CN106987281A - The method of pulverized coal pyrolysis gasification integrated reactor and processing fine coal - Google Patents
The method of pulverized coal pyrolysis gasification integrated reactor and processing fine coal Download PDFInfo
- Publication number
- CN106987281A CN106987281A CN201710381212.2A CN201710381212A CN106987281A CN 106987281 A CN106987281 A CN 106987281A CN 201710381212 A CN201710381212 A CN 201710381212A CN 106987281 A CN106987281 A CN 106987281A
- Authority
- CN
- China
- Prior art keywords
- pyrolysis
- heater
- gasification
- semicoke
- chamber
- 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.)
- Pending
Links
- 238000000197 pyrolysis Methods 0.000 title claims abstract description 158
- 238000002309 gasification Methods 0.000 title claims abstract description 126
- 239000003245 coal Substances 0.000 title claims abstract description 107
- 238000000034 method Methods 0.000 title claims abstract description 27
- 230000015572 biosynthetic process Effects 0.000 claims abstract description 57
- 238000003786 synthesis reaction Methods 0.000 claims abstract description 57
- 239000003795 chemical substances by application Substances 0.000 claims abstract description 23
- 239000000446 fuel Substances 0.000 claims abstract description 6
- 238000006243 chemical reaction Methods 0.000 claims description 16
- 230000005484 gravity Effects 0.000 claims description 9
- 238000011068 loading method Methods 0.000 claims description 7
- 239000007789 gas Substances 0.000 description 70
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 7
- 238000005265 energy consumption Methods 0.000 description 7
- 239000003077 lignite Substances 0.000 description 5
- 238000003860 storage Methods 0.000 description 5
- 239000003570 air Substances 0.000 description 4
- 229910002092 carbon dioxide Inorganic materials 0.000 description 4
- 238000002485 combustion reaction Methods 0.000 description 4
- 238000009826 distribution Methods 0.000 description 4
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 3
- 239000001569 carbon dioxide Substances 0.000 description 3
- 239000000463 material Substances 0.000 description 3
- 229910052760 oxygen Inorganic materials 0.000 description 3
- 239000001301 oxygen Substances 0.000 description 3
- 238000006068 polycondensation reaction Methods 0.000 description 3
- 239000000126 substance Substances 0.000 description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 3
- 238000009825 accumulation Methods 0.000 description 2
- 238000004458 analytical method Methods 0.000 description 2
- 230000008901 benefit Effects 0.000 description 2
- 238000005336 cracking Methods 0.000 description 2
- 238000000354 decomposition reaction Methods 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 238000010438 heat treatment Methods 0.000 description 2
- 230000010354 integration Effects 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- VUZPPFZMUPKLLV-UHFFFAOYSA-N methane;hydrate Chemical compound C.O VUZPPFZMUPKLLV-UHFFFAOYSA-N 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 239000002245 particle Substances 0.000 description 2
- 238000010248 power generation Methods 0.000 description 2
- 230000008569 process Effects 0.000 description 2
- 239000004215 Carbon black (E152) Substances 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 238000004939 coking Methods 0.000 description 1
- 239000000470 constituent Substances 0.000 description 1
- 238000011109 contamination Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 239000000428 dust Substances 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 239000002360 explosive Substances 0.000 description 1
- 239000005431 greenhouse gas Substances 0.000 description 1
- 229930195733 hydrocarbon Natural products 0.000 description 1
- 150000002430 hydrocarbons Chemical class 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 230000003993 interaction Effects 0.000 description 1
- 238000002955 isolation Methods 0.000 description 1
- 238000005065 mining Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 239000005416 organic matter Substances 0.000 description 1
- 230000000149 penetrating effect Effects 0.000 description 1
- 238000010025 steaming Methods 0.000 description 1
- 229910052717 sulfur Inorganic materials 0.000 description 1
- 239000011593 sulfur Substances 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
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
- C10J3/66—Processes with decomposition of the distillation products by introducing them into the gasification zone
-
- 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
- C10B47/02—Destructive distillation of solid carbonaceous materials with indirect heating, e.g. by external combustion with stationary 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
- 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
- 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
Abstract
The invention discloses the method for pulverized coal pyrolysis gasification integrated reactor and processing fine coal.Pulverized coal pyrolysis gasification integrated reactor includes：It is pyrolyzed body of heater, pyrolysis chamber is defined in it, multiple radiant tubes are provided with pyrolysis chamber, there is fine coal entrance, the bottom of pyrolysis body of heater to have semicoke outlet on the top of pyrolysis body of heater, being pyrolyzed on body of heater has syngas outlet, and the side wall of pyrolysis body of heater has the fuel inlet and exhanst gas outlet of connection radiant tube；Gasify body of heater, and defining in it has gasification agent inlet on gasification chamber, gasification body of heater, and the top of gasification body of heater has semicoke entrance, and the bottom of gasification body of heater has lime-ash outlet, and gasification furnace body is located at the lower section of pyrolysis body of heater, and semicoke entrance is exported with semicoke and is connected.The semicoke that pulverized coal pyrolysis is obtained can be converted into using pulverized coal pyrolysis gasification integrated reactor by synthesis gas, and make full use of the sensible heat of synthesis gas, while solving the problem of semicoke is difficult by.
Description
Technical field
The present invention relates to derived energy chemical field, specifically, the present invention relates to pulverized coal pyrolysis gasification integrated reactor and
The method for handling fine coal.
Background technology
Coal is one of conventional resource that proved reserves are enriched the most in the world, and China is used as coal maximum in the world to give birth to
Production and country of consumption, energy resource structure feature are rich coal, oil-poor, few gas.In coal resources in China structure, the higher low order of fugitive constituent
Coal occupies larger ratio again, and it is about 130,000,000,000 tons that wherein lignite, which verifies reserves, accounts for the whole nation and verifies reserves
12.69% or so, the low order such as jet coal, non caking coal and weakly caking coal is grade metamorphic bituminous, accounts for the 42.46% of coal reserves.Low-order coal
It is the product at incoalation initial stage, because having, the high and low ash of moisture, low-sulfur, lower calorific value, volatile matter are high, density is small, bad adhesion
The features such as with activity by force so that its comprehensive utilization is largely limited.The main Land use systems of existing low-order coal have：Directly
Connect combustion power generation, pyrolysis upgrading, direct liquefaction, gasification and Valuable Chemicals etc..Wherein, direct combustion power generation is that it is the most normal
One of Land use systems seen, according to incompletely statistics, the low-order coal that China there are about 90% are directly used in station boiler and various industry
Boiler.And lignite is low as the direct efficiency of combustion of power fuel, greenhouse gas emissions are high, seriously polluted, and waste coal
In the hydrocarbon rich resource that contains.
Widely used simultaneously as modernization coal mining is polytechnic so that the ratio of lump coal declines, the rise of fine coal yield (reaches
More than 60%).Inflammable and explosive during accumulation because of the easy airborne dust of fine coal, comprehensive utilization difficulty is big, causes its unmarketable and largely accumulates
Pressure.The pyrolysis of coal is one of important channel for efficiently utilizing of low-order coal cleaning, is coal under isolation air or inert atmosphere conditions
During continuous heating to higher temperature, the change of a series of physical of generation and chemically react, including in coal organic matter cracking, cracking
The volatilization of light components in product, cracks the polycondensation of residue, decomposition of the volatile matter product during effusion, chemical combination, polycondensation
The further decomposition of product, then the process such as polycondensation.It will pass through in coal gasification, liquefaction, coking and combustion process or occur heat
Solution preocess.
However, the means of existing processing fine coal still have much room for improvement.
The content of the invention
It is contemplated that at least solving one of technical problem in correlation technique to a certain extent.Therefore, the present invention
One purpose is the method for proposing pulverized coal pyrolysis gasification integrated reactor and processing fine coal.Using pulverized coal pyrolysis gasification one
The semicoke that pulverized coal pyrolysis is obtained can be converted into synthesis gas by body reactor, and make full use of the sensible heat of synthesis gas, together
When solve semicoke the problem of be difficult by.
In the first aspect of the present invention, the present invention proposes a kind of pulverized coal pyrolysis gasification integrated reactor.According to this hair
Bright embodiment, the coal pyrolytic gasified integrated reactor includes：It is pyrolyzed in body of heater, the pyrolysis oven body and defines pyrolysis chamber
Multiple radiant tubes are provided with room, the pyrolysis chamber, the top of the pyrolysis body of heater has fine coal entrance, the pyrolysis body of heater
Bottom have there is syngas outlet on semicoke outlet, the pyrolysis body of heater, the side wall of the pyrolysis body of heater has connection institute
State the fuel inlet and exhanst gas outlet of radiant tube；Gasify body of heater, and gasification chamber, the gasification furnace are defined in the gasification furnace body
There is gasification agent inlet, the top of the gasification body of heater has semicoke entrance, and the bottom of the gasification body of heater has lime-ash on body
Outlet, the gasification furnace body is located at the lower section of the pyrolysis body of heater, and the semicoke entrance is connected with semicoke outlet.
Pulverized coal pyrolysis according to embodiments of the present invention gasifies integrated reactor by the way that fine coal to be pyrolyzed is supplied to pyrolysis
It is pyrolyzed in the pyrolysis chamber of body of heater, obtains semicoke, semicoke is fallen under gravity into the gasification chamber of gasification body of heater,
And gasification reaction occurs in the presence of gasifying agent, obtain synthesis gas；And then synthesis gas can be returned directly in pyrolysis chamber, profit
Heat is provided for the pyrolysis of fine coal with the sensible heat of synthesis gas, the syngas outlet discharge on pyrolysis body of heater, collects storage afterwards.
Thus, synthesis gas is converted into by the semicoke for obtaining pulverized coal pyrolysis using pulverized coal pyrolysis gasification integrated reactor,
And make full use of the sensible heat of synthesis gas to carry out pulverized coal pyrolysis, so as to significantly improve heat utilization efficiency, and synthesis gas product is obtained, solved
The problem of certainly semicoke is difficult by.
In addition, pulverized coal pyrolysis gasification integrated reactor according to the above embodiment of the present invention can also have following add
Technical characteristic：
In some embodiments of the invention, the width of the pyrolysis body of heater is 2~6m, and the height of the pyrolysis body of heater is
9~60m；The width of the gasification body of heater is 2~6m, and the height of the gasification body of heater is 20~55m.
In some embodiments of the invention, longitudinal center's overlapping of axles of the pyrolysis body of heater and the gasification body of heater.
In some embodiments of the invention, in many on longitudinal direction of the multiple radiant tube in the pyrolysis chamber
Layer arrangement, and interlamellar spacing is 230~770mm between adjacent two layers, in every layer the spacing of two neighboring radiant tube for 220~
730mm。
In some embodiments of the invention, the gasification agent inlet is arranged on the bottom of gasification body of heater, the synthesis gas
Outlet is arranged on the top of the pyrolysis body of heater.
In some embodiments of the invention, the pulverized coal pyrolysis gasification integrated reactor further comprises：Charging leakage
Bucket；And feed auger, the feed auger is connected with the loading hopper and the fine coal entrance respectively.
In the second aspect of the present invention, the present invention proposes a kind of pulverized coal pyrolysis gasification integration of use above-described embodiment
The method of reactor for treatment fine coal.Embodiments in accordance with the present invention, this method includes：Fine coal is delivered in pyrolysis oven body, and
It is pyrolyzed in pyrolysis chamber, to obtain semicoke；The semicoke is set to fall under gravity into gasification body of heater, and in gasification
Occurs gasification reaction in chamber in the presence of gasifying agent, to obtain synthesis gas；The synthesis gas is set to be entered by the gasification chamber
Enter the pyrolysis chamber and provide discharge after heat for the pyrolysis.
Thus, the method for processing fine coal according to embodiments of the present invention is by the way that fine coal to be pyrolyzed is supplied to pyrolysis body of heater
It is pyrolyzed in pyrolysis chamber, obtains semicoke, semicoke is fallen under gravity into the gasification chamber of gasification body of heater, and in gas
Gasification reaction occurs in the presence of agent, synthesis gas is obtained；And then synthesis gas can be returned directly in pyrolysis chamber, utilize synthesis
The sensible heat of gas provides heat for the pyrolysis of fine coal, and the syngas outlet discharge on pyrolysis body of heater, collects storage afterwards.Thus,
This method is converted into synthesis gas by the semicoke for obtaining pulverized coal pyrolysis, and makes full use of the sensible heat of synthesis gas to carry out fine coal
Pyrolysis, so as to significantly improve heat utilization efficiency, and obtains synthesis gas product, solves the problem of semicoke is difficult by.
In addition, the method for processing fine coal according to the above embodiment of the present invention can also have technology additional as follows special
Levy：
In some embodiments of the invention, the average grain diameter of the fine coal is not more than 10mm.Thus, it is possible to further carry
The efficiency of height pyrolysis.
In some embodiments of the invention, the temperature of the pyrolysis is 550~900 DEG C,.Thus, it is possible to further carry
The efficiency of height pyrolysis.
In some embodiments of the invention, the temperature of the synthesis gas is 500~900 DEG C.Thus, it is possible to described in
The sensible heat of synthesis gas fully provides heat for pyrolysis, so as to further reduce the energy consumption of technique.
In some embodiments of the invention, the temperature of the gasification reaction is 1100~1400 DEG C.Thus, it is possible to enter one
Step improves the efficiency of gasification reaction.
The additional aspect and advantage of the present invention will be set forth in part in the description, and will partly become from the following description
Obtain substantially, or recognized by the practice of the present invention.
Brief description of the drawings
The above-mentioned and/or additional aspect and advantage of the present invention will become from description of the accompanying drawings below to embodiment is combined
Substantially and be readily appreciated that, wherein：
Fig. 1 is pulverized coal pyrolysis gasification integrated reactor structural representation according to an embodiment of the invention；
Fig. 2 is according to the pulverized coal pyrolysis of further embodiment of the present invention gasification integrated reactor structural representation；
Fig. 3 is the method flow schematic diagram of processing fine coal according to an embodiment of the invention.
Embodiment
Embodiments of the invention are described below in detail, the example of the embodiment is shown in the drawings, wherein from beginning to end
Same or similar label represents same or similar element or the element with same or like function.Below with reference to attached
The embodiment of figure description is exemplary, it is intended to for explaining the present invention, and be not considered as limiting the invention.
In the description of the invention, it is to be understood that term " " center ", " longitudinal direction ", " transverse direction ", " length ", " width ",
" thickness ", " on ", " under ", "front", "rear", "left", "right", " vertical ", " level ", " top ", " bottom ", " interior ", " outer ", " axle
To ", " radial direction ", the orientation of the instruction such as " circumference " or position relationship be based on orientation shown in the drawings or position relationship, be only for
It is easy to the description present invention and simplifies description, rather than indicates or imply that signified device or element there must be specific side
Position, with specific azimuth configuration and operation, therefore be not considered as limiting the invention.
In the description of the invention, " multiple " are meant that at least two, such as two, three etc., unless otherwise clear and definite
It is specific to limit.
In the present invention, unless otherwise clearly defined and limited, term " connected ", " connection " etc. should be interpreted broadly,
For example, it may be fixedly connected or be detachably connected, or integrally；Can mechanically connect or be electrically connected
Connect；Can be joined directly together, can also be indirectly connected to by intermediary, can be two element internals connection or two members
The interaction relationship of part, unless otherwise clear and definite restriction.For the ordinary skill in the art, can be according to specific
Situation understands the concrete meaning of above-mentioned term in the present invention.
In the present invention, unless otherwise clearly defined and limited, fisrt feature can be with "above" or "below" second feature
It is that the first and second features are directly contacted, or the first and second features pass through intermediary mediate contact.Moreover, fisrt feature exists
Second feature " on ", " top " and " above " but fisrt feature are directly over second feature or oblique upper, or be merely representative of
Fisrt feature level height is higher than second feature.Fisrt feature second feature " under ", " lower section " and " below " can be
One feature is immediately below second feature or obliquely downward, or is merely representative of fisrt feature level height less than second feature.
In the first aspect of the present invention, the present invention proposes a kind of pulverized coal pyrolysis gasification integrated reactor.According to this hair
Bright embodiment, with reference to Fig. 1~2, the coal pyrolytic gasified integrated reactor includes：It is pyrolyzed body of heater 100 and gasification body of heater 200.
Wherein, defined in pyrolysis body of heater 100 in pyrolysis chamber 110, pyrolysis chamber 110 and be provided with multiple radiant tubes 120, be pyrolyzed body of heater
There is fine coal entrance 101, the bottom of pyrolysis body of heater 200 there is semicoke to export on 102, pyrolysis body of heater 100 on 100 top has conjunction
Into gas outlet 103, the side wall of pyrolysis body of heater 100 has the fuel inlet 104 and exhanst gas outlet 105 of connection radiant tube 120；Gasification
Being defined in body of heater 200 has gasification agent inlet 201 on gasification chamber 210, gasification body of heater 200, the top tool of gasification body of heater 200
There is semicoke entrance 202, there is lime-ash to export 203 for the bottom of gasification body of heater 200, and gasification body of heater 200 is located under pyrolysis body of heater 100
Side, and semicoke entrance 202 and semicoke export 102 and be connected.
Retouched in detail below with reference to Fig. 1~2 pair pulverized coal pyrolysis gasification integrated reactor according to embodiments of the present invention
State：
Define and be provided with pyrolysis chamber 110, pyrolysis chamber 110 in embodiments in accordance with the present invention, pyrolysis body of heater 100
There is fine coal entrance 101, the bottom of pyrolysis body of heater 200 to have semicoke outlet on multiple radiant tubes 120, the top of pyrolysis body of heater 100
102, being pyrolyzed on body of heater 100 has syngas outlet 103, and the fuel that the side wall of pyrolysis body of heater 100 has connection radiant tube 120 enters
Mouth 104 and exhanst gas outlet 105, pyrolysis body of heater 100 are suitable to fine coal to be pyrolyzed being pyrolyzed in pyrolysis chamber 110, so as to
To semicoke.
Embodiments in accordance with the present invention, the width for being pyrolyzed body of heater can be 2~6m, highly can be 9~60m.
Embodiments in accordance with the present invention, the high-temperature synthesis gas that being pyrolyzed can both have been obtained by follow-up char Gasification provides heat
Amount, can also provide heat by radiant tube 120.According to a particular embodiment of the invention, multiple radiant tubes 120 can be in pyrolysis
Be on longitudinal direction in chamber 110 between multi-tier arrangement, and adjacent two layers interlamellar spacing can be 230~770mm, phase in every layer
The spacing of adjacent two radiant tubes can be 220~730mm.Thus, it is possible to further improve heat distribution in pyrolysis chamber 110
The uniformity.
Embodiments in accordance with the present invention, the particle diameter of fine coal is not particularly restricted, and those skilled in the art can be according to reality
Border needs to be selected, according to a particular embodiment of the invention, and the average grain diameter of fine coal can be no more than 10mm, thus, can
Efficiency is pyrolyzed with further improve.
Embodiments in accordance with the present invention, the temperature of pyrolysis is not particularly restricted, and those skilled in the art can be according to reality
Border needs to be selected, according to a particular embodiment of the invention, and the temperature of pyrolysis can be 550~900 DEG C, thus, it is possible to enter
One step improves pyrolysis efficiency.
According to the specific embodiment of the present invention, above-mentioned radiant tube can for the specification of DN200~390 round tube, by
This, can further improve the uniformity of heat distribution in pyrolysis chamber.
Being defined in embodiments in accordance with the present invention, gasification body of heater 200 on gasification chamber 210, gasification body of heater 200 has gas
Agent entrance 201, the top of gasification body of heater 200 has semicoke entrance 202, and the bottom of gasification body of heater 200 has lime-ash outlet
203, gasification body of heater 200 is located at the lower section of pyrolysis body of heater 100, and semicoke entrance 202 is connected with semicoke outlet 102, and gasify body of heater
200 are suitable to semicoke carrying out gasification reaction in gasification chamber 210, to obtain synthesis gas.Specifically, in pyrolysis chamber 110
The semicoke that pulverized coal pyrolysis is obtained can be fallen under gravity into the gasification chamber 210 of gasification body of heater 200, and char Gasification is obtained
To high-temperature synthesis gas can directly return in pyrolysis chamber 110, and provide heat for pulverized coal pyrolysis using its sensible heat, so as to
To significantly reduce the energy consumption of radiant tube, and the discharge of dusty gas is reduced, follow-up synthesis gas can be from the conjunction on pyrolysis body of heater 100
Discharged into gas outlet 103, and be collected storage.
Embodiments in accordance with the present invention, the width for the body of heater 200 that gasifies can be 2~6m, and the height for the body of heater 200 that gasifies can be with
For 20~55m.
According to a particular embodiment of the invention, longitudinal center's overlapping of axles of pyrolysis body of heater 100 and gasification body of heater 200.
According to the specific embodiment of the present invention, semicoke entrance 202 can be located at the underface that semicoke exports 102, by
This, can effectively further be such that the semicoke obtained in pyrolysis chamber 110 falls directly into gasification chamber 210.
According to a particular embodiment of the invention, gasification agent inlet 201 is arranged on the bottom of gasification body of heater 200, and synthesis gas goes out
Mouth 103 is arranged on the top of pyrolysis body of heater 100, thus, it is possible to further improve gasification chamber 210 and be pyrolyzed in chamber 110
Heat and mass efficiency, improves heat utilization efficiency.It should be noted that term " bottom " refers to the lower section in the middle part of gasification body of heater.
According to a particular embodiment of the invention, the temperature of gasification reaction can be 1100~1400 DEG C.Thus, it is possible to enter one
Step improves the efficiency of gasification reaction.
According to a particular embodiment of the invention, the temperature of synthesis gas is 500~900 DEG C.Thus, it is possible to effectively utilize synthesis
The sensible heat of gas fully provides heat for pyrolysis, so as to further reduce the energy consumption of technique.
According to the specific embodiment of the present invention, gasifying agent can include selection oxygen, air, carbon dioxide and water and steam
One or more in gas, thus, it is possible to further improve the yield of synthesis gas.
With reference to Fig. 2, above-mentioned pulverized coal pyrolysis gasification integrated reactor can further include：Loading hopper 300 and enter
Expect spiral 400.
Embodiments in accordance with the present invention, feed auger 400 is connected with loading hopper 300 and fine coal entrance 101 respectively, by
This, can add fine coal to be pyrolyzed into loading hopper 300, and be extremely pyrolyzed by the supply of feed auger 400 in body of heater 100,
So as to further improve production efficiency.
Thus, pulverized coal pyrolysis gasification integrated reactor according to embodiments of the present invention by will fine coal be pyrolyzed supply to
It is pyrolyzed in the pyrolysis chamber for being pyrolyzed body of heater, obtains semicoke, semicoke is fallen under gravity into the gasification chamber of gasification body of heater
Interior, and occur gasification reaction in the presence of gasifying agent, obtain synthesis gas；And then synthesis gas can directly return to pyrolysis chamber
In, heat is provided for the pyrolysis of fine coal using the sensible heat of synthesis gas, so as to significantly reduce the energy consumption and contamination gas of radiant tube
Body is discharged, and the syngas outlet discharge on pyrolysis body of heater, is collected storage afterwards.Thus, gasified using the pulverized coal pyrolysis
Integrated reactor is converted into synthesis gas by the semicoke for obtaining pulverized coal pyrolysis, and makes full use of the sensible heat of synthesis gas to enter
Row pulverized coal pyrolysis, so as to significantly improve heat utilization efficiency, and obtains synthesis gas product, solves the problem of semicoke is difficult by.
In the second aspect of the present invention, the present invention proposes a kind of pulverized coal pyrolysis gasification integration of use above-described embodiment
The method of reactor for treatment fine coal.Embodiments in accordance with the present invention, this method includes：Fine coal is delivered in pyrolysis oven body, and
It is pyrolyzed in pyrolysis chamber, to obtain semicoke；Semicoke is set to fall under gravity into gasification body of heater, and in gasification chamber
Occurs gasification reaction in the presence of interior gasifying agent, to obtain synthesis gas；Make synthesis gas by gasification chamber enter pyrolysis chamber be
Pyrolysis is provided and discharged after heat.
The method of processing fine coal according to embodiments of the present invention is described in detail below with reference to Fig. 3.According to the present invention
Embodiment, this method includes：
S100：Pyrolysis
In the step, fine coal is delivered in pyrolysis oven body, and is pyrolyzed in pyrolysis chamber, to obtain semicoke.
Embodiments in accordance with the present invention, the width for being pyrolyzed body of heater can be 2~6m, highly can be 9~60m.
Embodiments in accordance with the present invention, the high-temperature synthesis gas that being pyrolyzed can both have been obtained by follow-up char Gasification provides heat
Amount, can also provide heat by radiant tube.According to a particular embodiment of the invention, multiple radiant tubes can be in pyrolysis chamber
Longitudinal direction on be between multi-tier arrangement, and adjacent two layers interlamellar spacing can be 230~770mm, two neighboring spoke in every layer
The spacing for penetrating pipe can be 220~730mm.Thus, it is possible to further improve the uniformity of heat distribution in pyrolysis chamber.
Embodiments in accordance with the present invention, the particle diameter of fine coal is not particularly restricted, and those skilled in the art can be according to reality
Border needs to be selected, according to a particular embodiment of the invention, and the average grain diameter of fine coal can be no more than 10mm, thus, can
Efficiency is pyrolyzed with further improve.
Embodiments in accordance with the present invention, the temperature of pyrolysis is not particularly restricted, and those skilled in the art can be according to reality
Border needs to be selected, according to a particular embodiment of the invention, and the temperature of pyrolysis can be 550~900 DEG C, thus, it is possible to enter
One step improves pyrolysis efficiency.
According to the specific embodiment of the present invention, above-mentioned radiant tube can for the specification of DN200~390 round tube, by
This, can further improve the uniformity of heat distribution in pyrolysis chamber.
S200：Gasification
In the step, semicoke is set to fall under gravity into gasification body of heater, and in gasification chamber in the presence of gasifying agent
Generation gasification reaction, to obtain synthesis gas.
Embodiments in accordance with the present invention, the width for the body of heater that gasifies can be 2~6m, the height of the body of heater that gasifies can for 20~
55m。
According to a particular embodiment of the invention, longitudinal center's overlapping of axles of pyrolysis body of heater and gasification body of heater.
According to the specific embodiment of the present invention, semicoke entrance can be located at the underface that semicoke is exported, thus, it is possible to
The semicoke obtained in pyrolysis chamber is effectively further set to fall directly into gasification chamber.
According to a particular embodiment of the invention, gasification agent inlet is arranged on the bottom of gasification body of heater, and syngas outlet is set
On the top of pyrolysis body of heater, thus, it is possible to further improve the heat and mass efficiency in gasification chamber and pyrolysis chamber, heat is improved
Utilization rate.It should be noted that term " bottom " refers to the lower section in the middle part of gasification body of heater.
According to a particular embodiment of the invention, the temperature of gasification reaction can be 1100~1400 DEG C.Thus, it is possible to enter one
Step improves the efficiency of gasification reaction.
According to a particular embodiment of the invention, the temperature of synthesis gas is 500~900 DEG C.Thus, it is possible to effectively utilize synthesis
The sensible heat of gas fully provides heat for pyrolysis, so as to further reduce the energy consumption of technique.
According to the specific embodiment of the present invention, gasifying agent can include selection oxygen, air, carbon dioxide and water and steam
One or more in gas, thus, it is possible to further improve the yield of synthesis gas.
S300：Collect synthesis gas
Embodiments in accordance with the present invention, are provided after heat by making synthesis gas enter pyrolysis chamber by gasification chamber for pyrolysis
Discharge, can significantly reduce the energy consumption of radiant tube, and reduce the discharge of dusty gas.
Thus, the method for processing fine coal according to embodiments of the present invention is by the way that fine coal to be pyrolyzed is supplied to pyrolysis body of heater
It is pyrolyzed in pyrolysis chamber, obtains semicoke, semicoke is fallen under gravity into the gasification chamber of gasification body of heater, and in gas
Gasification reaction occurs in the presence of agent, synthesis gas is obtained；And then synthesis gas can be returned directly in pyrolysis chamber, utilize synthesis
The sensible heat of gas provides heat for the pyrolysis of fine coal, so as to significantly reduce energy consumption and the dusty gas discharge of radiant tube, afterwards
Syngas outlet discharge on pyrolysis body of heater, is collected storage.Thus, this method passes through the semicoke that obtains pulverized coal pyrolysis
Synthesis gas is converted into, and makes full use of the sensible heat of synthesis gas to carry out pulverized coal pyrolysis, so that heat utilization efficiency is significantly improved, and
Synthesis gas product is obtained, the problem of semicoke is difficult by is solved.
Below with reference to specific embodiment, present invention is described, it is necessary to which explanation, these embodiments are only description
Property, without limiting the present invention in any way.
Embodiment
Inner Mongol lignite of the average grain diameter less than 10mm will be crushed in loading hopper through feed auger feeding pyrolysis chamber,
It is pyrolyzed chamber to heat by the synthesis gas from gasification chamber, temperature control is at 900 DEG C, during shortage of heat in pyrolysis chamber
Heat accumulation type radiant tube additional heat, while controlling tube wall temperature by gas control valve, material stops from top to bottom in the reactor
Stay 0.1 second~10 minutes, and be heated to 900 DEG C, complete pyrolytic process, be pyrolyzed the semicoke produced and fall into gasification chamber through semicoke outlet
In room, gasifying agent is delivered in gasification chamber by gasification agent inlet, and gasifying agent can be oxygen, air, carbon dioxide, water steaming
Gas etc., the temperature of gasification reaction is 1200 DEG C, and semicoke gasifies in the presence of gasifying agent generates synthesis gas, and synthesis gas returns to pyrolysis
Chamber is as heating source, and the high-temperature ash produced that gasifies passes through lime-ash outlet discharge gasification chamber.Wherein, the work of pending lignite
Industry analysis is as shown in table 1, and the composition of synthesis gas is as shown in table 2.
The pending lignite Industrial Analysis/wt% of table 1
| Mad | Vad | Aad | Fcad |
| 13.29 | 32.21 | 15.82 | 38.68 |
Table is 2-in-1 into gas composition/v%
| CH4 | H2 | CO | CO2 | Other |
| 7.8 | 42.1 | 39.5 | 10.02 | 5.98 |
In the description of this specification, reference term " one embodiment ", " some embodiments ", " example ", " specifically show
The description of example " or " some examples " etc. means to combine specific features, structure, material or the spy that the embodiment or example are described
Point is contained at least one embodiment of the present invention or example.In this manual, to the schematic representation of above-mentioned term not
Identical embodiment or example must be directed to.Moreover, specific features, structure, material or the feature of description can be with office
Combined in an appropriate manner in one or more embodiments or example.In addition, in the case of not conflicting, the skill of this area
Art personnel can be tied the not be the same as Example or the feature of example and non-be the same as Example or example described in this specification
Close and combine.
Although embodiments of the invention have been shown and described above, it is to be understood that above-described embodiment is example
Property, it is impossible to limitation of the present invention is interpreted as, one of ordinary skill in the art within the scope of the invention can be to above-mentioned
Embodiment is changed, changed, replacing and modification.
Claims (10)
- The integrated reactor 1. a kind of pulverized coal pyrolysis gasifies, it is characterised in that including：It is pyrolyzed to define in pyrolysis chamber, the pyrolysis chamber in body of heater, the pyrolysis oven body and is provided with multiple radiant tubes, it is described There is fine coal entrance, the bottom of the pyrolysis body of heater, which to have on semicoke outlet, the pyrolysis body of heater, on the top of pyrolysis body of heater has Syngas outlet, the side wall of the pyrolysis body of heater has the fuel inlet and exhanst gas outlet that connect the radiant tube；Gasify body of heater, and being defined in the gasification furnace body has gasification agent inlet, the gas on gasification chamber, the gasification body of heater Changing the top of body of heater has semicoke entrance, and the bottom of the gasification body of heater has lime-ash outlet, and the gasification furnace body is located at described The lower section of body of heater is pyrolyzed, and the semicoke entrance is connected with semicoke outlet.
- The integrated reactor 2. pulverized coal pyrolysis according to claim 1 gasifies, it is characterised in that the width of the pyrolysis body of heater Spend for 2~6m, the height of the pyrolysis body of heater is 9~60m；The width of the gasification body of heater is 2~6m, the gasification body of heater Highly it is 20~55m.
- The integrated reactor 3. pulverized coal pyrolysis according to claim 1 gasifies, it is characterised in that the pyrolysis body of heater and institute State longitudinal center's overlapping of axles of gasification body of heater.
- The integrated reactor 4. pulverized coal pyrolysis according to claim 1 gasifies, it is characterised in that the multiple radiant tube exists Be on longitudinal direction in the pyrolysis chamber between multi-tier arrangement, and adjacent two layers interlamellar spacing be 230~770mm, in every layer The spacing of two neighboring radiant tube is 220~730mm.
- The integrated reactor 5. pulverized coal pyrolysis according to claim 1 gasifies, it is characterised in that the gasification agent inlet is set Put in the bottom of gasification body of heater, the syngas outlet is arranged on the top of the pyrolysis body of heater.
- The integrated reactor 6. pulverized coal pyrolysis according to claim 1 gasifies, it is characterised in that further comprise：Loading hopper；AndFeed auger, the feed auger is connected with the loading hopper and the fine coal entrance respectively.
- 7. the method that a kind of any one of use claim 1~6 pulverized coal pyrolysis gasification integrated reactor handles fine coal, bag Include：Fine coal is delivered in pyrolysis oven body, and is pyrolyzed in pyrolysis chamber, to obtain semicoke；The semicoke is fallen under gravity into gasification body of heater, and gasified reverse occurs in gasification chamber in the presence of gasifying agent Should, to obtain synthesis gas；Make the synthesis gas be provided for the pyrolysis into the pyrolysis chamber by the gasification chamber to discharge after heat.
- 8. method according to claim 7, it is characterised in that the average grain diameter of the fine coal is not more than 10mm.
- 9. method according to claim 7, it is characterised in that the temperature of the pyrolysis is 550~900 DEG C, the synthesis The temperature of gas is 500~900 DEG C.
- 10. method according to claim 7, it is characterised in that the temperature of the gasification reaction is 1100~1400 DEG C.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201710381212.2A CN106987281A (en) | 2017-05-25 | 2017-05-25 | The method of pulverized coal pyrolysis gasification integrated reactor and processing fine coal |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201710381212.2A CN106987281A (en) | 2017-05-25 | 2017-05-25 | The method of pulverized coal pyrolysis gasification integrated reactor and processing fine coal |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN106987281A true CN106987281A (en) | 2017-07-28 |
Family
ID=59420822
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201710381212.2A Pending CN106987281A (en) | 2017-05-25 | 2017-05-25 | The method of pulverized coal pyrolysis gasification integrated reactor and processing fine coal |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN106987281A (en) |
Cited By (13)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107345166A (en) * | 2017-08-31 | 2017-11-14 | 北京神雾电力科技有限公司 | Pyrolytic gasification reactor |
| CN107446629A (en) * | 2017-08-31 | 2017-12-08 | 北京神雾电力科技有限公司 | The system and method for handling low-order coal |
| CN107474879A (en) * | 2017-09-07 | 2017-12-15 | 北京神雾电力科技有限公司 | For fine coal fast pyrogenation and the system and method for gasification |
| CN107541300A (en) * | 2017-10-20 | 2018-01-05 | 北京神雾电力科技有限公司 | A kind of coal grading conversion system and coal grading method for transformation |
| CN107723031A (en) * | 2017-11-23 | 2018-02-23 | 航天长征化学工程股份有限公司 | High-pressure gasification and pyrolysis integrated device for pulverized coal |
| CN107916142A (en) * | 2017-12-28 | 2018-04-17 | 北京神雾电力科技有限公司 | Biomass pyrogenation gasification system and pyrolysis gasification method |
| CN107936992A (en) * | 2017-12-22 | 2018-04-20 | 北京神雾电力科技有限公司 | A kind of high temperature three-segment formula waste heat recovery pyrolysis reactor |
| CN107987890A (en) * | 2017-12-28 | 2018-05-04 | 北京神雾电力科技有限公司 | Organic sludge pyrolysis gasification system and pyrolysis gasification method |
| CN108034458A (en) * | 2017-12-28 | 2018-05-15 | 北京神雾电力科技有限公司 | Low-order coal pyrolysis gasification system and pyrolysis gasification method |
| CN110283628A (en) * | 2019-07-10 | 2019-09-27 | 北京石油化工工程研究院 | A kind of cracking gasification reactor |
| CN110591745A (en) * | 2019-10-14 | 2019-12-20 | 西北大学 | Pyrolysis-gasification integrated device and process |
| CN112358893A (en) * | 2020-11-02 | 2021-02-12 | 浙江百能科技有限公司 | Process for coproducing oil gas by coal pyrolysis and gasification |
| CN115125044A (en) * | 2022-08-03 | 2022-09-30 | 陕西延长石油（集团）有限责任公司 | Method for coproducing electricity by using oil products prepared from low-rank coal and natural gas |
Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN202297531U (en) * | 2011-10-25 | 2012-07-04 | 陕西华祥能源科技集团有限公司 | Moving bed pulverized coal pyrolysis and fluidized bed coke breeze gasification coupling device |
| CN102604683A (en) * | 2011-12-20 | 2012-07-25 | 新奥科技发展有限公司 | Method for co-production of synthetic gas and coal tar |
| CN103980948A (en) * | 2014-06-11 | 2014-08-13 | 华东理工大学 | Coal powder pyrolysis and gasification method |
| CN105087078A (en) * | 2015-09-08 | 2015-11-25 | 航天长征化学工程股份有限公司 | Indirect pyrolysis system and pyrolysis method thereof |
| CN105441138A (en) * | 2014-08-29 | 2016-03-30 | 中国石油化工股份有限公司 | Coal pyrolysis and gasification coproduction method |
| 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 |
| CN106281383A (en) * | 2016-09-28 | 2017-01-04 | 尚柳彤 | Fine coal fast pyrogenation and char Gasification combined unit and process thereof |
-
2017
- 2017-05-25 CN CN201710381212.2A patent/CN106987281A/en active Pending
Patent Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN202297531U (en) * | 2011-10-25 | 2012-07-04 | 陕西华祥能源科技集团有限公司 | Moving bed pulverized coal pyrolysis and fluidized bed coke breeze gasification coupling device |
| CN102604683A (en) * | 2011-12-20 | 2012-07-25 | 新奥科技发展有限公司 | Method for co-production of synthetic gas and coal tar |
| CN103980948A (en) * | 2014-06-11 | 2014-08-13 | 华东理工大学 | Coal powder pyrolysis and gasification method |
| CN105441138A (en) * | 2014-08-29 | 2016-03-30 | 中国石油化工股份有限公司 | Coal pyrolysis and gasification coproduction method |
| CN105087078A (en) * | 2015-09-08 | 2015-11-25 | 航天长征化学工程股份有限公司 | Indirect pyrolysis system and pyrolysis method thereof |
| 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 |
| CN106281383A (en) * | 2016-09-28 | 2017-01-04 | 尚柳彤 | Fine coal fast pyrogenation and char Gasification combined unit and process thereof |
Cited By (13)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107345166A (en) * | 2017-08-31 | 2017-11-14 | 北京神雾电力科技有限公司 | Pyrolytic gasification reactor |
| CN107446629A (en) * | 2017-08-31 | 2017-12-08 | 北京神雾电力科技有限公司 | The system and method for handling low-order coal |
| CN107474879A (en) * | 2017-09-07 | 2017-12-15 | 北京神雾电力科技有限公司 | For fine coal fast pyrogenation and the system and method for gasification |
| CN107541300A (en) * | 2017-10-20 | 2018-01-05 | 北京神雾电力科技有限公司 | A kind of coal grading conversion system and coal grading method for transformation |
| CN107723031A (en) * | 2017-11-23 | 2018-02-23 | 航天长征化学工程股份有限公司 | High-pressure gasification and pyrolysis integrated device for pulverized coal |
| CN107936992A (en) * | 2017-12-22 | 2018-04-20 | 北京神雾电力科技有限公司 | A kind of high temperature three-segment formula waste heat recovery pyrolysis reactor |
| CN107916142A (en) * | 2017-12-28 | 2018-04-17 | 北京神雾电力科技有限公司 | Biomass pyrogenation gasification system and pyrolysis gasification method |
| CN107987890A (en) * | 2017-12-28 | 2018-05-04 | 北京神雾电力科技有限公司 | Organic sludge pyrolysis gasification system and pyrolysis gasification method |
| CN108034458A (en) * | 2017-12-28 | 2018-05-15 | 北京神雾电力科技有限公司 | Low-order coal pyrolysis gasification system and pyrolysis gasification method |
| CN110283628A (en) * | 2019-07-10 | 2019-09-27 | 北京石油化工工程研究院 | A kind of cracking gasification reactor |
| CN110591745A (en) * | 2019-10-14 | 2019-12-20 | 西北大学 | Pyrolysis-gasification integrated device and process |
| CN112358893A (en) * | 2020-11-02 | 2021-02-12 | 浙江百能科技有限公司 | Process for coproducing oil gas by coal pyrolysis and gasification |
| CN115125044A (en) * | 2022-08-03 | 2022-09-30 | 陕西延长石油（集团）有限责任公司 | Method for coproducing electricity by using oil products prepared from low-rank coal and natural gas |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN106987281A (en) | The method of pulverized coal pyrolysis gasification integrated reactor and processing fine coal | |
| EP3026098B1 (en) | Method for preparing hydrogen-rich gas by gasification of solid organic substance and steam | |
| CN102465043B (en) | Multi-section fractional pyrolysis gasification device and method for solid fuel | |
| CN104804775B (en) | The method and system of domestic garbage pyrolysis gasification production combustible gas | |
| CN101942313B (en) | Huadian type process and device for dry distillation of oil shale | |
| CN101649214B (en) | Externally-fired oil shale distillation process and device | |
| RU2544669C1 (en) | Method for processing combustible carbon- and/or hydrocarbon-containing products, and reactor for implementing it | |
| JP6899102B2 (en) | Biomass gasifier | |
| CN108467736A (en) | A kind of horizontal moving bed biomass pyrogenation gasification equipment of multistage subsection formula | |
| CN105885950B (en) | A kind of three combination pyrolytic gasifications of solid waste and coke tar cracking integral system | |
| CN101250419A (en) | Coal gas internal heating low-temperature cracking process | |
| JP6412261B2 (en) | Biomass gasifier | |
| CN100543116C (en) | The oxygen deprivation fluidized bed combustion downdraft gasification process and the device that prepare no tar products gas | |
| CN101993703A (en) | Oil shale oven and carbonification process | |
| CN207904190U (en) | A kind of two reactor system preparing hydrogen-rich synthetic gas for gasification of biomass | |
| CN206887041U (en) | Pulverized coal pyrolysis gasification integrated reactor | |
| CN103215081B (en) | Comprehensive high-efficiency carbon gasification pyrolysis equipment for biomass compact forming grains | |
| CN110747010A (en) | Self-produced gas combustion linkage type pyrolysis gasification device | |
| CN206887025U (en) | Fine coal dry thermal cracking integrated reactor | |
| CN100358974C (en) | Biomass moving bed gasification furnace using heat pipe supplying heat | |
| CN103189473A (en) | Method and equipment for producing coke during indirectly heated gasification | |
| RU144623U1 (en) | REACTOR FOR THE PROCESSING OF COMBUSTIBLE CARBON AND / OR HYDROCARBON-CONTAINING PRODUCTS | |
| CN106995710A (en) | The method of fine coal dry thermal cracking integrated reactor and processing fine coal | |
| CN207581747U (en) | Catalytic gasification rough coal gas processing system | |
| CN208121013U (en) | A kind of horizontal moving bed biomass pyrogenation gasification equipment of multistage subsection formula |
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 | ||
| TA01 | Transfer of patent application right |
Effective date of registration: 20200214 Address after: No. 1391, south side, 10th floor, new material venture building, No. 7, Fenghui Middle Road, Haidian District, Beijing Applicant after: Beijing Jiejing Environmental Protection Technology Co.,Ltd. Address before: 102200 Beijing city Changping District Machi Town kamis Road No. 18 building 201 room 2 Applicant before: BEIJING SHENWU POWER TECHNOLOGY Co.,Ltd. |
|
| TA01 | Transfer of patent application right | ||
| TA01 | Transfer of patent application right |
Effective date of registration: 20210421 Address after: 433099 B2205 room, B District, Xintiandi International Plaza, south of Golden Avenue, Xiantao, Hubei. Applicant after: Xiantao Fuzhong Biotechnology Co.,Ltd. Address before: No. 1391, south side, 10th floor, new material venture building, No. 7, Fenghui Middle Road, Haidian District, Beijing Applicant before: Beijing Jiejing Environmental Protection Technology Co.,Ltd. |
|
| TA01 | Transfer of patent application right | ||
| TA01 | Transfer of patent application right |
Effective date of registration: 20221021 Address after: 414018 No. 1, Baihua Avenue, Qianlianghu Town, Junshan District, Yueyang City, Hunan Province (in the yard of Hunan Jingtianren Paper Co., Ltd.) Applicant after: Hunan Dongqi Biomass Energy Co.,Ltd. Address before: 433099 B2205 room, B District, Xintiandi International Plaza, south of Golden Avenue, Xiantao, Hubei. Applicant before: Xiantao Fuzhong Biotechnology Co.,Ltd. |
|
| TA01 | Transfer of patent application right | ||
| RJ01 | Rejection of invention patent application after publication |
Application publication date: 20170728 |
|
| RJ01 | Rejection of invention patent application after publication |