushing and screening of drying installation 7, then discharges after dust-removal system 17 dedusting.

When normally running after startup, low order feed coal is broken and after sieving in raw coal pretreatment system, granularity enters drying installation 7 at the feed coal of 0 ~ 20mm, the high-temperature tail gas of about 150 DEG C from firing system 5 is utilized to carry out drying as thermal source to brown coal, brown coal moisture is down to about 10%, and dried brown coal enter the extraction that first montanin wax extraction system 2 carries out montanin wax.After extracting product montanin wax, enter fluidized bed dry distillation device 8 and carry out the quick destructive distillation of low temperature (500 ~ 650 DEG C); Since fluidized bed dry distillation device 7, the heat ash of about 900 DEG C of auto-combustion system is as thermophore, solid semicoke after destructive distillation and heat ash mixture enter charred ashes tripping device 10, semicoke under charred ashes tripping device is separated directly sends into gasification system 3, and the hot ash of destructive distillation enters ash silo 18; Gas-solid mixture after destructive distillation enters carbonization gas solid separation device 9, and the dust separated also enters ash silo 18; Gas after carbonization gas solid separation device is separated enters tar condensing retrieving arrangement 11 and reclaims tar, the raw gas part continuation circulation of discharging from tar condensing retrieving arrangement enters as fluidizing medium in fluidized bed dry distillation device 8, and another part is sent to raw gas gas-holder 19 and preserves after purification.

The semicoke (about 500 DEG C ~ 600 DEG C) that destructive distillation produces enters gasification system 4, reacts with water vapor (about 0.6MPa, 165 DEG C), oxygen generating gasification.Water vapour comes from the low-pressure steam that firing system produces.Gasification system can be designed as normal pressure, fluidized-bed form, temperature about 900 DEG C.Water vapour and oxygen are blended in stove as main reactant and semicoke on the one hand and carry out gasification reaction, play the effect of fluidizing medium carrier gas on the other hand.In gasification system, part semicoke and water vapor, the reaction of oxygen generating gasification are consumed, gasification product coal gas is discharged from top of gasification furnace and is entered gasification section gas change heater 12, water in interchanger absorbs heat and produces water vapour, after heat exchange, gas temperature reduction enters gas recovery system for oil 20, and the coal gas after purifying treatment is sent to gas-holder storage.After the semicoke that another part is not consumed absorbs heat and heats up in gasification system, (about 900 DEG C) are discharged gasification system as high-temperature semi-coke and are entered firing system 5 and burn.

Firing system 5 comprises fluidized-bed combustion boiler 14, burning bed cyclonic separator 13 and heat exchange unit 15, ash in ash silo 18 sends into fluidized-bed combustion boiler 14, the heat that high-temperature semi-coke combustion processes produces heats this part ash and forms heat ash, the flue gas that burning produces carries hot ash and enters burning bed cyclonic separator 13, and the heat ash under cyclonic separator is separated sends fluidized bed dry distillation device 8 back to as thermal barrier; Heat smoke after cyclonic separator is separated and heat exchange unit 15 heat exchange of fluidized-bed combustion boiler, the water in heat exchange unit 15 is added thermogenesis water vapour, and the heat smoke after cooling enters the coal sample after the dry fragmentation of drying installation 7, then discharges through dust-removal system 17 dedusting.Consider that whole system material, energy balance regulate, the heat ash that burning bed cyclonic separator 13 separates, transport pipe leaves bypass, and unnecessary heat ash does not enter dry distillation tower and is directly disposed to refrigerating unit from bypass, cool laggard enter lime-ash storage tank.

The circulating gas intake ducting of fluidized bed dry distillation device 8 can set up gas preheater, gas temperature is preheating to raw gas is preheating to about 200-350 DEG C, the control to destructive distillation device interior reaction temperature can be strengthened, make the control of temperature in destructive distillation device, regulate sensitiveer, timely.

The high pressure steam that heat exchange unit 15 produces is used for power generation system 16 and generates electricity, and low-pressure steam delivers to gasification system 4 as vaporized chemical, and the flue gas recirculation that gasification system 4 produces gets back to drying installation 7 as the coal sample after the dry crushing and screening of thermal source.

Cascade development of the present invention uses low-rank coal, substantially increases the added value of low-rank coal.Whole technique has been coupled fluidized bed dry distillation, gasification technology, solid heat-carrying technology and Combustion technology of circulating fluidized, and entire system efficiency of utilization is higher, pollutant emission is less, has good economic benefit.

Claims (1)

1. low-rank coal cascade utilization multi-production process, comprises raw coal pretreatment system (1), montanin wax extraction system (2), distillation system (3), gasification system (4), firing system (5), power generation system (16) and dust-removal system (17); Described raw coal pretreatment system (1) comprises crushing and screening device (6), drying installation (7); Distillation system (3) comprises fluidized bed dry distillation device (8), carbonization gas solid separation device (9) and charred ashes tripping device (10), it is characterized in that:
1) when starting, after the fragmentation in raw coal pretreatment system of low order feed coal, screening, particle diameter enters firing system (5) burning at the feed coal of 0 ~ 20mm, the heat ash produced enters burning bed cyclonic separator (13) with gas elutriation, and the heat ash under cyclonic separator is separated delivers to fluidized bed dry distillation device (8) as thermal barrier; Heat smoke after cyclonic separator is separated and heat exchange unit (15) heat exchange of fluidized-bed combustion boiler, water in heat exchange unit (15) is added thermogenesis water vapour, heat smoke after cooling enters into the feed coal after drying installation (7) dry crushing and screening, then discharges after dust-removal system (17) dedusting;
2), after low order feed coal is broken, sieves in raw coal pretreatment system, granularity enters drying installation (7) at the feed coal of 0 ~ 20mm, utilizes the heat smoke from firing system (5) to carry out drying; Dried low-rank coal enters montanin wax extraction system (2), and after extracting product montanin wax, enter fluidized bed dry distillation device (8) and carry out the quick destructive distillation of low temperature, low-temperature pyrolysis temperature is 500 ~ 650 DEG C; Fluidized bed dry distillation device (7) is using heat ash as thermophore, and the solid semicoke after destructive distillation and heat ash mixture enter charred ashes tripping device (10), and the semicoke under charred ashes tripping device is separated directly sends into gasification system (3), and the hot ash of destructive distillation enters ash silo (18); Gas-solid mixture after destructive distillation enters carbonization gas solid separation device (9), and the dust separated enters ash silo (18); Gas after carbonization gas solid separation device is separated enters tar condensing retrieving arrangement (11) and reclaims tar, the raw gas part continuation circulation of discharging from tar condensing retrieving arrangement enters as fluidizing medium in fluidized bed dry distillation device (8), and another part is sent to raw gas gas-holder (19) storage after purification;
3) the semicoke part entering gasification system (4) is reacted with water vapor, oxygen generating gasification, gasification product coal gas is discharged from top of gasification furnace and is entered gasification section gas change heater (12), water in interchanger absorbs heat and produces water vapour, after heat exchange, gas temperature reduction enters gas recovery system for oil (20), and the coal gas after purifying treatment is sent to gas-holder storage; Another part semicoke endothermic temperature in gasification system raises further, and high-temperature semi-coke is discharged gasification system and entered firing system (5) burning;
4) firing system (5) comprises fluidized-bed combustion boiler (14), burning bed cyclonic separator (13) and heat exchange unit (15), ash in ash silo (18) sends into fluidized-bed combustion boiler (14), the heat that high-temperature semi-coke combustion processes produces heats this part ash and forms heat ash, the flue gas that burning produces carries hot ash and enters burning bed cyclonic separator (13), and the heat ash under cyclonic separator is separated sends fluidized bed dry distillation device (8) back to as thermal barrier; Heat smoke after cyclonic separator is separated and heat exchange unit (15) heat exchange of fluidized-bed combustion boiler, water in heat exchange unit (15) is added thermogenesis water vapour, heat smoke after cooling enters the coal sample after drying installation (7) dry fragmentation, then discharges through dust-removal system (17) dedusting;
5)from the raw gas that the tar condensing retrieving arrangement (11) of distillation system (3) is discharged, circulation enter fluidized bed dry distillation device (8) as fluidizing medium before, first through gas preheater heat exchange, raw gas is preheating to 200-350 DEG C, then sends into fluidized bed dry distillation device (8);
6)the height that heat exchange unit (15) produces, middle pressure steam generate electricity for power generation system (16), low-pressure steam delivers to gasification system (4) as vaporized chemical, and the flue gas recirculation that gasification system (4) produces gets back to drying installation (7) as the coal sample after the dry crushing and screening of thermal source.
CN201410029216.0A 2014-01-22 2014-01-22 The multi-production process of low-rank coal cascade utilization CN103740389B (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
CN201410029216.0A CN103740389B (en) 2014-01-22 2014-01-22 The multi-production process of low-rank coal cascade utilization

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
CN201410029216.0A CN103740389B (en) 2014-01-22 2014-01-22 The multi-production process of low-rank coal cascade utilization

Publications (2)

Publication Number Publication Date
CN103740389A CN103740389A (en) 2014-04-23
CN103740389B true CN103740389B (en) 2015-11-18

Family

ID=50497458

Family Applications (1)

Application Number Title Priority Date Filing Date
CN201410029216.0A CN103740389B (en) 2014-01-22 2014-01-22 The multi-production process of low-rank coal cascade utilization

Country Status (1)

Country Link
CN (1) CN103740389B (en)

Families Citing this family (10)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN103952197A (en) * 2014-05-13 2014-07-30 西南化工研究设计院有限公司 Process for co-producing LNG (Liquefied Natural Gas) by using pyrolysis gas generated in power generation system
CN105441135A (en) * 2014-06-25 2016-03-30 通用电气公司 Coal gasification method
CN104087327B (en) * 2014-07-15 2015-06-24 黎城蓝天燃气开发有限公司 Destructive distillation gasification equipment
CN104099134B (en) * 2014-07-15 2015-12-02 黎城蓝天燃气开发有限公司 A kind of destructive gasifying device and the quick method for destructive distillation of coal dust
CN104946282B (en) * 2015-06-15 2017-05-31 宋军 A kind of handling process of smalls
CN105001899A (en) * 2015-07-07 2015-10-28 新疆帕拉菲精细化工股份有限公司 Method for preparing clean coal-based synthetic wax
CN105038827B (en) * 2015-07-10 2017-10-10 北京雷浩环保能源技术有限公司 A kind of low order broken coal sub-prime classification gradient utilization system and method
CN105131988B (en) * 2015-08-12 2017-08-01 石家庄新华能源环保科技股份有限公司 The device that a kind of pure carbon powder production heat integration is utilized
CN105400532B (en) * 2015-12-04 2017-10-10 中国重型机械研究院股份公司 A kind of polygenerations systeme and method based on pyrolysis of coal
CN105505467A (en) * 2015-12-04 2016-04-20 中国天辰工程有限公司 Coupling technology adopting lignite-gasification gas production and dry distillation upgrading

Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN101016482A (en) * 2006-01-18 2007-08-15 董久明 Fine coal grading cleaning multiple utilization technique with pyrolysis as first stage
CN102504842A (en) * 2011-11-09 2012-06-20 浙江大学 Three-fluidized-bed solid heat carrier coal pyrolysis, gasification and combustion cascade utilization method
CN103013576A (en) * 2012-12-10 2013-04-03 陕西华祥能源科技集团有限公司 IGCC (Integrated Gasification Combined Cycle) poly-generation device and method based on pyrolysis and gasification of low metamorphic powdered coal

Family Cites Families (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP2013241487A (en) * 2012-05-17 2013-12-05 Central Research Institute Of Electric Power Industry System for carbonizing and gasifying biomass

Patent Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN101016482A (en) * 2006-01-18 2007-08-15 董久明 Fine coal grading cleaning multiple utilization technique with pyrolysis as first stage
CN102504842A (en) * 2011-11-09 2012-06-20 浙江大学 Three-fluidized-bed solid heat carrier coal pyrolysis, gasification and combustion cascade utilization method
CN103013576A (en) * 2012-12-10 2013-04-03 陕西华祥能源科技集团有限公司 IGCC (Integrated Gasification Combined Cycle) poly-generation device and method based on pyrolysis and gasification of low metamorphic powdered coal

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
朱之培.煤的化工利用.《煤的化工利用》.化学工业出版社,1979,第134-137. *

Also Published As

Publication number Publication date
CN103740389A (en) 2014-04-23

Similar Documents

Publication Publication Date Title
Vamvuka Bio‐oil, solid and gaseous biofuels from biomass pyrolysis processes—an overview
RU2519441C1 (en) Technology and device for obtaining synthesis gas from biomass by pyrolysis
Chopra et al. A review of fixed bed gasification systems for biomass
Erlach et al. Combined hydrothermal carbonization and gasification of biomass with carbon capture
US6148599A (en) Process and apparatus for gasifying solid carbonaceous material having a high moisture content
AU2008215182B2 (en) Drying and gasification process
CN102212399B (en) Thermal pyrolysis combination method and device
CN101921627B (en) Air-oil co-production device forcoupling fluidized bed pulverized coal gasification and solid heat carrier pyrolysis and method therefor
RU2128683C1 (en) Method of utilizing solid fuels with low calorific capacity
CN101613615B (en) Method and system for decoupling and upgrading coal
JP5619269B2 (en) Method and system for producing synthesis gas from biomass by carbonization
CN101260307B (en) Brown coal drying quality-increasing device and technique
CN1931959B (en) Compositely circulating high temperature gasifying process for making synthetic gas with biomass
CN1173015C (en) Fluidized bed water gas production method equipped with auxiliary bed reactor and installation thereof
CN101781583B (en) Method and device for utilizing high value through pyrolysis and gasification of coal
CN103758592B (en) CO2 gas coke chemical-looping combustion power generating system and method
CN101113344B (en) Kerosene shale comprehensive utilization process
CN104789245B (en) A kind of pyrolysis gasifying device and technique
CN101108970B (en) Method for manufacturing wet fuel by rapid common thermal decomposition of biomass and coal
CN101117584A (en) Integral process for oil shale retorting oil refining and coal-char combustion power generation
CN101649214B (en) Externally-fired oil shale distillation process and device
CN102200275B (en) Combustion device for dewatering upgradation of lignite and reduction of nitrogen oxide emission and method thereof
CN102676236B (en) Method and device for three-stage separating biomass gasification
CN102585913B (en) Coal gas, tar, semi-coke and steam poly-generation method based on fluidized bed pyrolysis technology
CN104673340B (en) Systematic device and method for biomass microwave pyrolysis poly-generation by adopting combined washing and baking pretreatment

Legal Events

Date Code Title Description
C06 Publication
PB01 Publication
C10 Entry into substantive examination
SE01 Entry into force of request for substantive examination
COR Change of bibliographic data
CB02 Change of applicant information

Address after: 100084 room 4, floor 406, building B, comprehensive research building, Tsinghua University, Beijing, Haidian District

Applicant after: BEIJING LIHUA SCIENCE TECHNOLOGY CO., LTD.

Address before: 100084 room 4, floor 406, building B, comprehensive research building, Tsinghua University, Beijing, Haidian District

Applicant before: BEIJING TIANSU SUNLIGHT LOW CARBON TECHNOLOGY CO., LTD.

C14 Grant of patent or utility model
GR01 Patent grant
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: 20151118

Termination date: 20180122