CN115246628B - Purification method for synthesis gas at outlet of organic hazardous waste plasma gasification melting furnace - Google Patents
Purification method for synthesis gas at outlet of organic hazardous waste plasma gasification melting furnace Download PDFInfo
- Publication number
- CN115246628B CN115246628B CN202110908439.4A CN202110908439A CN115246628B CN 115246628 B CN115246628 B CN 115246628B CN 202110908439 A CN202110908439 A CN 202110908439A CN 115246628 B CN115246628 B CN 115246628B
- Authority
- CN
- China
- Prior art keywords
- synthesis gas
- melting furnace
- gasification melting
- plasma gasification
- oxygen
- 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.)
- Active
Links
- 230000015572 biosynthetic process Effects 0.000 title claims abstract description 78
- 238000003786 synthesis reaction Methods 0.000 title claims abstract description 78
- 238000002844 melting Methods 0.000 title claims abstract description 29
- 230000008018 melting Effects 0.000 title claims abstract description 29
- 238000009272 plasma gasification Methods 0.000 title claims abstract description 29
- 238000000034 method Methods 0.000 title claims abstract description 28
- 239000002920 hazardous waste Substances 0.000 title claims abstract description 22
- 238000000746 purification Methods 0.000 title claims abstract description 8
- 239000007789 gas Substances 0.000 claims abstract description 93
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims abstract description 39
- 239000001301 oxygen Substances 0.000 claims abstract description 39
- 229910052760 oxygen Inorganic materials 0.000 claims abstract description 39
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims abstract description 38
- 238000006243 chemical reaction Methods 0.000 claims abstract description 25
- 238000011084 recovery Methods 0.000 claims description 18
- 238000005406 washing Methods 0.000 claims description 18
- 239000000428 dust Substances 0.000 claims description 17
- 239000002918 waste heat Substances 0.000 claims description 11
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims description 9
- 239000003513 alkali Substances 0.000 claims description 7
- 239000004744 fabric Substances 0.000 claims description 6
- 238000011143 downstream manufacturing Methods 0.000 claims description 3
- 239000007788 liquid Substances 0.000 claims description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 3
- 238000002407 reforming Methods 0.000 claims 1
- 238000005516 engineering process Methods 0.000 abstract description 7
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 abstract description 4
- 230000003197 catalytic effect Effects 0.000 abstract description 4
- 230000003647 oxidation Effects 0.000 abstract description 4
- 238000007254 oxidation reaction Methods 0.000 abstract description 4
- 239000010865 sewage Substances 0.000 abstract description 2
- 239000000571 coke Substances 0.000 description 4
- 238000002309 gasification Methods 0.000 description 4
- 230000000694 effects Effects 0.000 description 3
- 239000000463 material Substances 0.000 description 3
- 239000007800 oxidant agent Substances 0.000 description 3
- 230000001590 oxidative effect Effects 0.000 description 3
- 238000005336 cracking Methods 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000011160 research Methods 0.000 description 2
- 238000005507 spraying Methods 0.000 description 2
- 239000002699 waste material Substances 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- 206010021143 Hypoxia Diseases 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000010891 electric arc Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 238000002386 leaching Methods 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 238000009832 plasma treatment Methods 0.000 description 1
- 238000010248 power generation Methods 0.000 description 1
- 239000000047 product Substances 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
- 238000012827 research and development Methods 0.000 description 1
- 238000005201 scrubbing Methods 0.000 description 1
- 239000002002 slurry Substances 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 239000002910 solid waste Substances 0.000 description 1
- 239000013589 supplement Substances 0.000 description 1
- 238000012360 testing method Methods 0.000 description 1
- 238000004065 wastewater treatment Methods 0.000 description 1
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
- C01B3/50—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
- C01B2203/0465—Composition of the impurity
- C01B2203/048—Composition of the impurity the impurity being an organic compound
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Engineering & Computer Science (AREA)
- Combustion & Propulsion (AREA)
- Inorganic Chemistry (AREA)
- Processing Of Solid Wastes (AREA)
Abstract
The invention discloses a purification method for synthesis gas at an outlet of an organic hazardous waste plasma gasification melting furnace, and belongs to the technical field of organic hazardous waste treatment. The method mainly comprises the steps that a synthesis gas outlet of a plasma gasification melting furnace is communicated with an outer annular channel of a conversion burner on a reformer through a pipeline, so that crude synthesis gas generated by the plasma gasification melting furnace is sprayed into the reformer through the outer annular channel; the oxygen source is communicated with the inner central pipeline of the conversion burner, so that oxygen generated by the oxygen source is sprayed into the conversion furnace through the inner central pipeline simultaneously with the crude synthetic gas, and the relation between the pressure, flow and temperature of the crude synthetic gas and the oxygen is limited. The method solves the problem that the crude synthesis gas contains tar and methane and the problem of sewage treatment by a pure oxygen non-catalytic partial oxidation technology; meanwhile, the method ensures that the synthetic gas does not contain methane, improves the content of effective gas, can meet the demands of downstream users, and has low operation cost.
Description
Technical Field
The invention relates to a purification method for synthesis gas at an outlet of an organic hazardous waste plasma gasification melting furnace, and belongs to the technical field of organic hazardous waste treatment.
Background
The plasma treatment technology of solid waste starts in the 70 s of the last century and is primarily used for treating low-radioactivity waste and destroying military weapons, and enters civilian use in 1990. At present, tens of research units for treating dangerous waste by plasma are in China, and with technology upgrading and research and development, part of the research units start to enter a commercial test operation stage. The technology used at the present stage adopts a plasma torch to directly gasify the hazardous waste at high temperature, generates plasma with the temperature of up to 5000 ℃ through arc discharge, heats the hazardous waste to the cracking temperature, and supplements air or oxygen-enriched air at the same time to crack and gasify the organic matters in the hazardous waste to be converted into synthesis gas. The synthesis gas is usually subjected to heat recovery through a waste heat boiler, and then washed and purified to produce the synthesis gas for downstream use.
The plasma gasification melting furnace is used for treating organic hazardous waste with carbon content up to 35%, and because the organic hazardous waste is affected by morphology, viscosity and the like, the organic hazardous waste is unevenly distributed in the gasification furnace, and synthesis gas containing tar and methane can be generated under the condition of oxygen deficiency. First, tar can cause fouling and plugging of downstream equipment pipelines and cause high-cost and difficult wastewater treatment problems; second, tar and methane can degrade the syngas quality and may not meet downstream customer requirements, thereby affecting downstream products.
The Chinese patent Xia Minggui et al CN200910272197.3 discloses a combustible material plasma high-temperature gasification process and equipment thereof, wherein a coke bed layer is paved at the bottom of a gasification furnace; and continuously putting the combustible material, the fluxing agent and the supplementary coke on a coke bed layer, spraying a primary oxidant, starting a primary plasma torch to generate high temperature and high heat, gasifying the combustible material to generate synthetic gas, introducing the crude synthetic gas into a gas-solid separator to remove impurities, and finally introducing the synthetic gas into a tar remover. And spraying a secondary oxidant and starting a secondary plasma torch to crack residual tar, so that a better effect is achieved. However, the tar remover is internally provided with the secondary plasma torch, so that the power consumption is increased and the treatment cost is increased; and because the secondary oxidant nozzle and the synthetic gas inlet are arranged separately, the structure is more complex, and the methane content in the outlet synthetic gas is high.
The invention patent No. Zheng Lihui et al CN202010632404.8 discloses a method for regulating the composition and the heat value of the synthesis gas of a plasma gasification melting furnace, which is characterized in that oxygen-enriched air is supplemented by establishing a slurry layer and a coke layer, and finally the synthesis gas meeting the urban gas standard is produced, so that a better effect is achieved. However, the synthesis gas produced by this method contains up to 2.3% of tar which may be removed physically by scrubbing.
In summary, the prior art cannot remove methane in the synthesis gas, and the tar removal method is relatively unreasonable, so that the problem cannot be thoroughly solved, the quality of the synthesis gas is low, and certain environmental protection problems are brought.
Disclosure of Invention
In order to solve the technical problems, the invention provides a purification method for the synthesis gas at the outlet of the organic hazardous waste plasma gasification melting furnace, which can effectively remove tar and methane in the crude synthesis gas to produce high-quality synthesis gas and has lower operation cost.
The technical scheme of the invention is as follows:
a purification method for the synthesis gas at the outlet of an organic hazardous waste plasma gasification melting furnace is characterized by comprising the following steps: the method comprises the steps that a synthesis gas outlet of a plasma gasification melting furnace is communicated with an outer annular channel of a conversion burner on a reformer through a pipeline, so that crude synthesis gas generated by the plasma gasification melting furnace is sprayed into the reformer through the outer annular channel; and communicating an oxygen source with an inner central pipeline of the conversion burner, so that oxygen generated by the oxygen source is sprayed into the conversion furnace through the inner central pipeline simultaneously with the crude synthesis gas.
The further technical scheme is as follows:
the pressure of the oxygen entering the inner central pipeline of the conversion burner is 6-7KPa higher than the pressure of the crude synthesis gas entering the outer annular channel of the conversion burner.
The further technical scheme is as follows:
the flow rate of oxygen entering the inner central pipeline of the conversion burner is 1.5-1.8 times of the flow rate of methane in the crude synthesis gas entering the outer annular channel.
The further technical scheme is as follows:
the temperature of the raw synthesis gas exiting the synthesis gas outlet of the plasma gasification melting furnace is 900-1100 ℃.
The further technical scheme is as follows:
the oxygen concentration of the inner central conduit entering the reformer burner is at least 90vol.%.
The further technical scheme is as follows:
the method further comprises the steps of sequentially carrying out waste heat recovery, dust removal and alkali washing on the synthesis gas exiting the reformer to obtain purified synthesis gas, wherein the purified synthesis gas can be directly used for downstream processes.
The further technical scheme is as follows:
the waste heat recovery mode is at least one of steam boiler type heat recovery, hot water heat exchanger type heat recovery and air heat exchanger type heat recovery.
The further technical scheme is as follows:
the dust removing mode is at least one of cyclone dust removing and cloth bag dust removing.
The further technical scheme is as follows:
the alkaline washing mode is that a 1-4-level alkaline washing tower is adopted for alkaline washing, wherein the alkaline liquid of the alkaline washing tower adopts 5-15 wt.% sodium hydroxide solution, and the flow is 150-400m 3 /h。
The beneficial technical effects of the invention are as follows:
the invention utilizes pure oxygen non-catalytic partial oxidation technology to introduce the crude synthesis gas and oxygen generated by the plasma gasification melting furnace into different channels of the conversion burner, wherein the oxygen is sprayed out from an inner central pipeline, the crude synthesis gas is sprayed out from an outer annular channel, and the oxygen sprayed out from the center has the functions of fully atomizing and mixing the crude synthesis gas sprayed out from the outer annular channel. After entering the reformer, the oxygen molecules crack tar and synthesis gas at high temperature, and the synthesis gas exiting the reformer can be directly used in downstream after waste heat recovery, dust removal and alkali leaching, including use in gas boilers, gas power generation, other gas heating equipment and the like.
The method solves the problem that the crude synthesis gas contains tar and methane, and solves the problem of sewage treatment by cracking and gasifying the tar and the methane through a pure oxygen non-catalytic partial oxidation technology; meanwhile, the method ensures that the synthetic gas does not contain methane, improves the content of effective gas, can meet the demands of downstream users, and has low operation cost.
Drawings
FIG. 1 is a process flow diagram of the method of the present invention.
Detailed Description
In order that the manner in which the above recited features of the present invention are attained and can be understood in detail, a more particular description of the invention, briefly summarized below, may be had by reference to the appended drawings and examples, which are illustrated in their embodiments, but are not intended to limit the scope of the invention.
The invention discloses a purification method for synthesis gas at an outlet of an organic hazardous waste plasma gasification melting furnace, which comprises the steps of communicating a synthesis gas outlet of the plasma gasification melting furnace with an outer annular channel of a conversion burner on a reformer through a pipeline, so that crude synthesis gas generated by the plasma gasification melting furnace is sprayed into the reformer through the outer annular channel; and communicating an oxygen source with an inner central pipeline of the conversion burner, so that oxygen generated by the oxygen source is sprayed into the conversion furnace through the inner central pipeline simultaneously with the crude synthesis gas.
The temperature of the crude synthesis gas discharged from the synthesis gas outlet of the plasma gasification melting furnace is 900-1100 ℃, and the main components of the crude synthesis gas comprise CO and CO 2 、H 2 、H 2 O、N 2 、CH 4 (methane) and tar. The oxygen concentration of the inner central tube entering the reformer burner used above is at least 90vol.%, the higher the concentration, the better the oxygen concentration, and in this embodiment the oxygen concentration of the oxygen source used is 92vol.% in combination with the prior art and cost requirements etc.
When the raw synthesis gas and oxygen are introduced into the conversion burner, the pressure of the oxygen entering the inner central pipeline of the conversion burner is 6-7KPa higher than the pressure of the raw synthesis gas entering the outer annular channel of the conversion burner, and the flow rate of the oxygen entering the inner central pipeline of the conversion burner is 1.5-1.8 times of the flow rate of methane in the raw synthesis gas entering the outer annular channel, wherein the flow rate of the oxygen is calculated as 92vol.% concentration oxygen.
In addition, the method further comprises the steps of sequentially carrying out waste heat recovery, dust removal and alkali washing on the synthesis gas discharged from the reformer to obtain purified synthesis gas, wherein the purified synthesis gas can be directly used for downstream processes.
The waste heat recovery mode is at least one of steam boiler type heat recovery, hot water heat exchanger type heat recovery and air heat exchanger type heat recovery, and can also be other heat recovery or heat utilization modes.
The dust removing mode is at least one of cyclone dust removing and cloth bag dust removing, and the gas dust removing efficiency is up to 99.9% or above.
Wherein the alkaline washing mode is that a 1-4-level alkaline washing tower is adopted for alkaline washing, wherein the alkaline liquid of the alkaline washing tower adopts 5-15 wt.% sodium hydroxide solution, and the flow is 150-400m 3 /h。
Detailed description of the preferred embodiments
(1) The calorific value of the organic hazardous waste is 3496kcal/kg, and 3 tons per hour are treated.
(2) The temperature of the raw synthesis gas exiting the plasma gasification melting furnace was 1050 ℃, and the flow rate was 5208Nm 3 /h, pressure 15KPa, wherein CO/CO 2 /H 2 /H 2 O/N 2 /CH 4 The contents (V%) of (C) were 32.12, 10.21, 23.54, 18.98, 10.01, 4.21, respectively, and tar was 6.3g/Nm 3 。
(3) 92vol.% oxygen concentration in the reformer at 21KPa, ambient temperature, 389Nm flow 3 /h。
(4) The synthesis gas from the reformer was discharged with a tar content of 5ppm.
(5) The synthesis gas from the reformer is recovered by a waste heat boiler, and after dust removal by a cloth bag and alkali liquor washing, the purified synthesis gas flow is 4558Nm 3 /h, wherein CO/CO 2 /H 2 /H 2 O/N 2 The contents (V%) of (C) are 43.08, 12.75, 27.72, 0.16 and 12.2 respectively, the tar content is less than 1ppm, and the methane content is 65ppm.
Second embodiment
(1) The calorific value of the organic hazardous waste is 3518kcal/kg, 3 tons per hour being treated.
(2) Raw synthesis gas temperature 1057 ℃ and flow 5119Nm of plasma gasification melting furnace 3 /h, pressure 15KPa, wherein CO/CO 2 /H 2 /H 2 O/N 2 /CH 4 The contents (V%) of (C) were 33.28, 11.38, 23.27, 17.95, 9.08, 3.36, respectively, and tar was 5.9g/Nm 3 。
(3) 92vol.% of oxygen concentration in the reformer, 21KPa, normal temperatureFlow rate 326Nm 3 /h。
(4) The synthesis gas from the reformer was taken off with a tar content of 6ppm.
(5) The synthesis gas from the reformer is recovered by a waste heat boiler, and after dust removal by a cloth bag and alkali liquor washing, the purified synthesis gas flow is 4526Nm 3 /h, wherein CO/CO 2 /H 2 /H 2 O/N 2 The contents (V%) of (C) are 42.51, 13.06, 26.14, 0.13 and 13.59 respectively, the tar content is less than 1ppm, and the methane content is 54ppm.
Detailed description of the preferred embodiments
(1) The calorific value of the organic hazardous waste is 4004kcal/kg, and 3 tons per hour are treated.
(2) The raw synthesis gas temperature exiting the plasma gasification melting furnace was 1048 ℃, and the flow 5671Nm 3 /h, pressure 15KPa, wherein CO/CO 2 /H 2 /H 2 O/N 2 /CH 4 The contents (V%) of (C) were 34.89, 12.39, 22.76, 16.56, 6.30, 6.21, respectively, and tar was 6.8g/Nm 3 。
(3) Oxygen concentration in the reformer was 92%, pressure 21KPa, ambient temperature, flow 560Nm 3 /h。
(4) The synthesis gas from the reformer was discharged with a tar content of 5ppm.
(5) The synthesis gas from the reformer is recovered by a waste heat boiler, and after dust removal by a cloth bag and alkali liquor washing, the purified synthesis gas flow is 5291Nm 3 /h, wherein CO/CO 2 /H 2 /H 2 O/N 2 The contents (V%) of (C) are 46.09, 13.07, 25.22, 0.07 and 6.8 respectively, the tar content is less than 1ppm and the methane content is 56ppm.
The method uses pure oxygen non-catalytic partial oxidation technology, and the crude synthesis gas and high-concentration oxygen which are discharged from the plasma gasification melting furnace are introduced into a conversion burner from different channels, and after being introduced into the conversion furnace, the high-temperature oxygen molecules crack tar and methane in the gasification synthesis gas, remove the tar and methane, and produce high-quality synthesis gas with low running cost.
The above description is only of the preferred embodiments of the present invention and is not intended to limit the present invention, and it should be noted that it is possible for those skilled in the art to make several improvements and modifications without departing from the technical principle of the present invention, and these improvements and modifications should also be regarded as the protection scope of the present invention.
Claims (4)
1. A purification method for the synthesis gas at the outlet of an organic hazardous waste plasma gasification melting furnace is characterized by comprising the following steps: the method comprises the steps that a synthesis gas outlet of a plasma gasification melting furnace is communicated with an outer annular channel of a conversion burner on a reformer through a pipeline, so that crude synthesis gas generated by the plasma gasification melting furnace is sprayed into the reformer through the outer annular channel; communicating an oxygen source with an inner central pipeline of the conversion burner, so that oxygen generated by the oxygen source is sprayed into the conversion furnace through the inner central pipeline simultaneously with the crude synthesis gas;
the temperature of the crude synthesis gas exiting the synthesis gas outlet of the plasma gasification melting furnace is 900-1100 ℃;
the oxygen concentration of the inner central conduit entering the reforming burner is at least 90vol.%;
the pressure of the oxygen entering the inner central pipeline of the conversion burner is 6-7KPa higher than the pressure of the crude synthesis gas entering the outer annular channel of the conversion burner;
the flow rate of oxygen entering the inner central pipeline of the conversion burner is 1.5-1.8 times of the flow rate of methane in the crude synthesis gas entering the outer annular channel;
the method further comprises the steps of sequentially carrying out waste heat recovery, dust removal and alkali washing on the synthesis gas exiting the reformer to obtain purified synthesis gas, wherein the purified synthesis gas can be directly used for downstream processes.
2. The method for purifying synthesis gas at the outlet of an organic hazardous waste plasma gasification melting furnace according to claim 1, wherein: the waste heat recovery mode is at least one of steam boiler type heat recovery, hot water heat exchanger type heat recovery and air heat exchanger type heat recovery.
3. The method for purifying synthesis gas at the outlet of an organic hazardous waste plasma gasification melting furnace according to claim 1, wherein: the dust removing mode is at least one of cyclone dust removing and cloth bag dust removing.
4. The method for purifying synthesis gas at the outlet of an organic hazardous waste plasma gasification melting furnace according to claim 1, wherein: the alkaline washing mode is that a 1-4-level alkaline washing tower is adopted for alkaline washing, wherein the alkaline liquid of the alkaline washing tower adopts 5-15 wt.% sodium hydroxide solution, and the flow is 150-400m 3 /h。
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202110908439.4A CN115246628B (en) | 2021-08-09 | 2021-08-09 | Purification method for synthesis gas at outlet of organic hazardous waste plasma gasification melting furnace |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202110908439.4A CN115246628B (en) | 2021-08-09 | 2021-08-09 | Purification method for synthesis gas at outlet of organic hazardous waste plasma gasification melting furnace |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN115246628A CN115246628A (en) | 2022-10-28 |
| CN115246628B true CN115246628B (en) | 2024-02-27 |
Family
ID=83696174
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202110908439.4A Active CN115246628B (en) | 2021-08-09 | 2021-08-09 | Purification method for synthesis gas at outlet of organic hazardous waste plasma gasification melting furnace |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN115246628B (en) |
Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101309857A (en) * | 2005-09-19 | 2008-11-19 | 乔治洛德方法研究和开发液化空气有限公司 | Method for producing synthetic gas using an oxygen-containing gas produced by at least one gas turbine |
| CN104093847A (en) * | 2011-11-28 | 2014-10-08 | 科斯卡塔公司 | Processes for the conversion of biomass to oxygenated organic compound, apparatus therefore and compositions produced thereby |
| CN105668517A (en) * | 2016-01-12 | 2016-06-15 | 华东理工大学 | Method for preparing synthetic gas from high temperature hydrocarbon-containing gas |
| WO2017121248A1 (en) * | 2016-01-12 | 2017-07-20 | 华东理工大学 | Partial oxidation process burner and use thereof |
| CN106987275A (en) * | 2017-05-02 | 2017-07-28 | 山东博润工业技术股份有限公司 | The high-temperature plasma gasification and melting processing system and method for trade waste |
| CN108097703A (en) * | 2017-12-22 | 2018-06-01 | 江苏天楹环保能源成套设备有限公司 | A kind of plasma gasification fusing system of solid waste centralized processing |
| CN111471489A (en) * | 2020-04-01 | 2020-07-31 | 华东理工大学 | Method and device for preparing synthesis gas from carbon-containing solid waste |
Family Cites Families (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101906325B (en) * | 2010-07-20 | 2013-09-04 | 阳光凯迪新能源集团有限公司 | Process and apparatus thereof for low-temperature cracking and high-temperature gasification of biomass |
-
2021
- 2021-08-09 CN CN202110908439.4A patent/CN115246628B/en active Active
Patent Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101309857A (en) * | 2005-09-19 | 2008-11-19 | 乔治洛德方法研究和开发液化空气有限公司 | Method for producing synthetic gas using an oxygen-containing gas produced by at least one gas turbine |
| CN104093847A (en) * | 2011-11-28 | 2014-10-08 | 科斯卡塔公司 | Processes for the conversion of biomass to oxygenated organic compound, apparatus therefore and compositions produced thereby |
| CN105668517A (en) * | 2016-01-12 | 2016-06-15 | 华东理工大学 | Method for preparing synthetic gas from high temperature hydrocarbon-containing gas |
| WO2017121248A1 (en) * | 2016-01-12 | 2017-07-20 | 华东理工大学 | Partial oxidation process burner and use thereof |
| CN106987275A (en) * | 2017-05-02 | 2017-07-28 | 山东博润工业技术股份有限公司 | The high-temperature plasma gasification and melting processing system and method for trade waste |
| CN108097703A (en) * | 2017-12-22 | 2018-06-01 | 江苏天楹环保能源成套设备有限公司 | A kind of plasma gasification fusing system of solid waste centralized processing |
| CN111471489A (en) * | 2020-04-01 | 2020-07-31 | 华东理工大学 | Method and device for preparing synthesis gas from carbon-containing solid waste |
Non-Patent Citations (2)
| Title |
|---|
| 等离子体处置危险废物及烟气净化系统工艺浅析;杨崇;广东化工;第47卷(第04期);第132、139页 * |
| 等离子气化技术处理危险废物工程应用;谢孟伟;曹莉萍;董坤;陈彤;资源节约与环保(第03期);第10-12、16页 * |
Also Published As
| Publication number | Publication date |
|---|---|
| CN115246628A (en) | 2022-10-28 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| JP5959665B2 (en) | Biomass gasification island method at high temperature and normal pressure | |
| RU2604624C2 (en) | Method and device for gasification of biomass by recycling carbon dioxide without oxygen | |
| CN102559266B (en) | Method for producing water gas by pure oxygen continuous gasification in fixed bed | |
| CN100579896C (en) | Method and system for preparing synthetic gas with appropriate hydrogen-carbon ratio from lurgi furnace outlet coal gas through non-catalytic partial oxidation by pure oxygen | |
| CN102146301A (en) | Method for two-stage coal gasification on composite external heat fixed bed and gas furnace | |
| CN102506435B (en) | Tail gas recovery method of device for manufacturing methanol and dimethyl ether by using tail gas of calcium carbide furnace and yellow phosphorus tail gas purified by using variable-temperature and variable-pressure adsorption method | |
| CN115246628B (en) | Purification method for synthesis gas at outlet of organic hazardous waste plasma gasification melting furnace | |
| CN102320568A (en) | Method and device for preparing synthetic gas or hydrogen with BGL pressuring slag gasification and pure oxygen non-catalytic partial oxidation | |
| CN202208705U (en) | Device for preparing synthesis gas or hydrogen through BGL pressurizing molten slag gasification with pure oxygen non-catalytic partial oxidation | |
| CN113969193B (en) | Heat energy recovery gasification metallurgy integrated process | |
| CN105779020B (en) | A kind of raw gas purifying and waste heat recycling system and method | |
| CN209923374U (en) | Production system for producing direct reduced iron by gas-based shaft furnace | |
| CN201386074Y (en) | Biomass gasifier | |
| CN114774611A (en) | Hydrogen rich gas CO2Method for producing iron by oxidation conversion and hydrogen-based shaft furnace direct reduction | |
| CN201102901Y (en) | System for preparing synthetic gas or hydrogen gas from lurgi-furnace outlet coal gas by non-catalysis and partial oxidation | |
| CN115245951B (en) | Method for improving thermal efficiency of treating hazardous waste by plasma gasification melting furnace | |
| CN202047043U (en) | Composite external heating two-section gas furnace with fixed bed | |
| CN110835544A (en) | Continuous and efficient waste tire gasification recycling treatment system and treatment method thereof | |
| CN109825659A (en) | A kind of technique and production system of gas-based shaft kiln production direct reduced iron | |
| CN219530876U (en) | Purifying coupling system for waste engine oil treatment and organic pyrolysis gas | |
| CN212316043U (en) | High-calorific-value solid waste gasification hydrogen production system | |
| CN214654697U (en) | Coal gasification device | |
| CN209872879U (en) | Dry coal powder quenching dry powder fuel gasification pyrolysis device | |
| CN210683700U (en) | Thermal power plant pyrolysis hydrogen production system | |
| CN109553508B (en) | Device and method for producing methanol by directly reforming raw coke oven gas with water vapor |
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 | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |