CN86101230A - Gasification and reforming carbon carrier - Google Patents
Gasification and reforming carbon carrier Download PDFInfo
- Publication number
- CN86101230A CN86101230A CN198686101230A CN86101230A CN86101230A CN 86101230 A CN86101230 A CN 86101230A CN 198686101230 A CN198686101230 A CN 198686101230A CN 86101230 A CN86101230 A CN 86101230A CN 86101230 A CN86101230 A CN 86101230A
- Authority
- CN
- China
- Prior art keywords
- plasma generator
- gas
- separator
- fuel
- carbon carrier
- 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
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Classifications
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
- C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
- C01B3/32—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air
- C01B3/34—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents
- C01B3/36—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents using oxygen or mixtures containing oxygen as gasifying agents
-
- 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
- C10J3/46—Gasification of granular or pulverulent flues in suspension
- C10J3/48—Apparatus; Plants
- C10J3/485—Entrained flow gasifiers
-
- 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
- C10J2300/12—Heating the gasifier
- C10J2300/123—Heating the gasifier by electromagnetic waves, e.g. microwaves
- C10J2300/1238—Heating the gasifier by electromagnetic waves, e.g. microwaves by plasma
Abstract
The invention relates to the production composition and be mainly H
2The method and apparatus of the coal gas of+CO, wherein H
2O+CO
2Content be lower than 10%, simultaneously, can also improve the content of hydrogen in the said products, make the percentage composition that is higher than in the fuel.With spray regime oxygenant and fuel are joined in the reaction formula (2), use at least one plasma generator (5) to supply with external energy simultaneously, reactive carbon carrier is ejected in the gaseous mixture by nozzle (15,16,17), in order to make H
2O and CO
2Carbonization allows this gas mixture stop time enough in equipment, guarantees that carbonization is complete, like this H
2O and CO
2Remaining quantity in coal gas just can hang down to desired index.
Description
Content of the present invention is the method and apparatus about gasification fossil oil and reformed gas fuel, is CO+H to make major ingredient
2Coal gas, H wherein
2O+CO
2Content is less than 10%; Simultaneously, improve hydrogen content in the gas products that the present invention can also make above-mentioned carbonaceous fuel form.
Contain carbon monoxide and hydrogen and be the reducing gas on basis or the generation of burning gas, current can the realization with several technological processs of complete different principle, however they all respectively have some drawback.To these methods generally speaking, required energy is to burn and provide by initial carbonaceous material is ejected into furnace inner space together with oxygenant.For the needs heat, the CO and the H of certain share must be arranged in process of production
2Burn and produce CO
2And H
2O, therefore, the carbonic acid gas in this kind coal gas and the content of water are often than desirable height.
For after some carbonization technique process of knowing, must have a sepn process that water too much in the coal gas and carbonic acid gas composition are removed, reheat coal gas is followed in cooling earlier for this reason.In the other technological process, low tar and the phenol of consequently generating of the temperature of employing.This just means must to wash earlier before removing separation circuit follows reheat.
For this reason, an object of the present invention is to provide the method for gasification fossil oil and reformed gas fuel.With H in the coal gas of this method production
2O+CO
2Content can reduce to 0%.
A further object of the invention provides a kind of device of realizing the inventive method.This kind device also is applicable to gasification under the high pressure.
The purpose of above-mentioned requirements can reach by the method that the present invention adopts, comprising oxygenant and carbon support are ejected in the reaction chamber, at this moment supply with external energy by the plasma generator heated air, the reactive carrier carbon that spray fine is morcelled plays the H that makes existence in this reaction chamber
2O and CO
2The effect of carbonization allows this kind coal gas that enough residence time are arranged in equipment then, guarantees that carboniogenesis can make H
2O and CO
2In coal gas, reach desired residue content.Technological process of the present invention has some advantage compared with previously known method, since the coal gas that has adopted plasma generator to provide external energy to produce, its CO
2+ H
2The content of O is lower, accounts for 15% greatly, and the gas self heat is also high, and it can utilize self high temperature to carry out and then further reducing CO in the carboniogenesis step of back
2+ H
2The content of O.CO in principle
2+ H
2O content can reach 0%, and index often is chosen as 2-8% in practice.Spray fine is morcelled the technological operation of reactive carbon carrier can take high pressure, opposite, and when adopting block coke in the technological process when the sealing gland lock is fed in the furnace chamber, pressure is placed restrictions at about 3 crust.
According to the embodiment that the present invention suits, the approach of jet paraffin oxidation agent can be all or partially to pass through plasma generator.
According to another suitable embodiment of the present invention, gas is heated to 2000-3000 ℃ in plasma generator.
According to another suitable embodiment of the present invention, the injection of recirculating gas is by plasma generator, and oxygenant sprays into via the nozzle at the ventage place that is contained in plasma generator.
According to another suitable embodiment of the present invention, pure oxygen is used as oxygenant.
According to another suitable embodiment of the present invention, O
2, H
2O and/or CO
2, can also add small amount of N
2Gas mixture as oxygenant.
According to another suitable embodiment of the present invention, coal, mud coal/or the oiliness fossil oil, can mixing water, at this time H
2O is as oxygenant partly.
According to another suitable embodiment of the present invention, geseous fuel mainly is CH
4
According to another suitable embodiment of the present invention, the injection of carbonaceous fuel abuts against the ventage place of plasma generator.
According to another suitable embodiment of the present invention, be to spray into by nozzle with the injection of mud coal or oiliness carbonaceous fuel.This nozzle is contained in and is right after near the plasma generator ventage.
According to another suitable embodiment of the present invention, dryness material and gas are by one or more nozzles/or spray into by an annulus during as carbonaceous fuel, nozzle or annulus be installed in plasma generator ventage around.
According to another suitable embodiment of the present invention, reactive carbon carrier sprays into via one or more nozzles, the most handy coke of reactive carbon carrier.
According to another suitable embodiment of the present invention, most of waste residue is to discharge with liquid state.
According to another suitable embodiment of the present invention, the coal gas of generation will carry out heat exchange or cooling.
According to another suitable embodiment of the present invention, the sulphur receptor sprays into by one or more nozzles, meticulous lime of morcelling and rhombspar that the sulphur receptor is selected for use.
For the device of realizing the inventive method should comprise the following parts: have a reaction chamber (stove) at least; At least one plasma generator is to supply with external energy; Feed device with the gas of plasma generator heating; Be connected near the feed device that is used as jet paraffin oxidation agent and fuel of plasma generator; The feed device of reactive carbon carrier and sulphur receptor material; The outlet pipe of gas outlet tube and discharging waste residue and slag ash.
According to the suitable embodiment of the present invention, plasma generator contains cylindrical electrode, between the electrode, produces electric arc.
According to another suitable embodiment of the present invention, plasma generator is a kind of moving electric arc type.
According to another suitable embodiment of the present invention.Its device is made up of following, a vertical columnar stove, divide as gasification zone and carbonizing zone, between these two districts, can have one to tighten shape, have an outlet to be used for the removal liquid state waste slag in the furnace chamber bottom, low part device one gas eduction tube at furnace chamber, this pipe coupling is to back one separator, and an outlet is arranged at the bottom of separator, is used for discharging solid slag, with non-volatile material, at the upper unit gas outlet tube of separator.The feed device of described reactive carbon carrier and sulphur receptor is a place or the many places that are assemblied in furnace chamber, and its position is to be connected gas to leave near the outlet pipe of furnace chamber.
According to another suitable embodiment of the present invention, separator designs becomes the cyclonic separator pattern, is particularly suitable for removing the solid particulate in the coal gas.
According to another suitable embodiment of the present invention, heat exchanger is arranged at the gas outlet device of vertical furnace chamber gas outlet and/or separator.
According to another suitable embodiment of the present invention, the method for feeding of carbon carrier and oxygenant is spurted into furnace chamber by at least one and/or an annulus, and it is assemblied near the gas port place that is connected of furnace chamber and plasma generator.
Further with regard to characteristics of the present invention, advantage, and embodiment are further described below.
Have a tangible advantage be in the gasification zone pneumatolysis major part finish, then carboniogenesis reaches degree completely in carbonizing zone.
Gasification can at high temperature be carried out in this case, and the gasification effect is always carried out being higher than under the melting temperature of waste residue, generally is higher than 1400 ℃, and thereafter, the heat of self can carry out carboniogenesis effectively in the carbonization chamber of back.Because just stop 1000 ℃ of following carboniogenesiss.
Excessive heat in the coal gas can be used by several means.In the coal gas that in vaporizer, generates, water that content is lower and carbonic acid gas can utilize heat further reduction after running into the reactive carbon carrier that sprays furnace chamber of coal gas self comparatively speaking, and water and carbonic acid gas convert hydrogen and carbon monoxide separately to as a result.
Illustrate, to CO
2And H
2The O content requirement is low, in fact can not directly reach at vaporizing chamber, because amount of oxygen is few, so the speed of reaction between fuel and oxygenant is also low, thereby the gasification effect is incomplete.
Carbonaceous fuel can be selected from a following class material: oil, coal, coke, charcoal, mud coal, sawdust and their various mixtures, gaseous hydrocarbons be CH for example
4Propose these some, come ratio with in the past coal gasification technical process, have very economical superiority, technology in the past nearly all is subjected to about selecting placing restrictions on of starting material.
Now with regard to device of the present invention, the contrast accompanying drawing is described in further detail.The device that draws among the figure is for realizing the preferred means scheme of the inventive method.
Include a vertical cylindrical chamber 1 in the device, it is made up of zone of transformation 2 and carbonizing zone 3, and these two districts by deflation place 4 separately can still communicate each other.Have a plasma generator 5 at least, device is located in the import (6) at the top of furnace chamber, and the gas of introducing is heated in plasma generator.Installed annulus 7 in addition, for supplying with oxygenant and carrier carbon in furnace chamber, the ventage near plasma generator installed very nearby inlet pipe 7 ' and nozzle 8,8 '.
The carbonizing zone 3 that is positioned at below the gasification zone is connected with separator 11 by a gas pipeline 10, guarantees that with this coal gas has the sufficiently long residence time in device, thereby makes carboniogenesis carry out fully, to reach desired H
2O and CO
2Low residual volume index.Separator is the vertical shaft 12 of a round shape, if it is made the form of cyclonic separator, better effects if makes and can remove deleterious solids in the coal gas at an easy rate, such as the waste residue and the non-volatile material of drop.
The most waste residue that produces in the gasification zone 2 is to discharge through the waste residue outlet pipe under the round shape gasification zone of furnace chamber 1 13.The particle of carrying secretly in the coal gas then is waste residue outlet pipe 14 dischargings through the separator bottom.
Airway 10 also plays the partly effect of carbonizing zone 3 on function.For the supply response carbon carrier and/or supply with the sulphur receptor in furnace chamber, installed nozzle 15,16,17, the position is respectively in the gasification zone, carbonizing zone and airway 10 places of being chatted.Need on the technology, the waste residue thing also can be ejected in the device by these several nozzles and go.
Install gas change heater 18 above separator 11, its effect makes product coal gas carry out heat exchange or cooling, can give hot oxidant with the waste heat of coal gas, and coal gas can also have the alternative heat exchange by the interchanger of device at airway 10 places.
Colder product coal gas can also be given to recirculation heating in plasma generator, in this case, oxygenant mainly is to enter through nozzle 8,8 ' injection.
Claims (23)
1, provides about the gasification fossil oil and transform vaporising fuel to produce major ingredient be CO and H
2The method of coal gas, it is characterized in that wherein H
2O+CO
2Content less than 10%, be generally 2-8%, hydrogen content in this coal gas composition can be brought up to the composition that is higher than carbonaceous fuel by measure of the present invention, these measures comprise: the method with the plasma generator heated air provides external energy, while jet paraffin oxidation agent and carbon carrier in reaction chamber, the reactive carbon carrier that spray fine is morcelled is sneaked into by in the gaseous mixture that flows down in the reaction chamber, makes the H of existence
2O and CO
2Play carboniogenesis, and allow gas mixture that enough residence time are arranged, so that H in the coal gas that obtains
2O and CO
2Content reaches desired low index.
2, according to the process of claim 1 wherein that spraying into of oxygenant can be fully or partly pass through plasma generator.
3, according to the process of claim 1 wherein, gas is heated to 2000～3000 ℃ in plasma generator.
4, according to the process of claim 1 wherein that recirculating gas is to spurt in the furnace chamber via plasma generator, and oxygenant is to spray into by the nozzle near the ventage of plasma generator.
5, according to the process of claim 1 wherein that pure oxygen is used as oxygenant.
6, according to the process of claim 1 wherein O
2, H
2O and/or CO
2, perhaps add small amount of N
2Gas mixture be used as oxygenant.
7, according to the process of claim 1 wherein coal, mud coal and/or contain the butyrous fossil oil, can ooze a little water of amalgamation, water can be used as the partial oxidation agent and used this moment.
8, according to the process of claim 1 wherein that geseous fuel mainly is meant CH
4(methane).
9, according to the process of claim 1 wherein that carbonaceous fuel is to spray into from abutting against the plasma generator ventage.
10, according to the method for claim 9, wherein carbonaceous fuel is if mud coal or oiliness thing, and spraying into of it is that nozzle by abutting against plasma generator ventage vicinity sprays into.
11, according to the method for claim 9, wherein carbonaceous fuel be dryness or during gaseous state, spraying into by device of it sprays at one or more nozzles in plasma generator ventage place and/or an annulus.
12, according to the process of claim 1 wherein reactive carbon carrier best be coke, it sprays into by one or more nozzles.
13, according to claim 1, wherein Da Bufen waste residue is to discharge with liquid state.
14, according to claim 1, wherein the coal gas that is generated is in the front of separator and/or the back of separator, the experience heat exchanging process.
15, according to the process of claim 1 wherein that sulphur receptor material is to spray into by one or more nozzles, the sulphur receptor selects for use the meticulous lime of morcelling better.
16, produce with CO and H with gasification fossil oil and reformed gas fuel
2Be the coal gas of main component, require wherein H
2O+CO
2Content is less than 10%, and general requirement is 2-8%, and the hydrogen content that can also improve in the coal gas makes the composition that is higher than carbonaceous fuel, reaches these requirements, and device of the present invention comprises at least one reaction chamber (2); Have at least a plasma generator (5) to provide external energy, make gas enter (6) back and heated by plasma generator with (5); Its device of nozzle (8,8 ') that is used for jet paraffin oxidation agent and fuel is near the plasma generator end opening; Feed device (15,16,17) is used for reactive carbon carrier and the surge of sulphur receptor are advanced furnace chamber; Gas outlet tube (19) and waste residue and slag ash relief outlet (13,14).
17, according to the device of claim 16, wherein the action type of plasma generator (5) is an electric arc in producing between two electrodes.
18, according to the device of claim 16, wherein plasma generator (5) is the moving electric arc type.
19, according to the device of claim 16, include a cylindrical chamber (1), it is divided into two districts, one be gasification zone (2) another be carbonizing zone (3), can have one to tighten shape between two districts, the outlet pipe (13) of discharge liquid waste residue is housed in the furnace chamber bottom, lower position attaching one gas eduction tube (10) at furnace chamber, it links to each other with the separator (11) of back, the bottom of separator is the outlet pipe (14) of discharging solid slag and non-volatile part of material, and gas outlet tube (19) is installed in the top of separator.
20, according to the device of claim 16, the feed device (15,16,17) that wherein is used for spraying reactive carbon carrier and sulphur receptor material respectively is installed in a place of furnace chamber or a few place and nozzle (17) respectively and is connected the other airway (10) of furnace chamber and locates.
21, according to the device of claim 16, wherein work as separator (11) and be designed to cyclonic separator, help from product coal gas, removing solids.
22, according to the device of claim 16, to locate and/or the outlet pipe (19) on separator (11) top is located device interchanger is arranged at the gas export control (10) that connects vertical furnace chamber, the latter's interchanger is numbered (18).
23, according to the device of claim 16, wherein constituting of the feed device of carbon carrier and oxygenant has each (8,8 ') nozzle at least and/or abuts against plasma generator (5) and device one annulus, Link Port place of reaction chamber (2).
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| SE8501006-4 | 1985-03-01 | ||
| SE8501006A SE453920B (en) | 1985-03-01 | 1985-03-01 | SET AND DEVICE FOR GASING OF FOSSIL FUEL AND REFORM OF GAS FUEL |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN86101230A true CN86101230A (en) | 1986-10-01 |
Family
ID=20359324
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN198686101230A Pending CN86101230A (en) | 1985-03-01 | 1986-03-01 | Gasification and reforming carbon carrier |
Country Status (7)
| Country | Link |
|---|---|
| CN (1) | CN86101230A (en) |
| AU (1) | AU5400786A (en) |
| BR (1) | BR8600856A (en) |
| DE (1) | DE3605715A1 (en) |
| FR (1) | FR2578263B1 (en) |
| SE (1) | SE453920B (en) |
| ZA (1) | ZA861260B (en) |
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101220297B (en) * | 2008-01-30 | 2011-12-28 | 广东科达机电股份有限公司 | Method and apparatus for gas production |
| CN101910375B (en) * | 2007-12-28 | 2014-11-05 | 格雷特波因特能源公司 | Steam generating slurry gasifier for the catalytic gasification of a carbonaceous feedstock |
| CN106947543A (en) * | 2017-04-14 | 2017-07-14 | 中美新能源技术研发（山西）有限公司 | A kind of GPG II gasification and pyrolysis integral reactor and process units and technique |
| CN106947544A (en) * | 2017-04-14 | 2017-07-14 | 中美新能源技术研发（山西）有限公司 | A kind of gasification and pyrolysis integral type top spray reactors of GPG IV and process units and technique |
| CN106947542A (en) * | 2017-04-14 | 2017-07-14 | 中美新能源技术研发（山西）有限公司 | A kind of GPG V gasification and pyrolysis integral type top spray reactor and process units and technique |
| CN106978213A (en) * | 2017-04-14 | 2017-07-25 | 中美新能源技术研发（山西）有限公司 | A kind of gasification and pyrolysis integral reactors of GPG I and process units and technique |
| CN106995725A (en) * | 2017-04-14 | 2017-08-01 | 中美新能源技术研发（山西）有限公司 | A kind of gasification and pyrolysis integral type top spray reactors of GPG III and process units and technique |
Families Citing this family (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| SE457355B (en) * | 1985-09-25 | 1988-12-19 | Skf Steel Eng Ab | MAKE SURE TO PREPARE A CLEAN, CARBON OXIDE AND GAS GAS INCLUDING GAS |
| EP0305047B1 (en) * | 1987-08-28 | 1993-02-17 | Texaco Development Corporation | High temperature desulfurization of synthesis gas |
| US4880439A (en) * | 1988-05-05 | 1989-11-14 | Texaco Inc. | High temperature desulfurization of synthesis gas |
| DD299613A7 (en) * | 1990-02-26 | 1992-04-30 | �������@������������@��k�� | PROCESS FOR THE STABLE OPERATION OF PLASMATRONS WITH WATER VAPOR AS PLASMAGAS |
| DE19739181A1 (en) * | 1997-09-08 | 1999-03-11 | Abb Research Ltd | Discharge reactor and use of the same |
| ATE350334T1 (en) * | 2001-06-26 | 2007-01-15 | H2 Tec Ag | METHOD AND DEVICE FOR PRODUCING HYDROGEN |
| AT503517B1 (en) * | 2002-11-04 | 2010-05-15 | New Plasma Gmbh & Co Keg | METHOD FOR ACTIVATING, ESPECIALLY GASOLATED, CARBON CONTAINING SUBSTANCES |
Family Cites Families (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| SE371453C (en) * | 1973-03-26 | 1978-01-12 | Skf Ind Trading & Dev | KIT FOR PRODUCTION OF REDUCTION GAS |
| CA1059065A (en) * | 1975-12-12 | 1979-07-24 | Terence E. Dancy | Arc reforming of hydrocarbons |
| US4013428A (en) * | 1976-01-26 | 1977-03-22 | The Marquardt Company | Coal gasification process |
| DE2822862C2 (en) * | 1978-05-26 | 1984-01-05 | Ruhrchemie Ag, 4200 Oberhausen | Process for the production of gas mixtures containing hydrogen and carbon monoxide by gasifying carbon-containing, ash-forming fuels |
| US4278446A (en) * | 1979-05-31 | 1981-07-14 | Avco Everett Research Laboratory, Inc. | Very-high-velocity entrained-bed gasification of coal |
| EP0050863A1 (en) * | 1980-10-24 | 1982-05-05 | Hitachi, Ltd. | Process of and apparatus for gasifying coals |
| DE3104281C2 (en) * | 1981-02-07 | 1985-10-31 | SKF Steel Engineering AB, Hofors | Method and device for the production of sponge iron |
-
1985
- 1985-03-01 SE SE8501006A patent/SE453920B/en not_active IP Right Cessation
-
1986
- 1986-02-20 ZA ZA861260A patent/ZA861260B/en unknown
- 1986-02-22 DE DE19863605715 patent/DE3605715A1/en not_active Ceased
- 1986-02-24 AU AU54007/86A patent/AU5400786A/en not_active Abandoned
- 1986-02-28 FR FR868602841A patent/FR2578263B1/en not_active Expired - Fee Related
- 1986-02-28 BR BR8600856A patent/BR8600856A/en unknown
- 1986-03-01 CN CN198686101230A patent/CN86101230A/en active Pending
Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101910375B (en) * | 2007-12-28 | 2014-11-05 | 格雷特波因特能源公司 | Steam generating slurry gasifier for the catalytic gasification of a carbonaceous feedstock |
| US9234149B2 (en) | 2007-12-28 | 2016-01-12 | Greatpoint Energy, Inc. | Steam generating slurry gasifier for the catalytic gasification of a carbonaceous feedstock |
| CN101220297B (en) * | 2008-01-30 | 2011-12-28 | 广东科达机电股份有限公司 | Method and apparatus for gas production |
| CN106947543A (en) * | 2017-04-14 | 2017-07-14 | 中美新能源技术研发（山西）有限公司 | A kind of GPG II gasification and pyrolysis integral reactor and process units and technique |
| CN106947544A (en) * | 2017-04-14 | 2017-07-14 | 中美新能源技术研发（山西）有限公司 | A kind of gasification and pyrolysis integral type top spray reactors of GPG IV and process units and technique |
| CN106947542A (en) * | 2017-04-14 | 2017-07-14 | 中美新能源技术研发（山西）有限公司 | A kind of GPG V gasification and pyrolysis integral type top spray reactor and process units and technique |
| CN106978213A (en) * | 2017-04-14 | 2017-07-25 | 中美新能源技术研发（山西）有限公司 | A kind of gasification and pyrolysis integral reactors of GPG I and process units and technique |
| CN106995725A (en) * | 2017-04-14 | 2017-08-01 | 中美新能源技术研发（山西）有限公司 | A kind of gasification and pyrolysis integral type top spray reactors of GPG III and process units and technique |
Also Published As
| Publication number | Publication date |
|---|---|
| ZA861260B (en) | 1987-10-28 |
| SE8501006L (en) | 1986-09-02 |
| DE3605715A1 (en) | 1986-09-04 |
| BR8600856A (en) | 1986-11-11 |
| SE453920B (en) | 1988-03-14 |
| FR2578263B1 (en) | 1991-03-22 |
| FR2578263A1 (en) | 1986-09-05 |
| SE8501006D0 (en) | 1985-03-01 |
| AU5400786A (en) | 1986-09-04 |
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