CN108048140A - A kind of method and apparatus being pyrolyzed with gasification coupling coproduction oil gas - Google Patents
A kind of method and apparatus being pyrolyzed with gasification coupling coproduction oil gas Download PDFInfo
- Publication number
- CN108048140A CN108048140A CN201711439454.9A CN201711439454A CN108048140A CN 108048140 A CN108048140 A CN 108048140A CN 201711439454 A CN201711439454 A CN 201711439454A CN 108048140 A CN108048140 A CN 108048140A
- Authority
- CN
- China
- Prior art keywords
- gas
- gasification
- pyrolysis
- coal
- coproduction
- 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
Classifications
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/58—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels combined with pre-distillation of the fuel
- C10J3/60—Processes
- C10J3/64—Processes with decomposition of the distillation products
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/72—Other features
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/72—Other features
- C10J3/82—Gas withdrawal means
- C10J3/84—Gas withdrawal means with means for removing dust or tar from the gas
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2200/00—Details of gasification apparatus
- C10J2200/15—Details of feeding means
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0913—Carbonaceous raw material
- C10J2300/0916—Biomass
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0913—Carbonaceous raw material
- C10J2300/093—Coal
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/16—Integration of gasification processes with another plant or parts within the plant
- C10J2300/1603—Integration of gasification processes with another plant or parts within the plant with gas treatment
Landscapes
- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Combustion & Propulsion (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Organic Chemistry (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
- Industrial Gases (AREA)
Abstract
The invention discloses a kind of method and devices being pyrolyzed with gasification coupling coproduction oil gas.Method realizes that process is：Feed coal falls parallel with carrier gas in down-flow fluidized bed using ECT pyrolysis reaction section occurs pyrolytic reaction, and the biomass with subsequently adding in or carrier gas carry out copyrolysis, make the hydrogen migration in biomass into coal, semicoke and pyrolysis gas are obtained in down-flow fluidized bed using ECT pyrolysis reaction section bottom；Semicoke continues to fall eventually falls into fluidized gasification conversion zone by vertical gas mixing section, and generation gasification reaction, generation gasification gas and lime-ash are inversely contacted with gasifying agent without cooling；Gasification gas is flowed up carries out coke tar reforming reaction after vertical gas mixing section mixes with pyrolysis gas into horizontal type reforming reaction section, and burnt oil and gas is obtained after refrigerated separation.The invention discloses a kind of co-production technology for realizing high-quality tar, coal gas, have many advantages, such as it is easy to operate, it is compact-sized, the thermal efficiency is high, have great importance to Modern Coal-based Chemical industry development.
Description
Technical field
The invention belongs to technical field of energy utilization, are related to a kind of coal and biomass graded sub-prime high-efficiency cleaning conversion skill
Art, more particularly to a kind of using coal and biomass as the pyrolysis of raw material and the method and apparatus of gasification coupling coproduction oil gas.
Background technology
Coal is the main energy sources in China, within the following long duration, coal China's primary energy consumption in still
It occupies an leading position.With the reduction of high rotten coal resource, the utilization of low-order coal is increasingly taken seriously.But low-order coal is being burnt
Or gasification utilizes not only inefficiency, but also petroleum resources therein is wasted in the process.Based on pyrolysis of coal, coupling
Pyrolysis of coal, gasification and burning can be combined by closing the Poly-generation technology of other techniques, produce coal gas, oil product, cleaning
The multiple products such as semicoke, electricity and steam, the utility value for realizing coal resources maximize.But there is technique streams for the prior art
The problems such as journey is long, equipment is more, complicated for operation and oil quality is poor, and pipeline easily blocks.
The advantages that biomass energy is enriched due to possessing total amount, is widely distributed, hydrogen-carbon ratio is high and renewable is subject to various countries
Extensive concern.But biomass is seasonal strong, it is low to be not easy storage, energy density for a long time, if carry out using only, it is easy to
There is the problem of raw material supply is unstable.The characteristics of for coal richness carbon, biomass hydrogen-rich, coal and biomass are utilized altogether, not only
It can promote the sustainable use of fossil fuel and the abundant excavation of regenerative resource, while can also reduce environmental pollution, produce
The product of high-quality realizes efficient, the clean utilization of coal and biomass.
The content of the invention
In order to solve the problems in the existing technology, the invention discloses a kind of using coal and biomass as the pyrolysis of raw material
With the method and apparatus of gasification coupling coproduction oil gas, it is desirable to provide it is a kind of to realize high-quality tar, the method for coal gas coproduction,
The low temperature distillation technique of coal with gasification process is combined, the comprehensive utilization ratio of coal resources is improved, realizes
Step, cleaning, the high added value trans-utilization of coal resources, have many advantages, such as it is easy to operate, it is compact-sized, the thermal efficiency is high, it is right
Modern Coal-based Chemical industry development has great importance.
The technical proposal of the invention is realized in this way：
On the one hand, the invention discloses a kind of using coal and biomass as the pyrolysis of raw material and the method for gasification coupling coproduction oil gas,
Feed coal with carrier gas in down-flow fluidized bed using ECT pyrolysis reaction section falls and carries out pyrolytic reaction parallel, and biomass or load with subsequently adding in
Gas carries out copyrolysis, makes the hydrogen migration in biomass into coal, semicoke and pyrolysis gas are obtained in down-flow fluidized bed using ECT pyrolysis reaction section bottom；
Semicoke continues to fall eventually falls into fluidized gasification conversion zone by vertical gas mixing section, is inversely connect with gasifying agent without cooling
The raw gasification reaction of triggering, generation gasification gas and lime-ash；Gasification gas is flowed up to be mixed with pyrolysis gas in vertical gas mixing section
To pyrolytic gasification mixed gas, pyrolytic gasification mixed gas enters horizontal type reforming reaction section and coke tar reforming reaction occurs, through whirlwind
Deduster removes flying dust, and burnt oil and gas is obtained after refrigerated separation.
As a kind of preferred embodiment, the feed coal is low-order coal, and the biomass is agriculture and forestry organic waste material.
In order to reach preferably effect, coal and biomass mass ratio are 1 in the raw material:0.25~0.5;Carrier gas and raw material
（Coal and biomass）Than for: 0.6 Nm3/ kg；Gasifying agent and raw material（Coal and biomass）Than for 0.8 Nm3/ kg.
As a kind of preferred embodiment, the carrier gas is pyrolytic gasification mixed gas, the gasifying agent be by oxygen and
Vapor presses 1：2 volume ratio mixes.
As a kind of preferred embodiment, the temperature of the down-flow fluidized bed using ECT pyrolysis reaction section is 500-800 DEG C, the fluid bed
The temperature of gasification reaction section is 900-1000 DEG C, and the temperature of the horizontal type reforming reaction section is 400-600 DEG C, the vertical gas
Mixing section temperature is 400-600 DEG C, and the cyclone dust collectors temperature is 300-350 DEG C；It is preferred that the down-flow fluidized bed using ECT pyrolytic reaction
The temperature range of section is arranged to three-level step temperature from top to bottom, is respectively epimere:600-800 DEG C, stage casing：500-600 DEG C, under
Section：400-500 DEG C, wherein, the warm area size of three gradient temperatures and start-stop position are determined according to raw materials used property.
In addition, catalysis can be added in horizontal type reforming reaction section in order to improve the selectivity of reforming reaction and reforming efficiency
Agent.
On the other hand, it is used to implement above-mentioned pyrolysis and gasification using coal and biomass as raw material the invention also discloses a kind of
The device of coupled cogeneration oil gas, including coupled reactor and cold separation unit, the coupled reactor is by being interconnected
What down-flow fluidized bed using ECT pyrolysis reaction section, vertical gas mixing section, fluidized gasification conversion zone and horizontal type reforming reaction section were formed；Described
The top and middle part of down-flow fluidized bed using ECT pyrolysis reaction section are respectively equipped with the first feeder and the second feeder, and in first feeder
First charging aperture and the first carrier gas inlet are equipped with, second charging aperture is equipped on second feeder and the second carrier gas enters
Mouthful；The vertical gas mixing section respectively with the material outlet of the down-flow fluidized bed using ECT pyrolysis reaction section bottom, the fluidized gasification
The gaseous mixture arrival end of the top port of conversion zone and the horizontal type reforming reaction section connects, and passes through vertical gas mixing
Section is connected with fluidized gasification conversion zone；Gas distribution grid and pre- point are equipped in the lower part of the fluidized gasification conversion zone
The gas air compartment of cloth gasifying agent is equipped with gasification agent inlet on the air compartment side wall, and ash discharging hole is equipped in the air compartment bottom；Institute
The mixed gas outlet for stating horizontal type reforming reaction section is connected with cold separation unit；It can be petrochemical industry wherein to separate cooling unit
Any one or more equipment combination of separation, refrigerating function can be realized in field.The separation cooling unit is by dedusting
Device, cooler and separator composition, the mixed gas outlet end of the horizontal type pipe coke tar reforming conversion zone successively with deduster, cold
But device is connected with separator.
As a kind of preferred embodiment, first feeder and the second feeder are star-like feeder, and described the
One carrier gas inlet is located at the lower section of first charging aperture, and second carrier gas inlet is located at the lower section of second charging aperture.It is preferred that
The top of the first star-like feeder is equipped with opening as first charging aperture, enters in first star-like the first carrier gas of feeder lower end
Mouthful, opening is equipped at the top of the described second star-like feeder as second charging aperture, in the second star-like feeder lower end second
Carrier gas inlet.
Preferably, the deduster be cyclone dust collectors, the cooler be jacket type cooler, the separator
Strength of attaching most importance to liquid/gas separator.
The present invention advantageous effects be：
（1）The sub-prime that raw material has been coupled in a reactor utilizes, as pyrolysis-gasification-coke tar reforming process, has operation
Simply, the advantages of thermal efficiency is high realizes the coproduction of high-quality tar, coal gas；
（2）Down-flow fluidized bed using ECT pyrolysis reaction section is divided into three sections from top to bottom, is preferably set up step temperature field and carries out classification pyrolysis, regulation and control
The secondary response of volatiles improves tar yield, improves tar quality；
（3）Coal and biomass carry out quick copyrolysis, and the hydroperoxyl radical in biomass is made to participate in the pyrolytic process of coal, improve
Tar yield and improvement tar quality；
（4）The semicoke generated is pyrolyzed without supercooling direct gasification, gasification efficiency is improved, avoids semicoke cooling and reheat gas
The energy loss of change；
（5）Coal tar and biomass char carry out common gasification, and the alkali and alkaline earth metal ions being rich in biomass char play gasification reaction
To catalytic action, char Gasification reactivity is improved, gasification reaction temperature is reduced, so as to save energy consumption, reduces tar anti-
Answer the decomposition in device；
（6）Gaseous state tar it is uncooled it is preceding it is reformed using pyrolytic gasification gaseous mixture, improve tar quality；
（7）Obtained coal gas is the gaseous mixture of pyrolysis coal gas gentleization coal gas, combines gasification gas richness carbon and pyrolysis coal gas is rich
The two-fold advantage of hydrogen；Preparing synthetic gas technology is total to using gasification gas and pyrolysis coal gas, by CH4And CO2Synthesis is prepared after reformation
Gas.
Description of the drawings
It in order to illustrate the embodiments of the present invention more clearly or scheme of the prior art, below will be to embodiment or existing skill
Attached drawing is briefly described needed in art description, it should be apparent that, the accompanying drawings in the following description is only the present invention
Some embodiments, for those of ordinary skill in the art, without having to pay creative labor, can be with root
Other attached drawings are obtained according to these attached drawings.
Fig. 1 is pyrolysis and the structure diagram of gasification coupling coproduction oil gas device.
In figure：1. the first star-like feeder, 2. first carrier gas inlets, 3. first charging apertures, 4. second star-like feeders, 5.
Second carrier gas inlet, 6. second charging apertures, 7. down-flow fluidized bed using ECT pyrolysis reaction sections, the outlet of 8. pyrolysis products, 9. vertical gas mixing sections,
10. fluidized gasification conversion zone, 11. gas distribution grids, 12. air compartments, 13. gasification agent inlets, 14. ash discharging holes, 15. horizontal type pipes are burnt
Oily reforming reaction section, 16. mixed gas outlet ends, 17. cyclone dust collectors, 18. jacket type coolers, 19. gravity gas-liquid separators.
Specific embodiment
Below in conjunction with the attached drawing in the embodiment of the present invention, the technical solution in the embodiment of the present invention is carried out clear, complete
Site preparation describes.Obviously, described embodiment is only the part of the embodiment of the present invention, instead of all the embodiments.Base
Embodiment in the present invention, those of ordinary skill in the art obtained without making creative work it is all its
His embodiment, belongs to the scope of protection of the invention.
Embodiment
As shown in Figure 1 is a kind of using coal and biomass as the pyrolysis of raw material and the device of gasification coupling coproduction oil gas, including
Coupled reactor and cold separation unit；Wherein, the cold separation unit is by sequentially connected cyclone dust collectors 17, chuck
What formula cooler 18 and gravity gas-liquid separator 19 formed, the coupled reactor is by interconnected down-flow fluidized bed using ECT pyrolytic reaction
What section 7, vertical gas mixing section 9, fluidized gasification conversion zone 10 and horizontal type reforming reaction section 15 were formed；In down-flow fluidized bed using ECT heat
The top and middle part for solving conversion zone 7 are respectively equipped with the first star-like 1 and second star-like feeder 4 of feeder, and in first star
The bottom of type feeder 1 is equipped with opening as 3 and first carrier gas inlet 2 of first charging aperture, in the described second star-like feeder
4 bottom is equipped with opening as 6 and second carrier gas inlet 5 of second charging aperture；The vertical gas mixing section 9 respectively with institute
State the pyrolysis product outlet 8 of the bottom of down-flow fluidized bed using ECT pyrolysis reaction section 7, the top of the fluidized gasification conversion zone 10 port, with
And the combi inlet port end connection of the horizontal type reforming reaction section 15, form " T " font；In the fluidized gasification conversion zone 10
Lower part be equipped with gas distribution grid 11, the gas air compartment 12 of pre- distribution gasifying agent, gasifying agent is equipped on 12 side wall of air compartment
Entrance 13 is equipped with ash discharging hole 14 in 12 bottom of air compartment；The mixed gas outlet end of the horizontal type reforming reaction section 15 successively with
Cyclone dust collectors 17, jacket type cooler 18 and gravity gas-liquid separator 19 connect.
The method being pyrolyzed with gasification coupling coproduction oil gas is illustrated with reference to Fig. 1：
（1）The raw material low order coal particle entered by the first star-like feeder 1 and the carrier gas entered by the first carrier gas inlet 2（This
Method produces pyrolytic gasification mixed gas）Bring down-flow fluidized bed using ECT pyrolysis reaction section 7 into, whereabouts while carries out pyrolytic reaction；Raw material is given birth to
Material grains are entered by the second star-like feeder 4, the carrier gas entered from the second carrier gas inlet 5（The heat production of this method institute is vented one's spleen
Change mixed gas）It brings down-flow fluidized bed using ECT pyrolysis reaction section 7 into, raw material low order coal particle and biomass starting material particle is made to be pyrolyzed in down-flow fluidized bed using ECT
Be rapidly heated in conversion zone 7 in dropping process 500-800 DEG C progress copyrolysis, and make biomass pyrolytic generate it is hydrogeneous from
By group-transfer into pyrolysis of coal volatile matter, semicoke and pyrolysis gas are obtained in 7 bottom of down-flow fluidized bed using ECT pyrolysis reaction section；Semicoke and pyrolysis gas
Continue to move downwardly into the vertical gas mixing section 9 that temperature is 400-600 DEG C；
（2）Semicoke into vertical gas mixing section 9 continues to fall, into fluidized gasification conversion zone 10 without cooling directly with
Inversely contact issues raw gasification reaction at 900-1000 DEG C for the gasifying agent that is mixed by oxygen and vapor, generation gasification gas and
Lime-ash；Gasification lime-ash is discharged from bottom ash discharging hole 14；The gasification gas of generation is moved upwards into vertical gas mixing section 9 and pyrolysis
Gas is mixed to get pyrolytic gasification mixed gas, and pyrolytic gasification mixed gas enters horizontal type reforming reaction section 15；Pyrolytic gasification mixes
Occur to reform at 400-600 DEG C with other gases in pyrolytic gasification gaseous mixture anti-containing gaseous state tar, gaseous state tar in gas
It should；
（4）Pyrolytic gasification gaseous mixture from reforming reaction section 15 out is 300-350 DEG C of cyclone dust collectors 17 by temperature
Flying dust is removed, gaseous state tar is cooled down by jacket type cooler 18, it is isolated using gravity gas-liquid separator 19
Burnt oil and gas.
Certainly, catalysis can be added in horizontal type reforming reaction section 15 in order to improve the selectivity of reforming reaction and reforming efficiency
Agent.
The foregoing is merely illustrative of the preferred embodiments of the present invention, is not intended to limit the invention, all essences in the present invention
With within principle, any modifications, equivalent replacements and improvements are made should all be included in the protection scope of the present invention god.
Claims (10)
- A kind of 1. method being pyrolyzed with gasification coupling coproduction oil gas, it is characterised in that：Coal is with carrier gas in down-flow fluidized bed using ECT pyrolysis reaction section In fall pyrolytic reaction occurs parallel, and the biomass with subsequently adding in and carrier gas carry out copyrolysis, turn the hydrogen in biomass It moves on in coal, semicoke and pyrolysis gas is obtained in down-flow fluidized bed using ECT pyrolysis reaction section bottom；Semicoke, which continues to fall, passes through vertical gas mixing Section eventually falls into fluidized gasification conversion zone, and generation gasification reaction is inversely contacted with gasifying agent without cooling, generation gasification gas with Lime-ash；Gasification gas is flowed up is mixed to get pyrolytic gasification mixed gas, mixed gas with pyrolysis gas in vertical gas mixing section Coke tar reforming reaction is carried out into horizontal type reforming reaction section, flying dust is removed by cyclone dust collectors, tar is obtained after refrigerated separation And coal gas.
- 2. pyrolysis and the method for gasification coupling coproduction oil gas as described in claim 1, it is characterised in that：The feed coal is low order Coal, including lignite, jet coal, dross coal and weakly caking coal, the biomass is agriculture and forestry organic waste material.
- 3. pyrolysis and the method for gasification coupling coproduction oil gas as described in claim 1, it is characterised in that：Coal and the mass ratio of biomass are 1:0.25~0.5;Carrier gas is 0.6 Nm with coal and biomass ratio3/ kg；Gasifying agent and original Coal and biomass ratio are 0.8 Nm3/ kg.
- 4. pyrolysis and the method for gasification coupling coproduction oil gas as described in claim 1, it is characterised in that：The carrier gas is pyrolysis gas Change mixed gas, the gasifying agent is by 1 by oxygen and vapor：2 volume ratio mixes.
- 5. pyrolysis and the method for gasification coupling coproduction oil gas as described in claim 1, it is characterised in that：The down-flow fluidized bed using ECT pyrolysis is anti- Answering the temperature of section, the temperature of the fluidized gasification conversion zone is 900-1000 DEG C, the horizontal type pipe tar weight for 500-800 DEG C The temperature of whole conversion zone is 400-600 DEG C, and the vertical gas mixing section temperature is 400-600 DEG C, the cyclone dust collectors temperature It spends for 300-350 DEG C.
- 6. pyrolysis and the method for gasification coupling coproduction oil gas as claimed in claim 5, it is characterised in that：The down-flow fluidized bed using ECT pyrolysis is anti- The temperature of section is answered to be arranged to three-level step temperature from top to bottom.
- 7. a kind of be used to implement pyrolysis described in claim 1-6 and the device of gasification coupling coproduction oil gas, it is characterised in that：Including Coupled reactor and cold separation unit, the coupled reactor are by interconnected down-flow fluidized bed using ECT pyrolysis reaction section, vertical gas What body mixing section, fluidized gasification conversion zone and horizontal type reforming reaction section were formed；At the top of the down-flow fluidized bed using ECT pyrolysis reaction section The first feeder and the second feeder are respectively equipped with middle part, and first charging aperture and first are equipped on first feeder Carrier gas inlet is equipped with second charging aperture and the second carrier gas inlet on second feeder；The vertical gas mixing section point Not with the material outlet of the down-flow fluidized bed using ECT pyrolysis reaction section bottom, the top port of the fluidized gasification conversion zone, Yi Jisuo The gaseous mixture arrival end connection of horizontal type reforming reaction section is stated, in the lower part of the fluidized gasification conversion zone successively equipped with gas point The gas air compartment of fabric swatch, pre- distribution gasifying agent, gasification agent inlet is equipped on the air compartment side wall, is equipped in the air compartment bottom Ash discharging hole；The mixed gas outlet of the horizontal type reforming reaction section is connected with cold separation unit.
- 8. device as claimed in claim 7, it is characterised in that：The cold separation unit is by deduster, cooler and separation Device composition, the mixed gas outlet end of the horizontal type pipe coke tar reforming conversion zone connects successively with deduster, cooler and separator It connects.
- 9. pyrolysis and the device of gasification coupling coproduction oil gas as claimed in claim 7, it is characterised in that：First feeder and Second feeder is star-like feeder, and first carrier gas inlet is located at the lower section of first charging aperture, second carrier gas inlet Positioned at the lower section of second charging aperture.
- 10. pyrolysis and the device of gasification coupling coproduction oil gas as claimed in claim 7, it is characterised in that：The deduster is rotation Wind deduster, the cooler are jacket type cooler, and the separator is attached most importance to strength liquid/gas separator.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201711439454.9A CN108048140B (en) | 2017-12-27 | 2017-12-27 | Method and device for co-producing oil gas by pyrolysis and gasification coupling |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201711439454.9A CN108048140B (en) | 2017-12-27 | 2017-12-27 | Method and device for co-producing oil gas by pyrolysis and gasification coupling |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN108048140A true CN108048140A (en) | 2018-05-18 |
| CN108048140B CN108048140B (en) | 2020-07-07 |
Family
ID=62128207
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201711439454.9A Active CN108048140B (en) | 2017-12-27 | 2017-12-27 | Method and device for co-producing oil gas by pyrolysis and gasification coupling |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN108048140B (en) |
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108715766A (en) * | 2018-06-27 | 2018-10-30 | 北京清创晋华科技有限公司 | A kind of coal grading sub-prime for pulverized-coal fired boiler utilizes system and method |
| CN109054901A (en) * | 2018-08-01 | 2018-12-21 | 万华化学集团股份有限公司 | A kind of down-flow fluidized bed using ECT-fluidized bed tandem gasification process and device |
| CN109355073A (en) * | 2018-11-02 | 2019-02-19 | 武汉博立达农业科技发展有限公司 | Biomass and coal copyrolysis reactor |
| CN109355074A (en) * | 2018-11-02 | 2019-02-19 | 武汉博立达农业科技发展有限公司 | Biomass and coal copyrolysis reactor |
| CN113122335A (en) * | 2021-04-21 | 2021-07-16 | 新奥科技发展有限公司 | Biomass and coal co-gasification system and method |
| CN115181589A (en) * | 2022-07-06 | 2022-10-14 | 山东科技大学 | Organic solid waste hydrogen-rich catalytic pyrolysis series volatile matter reforming device and method |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE10158634A1 (en) * | 2001-11-29 | 2003-06-12 | Kordes Gmbh Forschung Und Entw | Light shredded automotive wastes disposed of by pyrolysis and gasfication in shaft with supplementary side-injectors |
| CN101955803A (en) * | 2009-07-15 | 2011-01-26 | 山东科技大学 | Low-rank coal carbonization method |
| CN102424359A (en) * | 2011-08-26 | 2012-04-25 | 北京大学深圳研究生院 | Method for preparing synthetic gas by three-phase type biomass pyrolysis-gasification-catalytic reforming |
| CN105273763A (en) * | 2014-05-27 | 2016-01-27 | 北京中矿科能煤炭地下气化技术研究中心 | Heat pipe heating type biomass and coal segmented collaborative pyrolysis system |
| CN105802646A (en) * | 2016-04-18 | 2016-07-27 | 山东科技大学 | High-sulphur coal pyrolysis device and method based on secondary catalytic tempering |
-
2017
- 2017-12-27 CN CN201711439454.9A patent/CN108048140B/en active Active
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE10158634A1 (en) * | 2001-11-29 | 2003-06-12 | Kordes Gmbh Forschung Und Entw | Light shredded automotive wastes disposed of by pyrolysis and gasfication in shaft with supplementary side-injectors |
| CN101955803A (en) * | 2009-07-15 | 2011-01-26 | 山东科技大学 | Low-rank coal carbonization method |
| CN102424359A (en) * | 2011-08-26 | 2012-04-25 | 北京大学深圳研究生院 | Method for preparing synthetic gas by three-phase type biomass pyrolysis-gasification-catalytic reforming |
| CN105273763A (en) * | 2014-05-27 | 2016-01-27 | 北京中矿科能煤炭地下气化技术研究中心 | Heat pipe heating type biomass and coal segmented collaborative pyrolysis system |
| CN105802646A (en) * | 2016-04-18 | 2016-07-27 | 山东科技大学 | High-sulphur coal pyrolysis device and method based on secondary catalytic tempering |
Cited By (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108715766A (en) * | 2018-06-27 | 2018-10-30 | 北京清创晋华科技有限公司 | A kind of coal grading sub-prime for pulverized-coal fired boiler utilizes system and method |
| CN109054901A (en) * | 2018-08-01 | 2018-12-21 | 万华化学集团股份有限公司 | A kind of down-flow fluidized bed using ECT-fluidized bed tandem gasification process and device |
| CN109054901B (en) * | 2018-08-01 | 2020-09-08 | 万华化学集团股份有限公司 | Descending bed-fluidized bed series type gasification method and device |
| CN109355073A (en) * | 2018-11-02 | 2019-02-19 | 武汉博立达农业科技发展有限公司 | Biomass and coal copyrolysis reactor |
| CN109355074A (en) * | 2018-11-02 | 2019-02-19 | 武汉博立达农业科技发展有限公司 | Biomass and coal copyrolysis reactor |
| CN109355074B (en) * | 2018-11-02 | 2023-12-01 | 武汉兰多生物科技有限公司 | Biomass and coal co-pyrolysis reactor |
| CN109355073B (en) * | 2018-11-02 | 2023-12-01 | 武汉兰多生物科技有限公司 | Biomass and coal co-pyrolysis reactor |
| CN113122335A (en) * | 2021-04-21 | 2021-07-16 | 新奥科技发展有限公司 | Biomass and coal co-gasification system and method |
| CN113122335B (en) * | 2021-04-21 | 2022-06-28 | 新奥科技发展有限公司 | Biomass and coal co-gasification system and method |
| CN115181589A (en) * | 2022-07-06 | 2022-10-14 | 山东科技大学 | Organic solid waste hydrogen-rich catalytic pyrolysis series volatile matter reforming device and method |
Also Published As
| Publication number | Publication date |
|---|---|
| CN108048140B (en) | 2020-07-07 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN108048140A (en) | A kind of method and apparatus being pyrolyzed with gasification coupling coproduction oil gas | |
| CN101245264B (en) | Single-bed self-heating type thermal decomposition gasification combustion reactor and thermal decomposition gasification combustion method | |
| CN103923705B (en) | Gasifying biomass produces the device and method of hydrogen-rich gas | |
| CN101781583B (en) | Method and device for utilizing high value through pyrolysis and gasification of coal | |
| CN102079685B (en) | Coal gasification process for methane preparation by two stage gasification stove | |
| CN104830358B (en) | A kind of biomass graded gasification produces the device and method of hydrogen-rich gas | |
| CN102977927A (en) | Apparatus for preparing synthesis gas based on dual fluidized bed biomass gasification and preparation method thereof | |
| CN109294626B (en) | Production process and device for preparing synthesis gas by biomass gasification | |
| CN108026459A (en) | Full steam gasification with carbon trapping | |
| CN104789245A (en) | Pyrolysis and gasification device and technology | |
| CN201241071Y (en) | Single-bed self-heating type thermal decomposition gasification combusting reactor | |
| CN107760377B (en) | Fluidized bed and fixed bed combined coal catalytic gasification reaction device and method thereof | |
| CN102585947A (en) | Method and device for preparing methane-containing gas by using coal | |
| CN103060012A (en) | Gasification method for classification conversion of hydrocarbon components of coal | |
| CN104974799A (en) | Method and system used for preparing high methane gas via co-gasifying of coal and biomass | |
| CN102604683A (en) | Method for co-production of synthetic gas and coal tar | |
| CN110643382A (en) | Biomass oil-gas co-production device and method based on chemical chain | |
| CN107474859A (en) | A kind of coal pyrolytic gasified technique coupling device and its method | |
| CN104531222B (en) | Pyrolysis of coal system and method using spouted bed reactor | |
| CN105087078A (en) | Indirect pyrolysis system and pyrolysis method thereof | |
| CN211111863U (en) | Biomass oil-gas co-production device based on chemical chain | |
| CN107267218A (en) | The method and system of solid fuel pyrolysis gasification | |
| CN202346964U (en) | Fluidized bed low temperature carbonization system and low temperature carbonization reactor | |
| KR20140080453A (en) | Circulating Fluidized Bed Gasifier Equipped with Heat Exchanger Therein | |
| CN207313542U (en) | A kind of coal dust gasification device for producing high heating value gas and low carbon left |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| CB03 | Change of inventor or designer information | ||
| CB03 | Change of inventor or designer information |
Inventor after: Kong Jiao Inventor after: Wang Meijun Inventor after: Yu Yanxu Inventor after: Li Ting Inventor after: Chang Liping Inventor after: Bao Weiren Inventor before: Wang Meijun Inventor before: Kong Jiao Inventor before: Yu Yanxu Inventor before: Li Ting Inventor before: Chang Liping Inventor before: Bao Weiren |
|
| GR01 | Patent grant | ||
| GR01 | Patent grant |