CN1644661A - Oven gas generation of plasma gasified coke oven - Google Patents
Oven gas generation of plasma gasified coke oven Download PDFInfo
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- 239000000571 coke Substances 0.000 title claims abstract description 28
- 239000007789 gas Substances 0.000 claims abstract description 71
- 238000000034 method Methods 0.000 claims abstract description 22
- 238000009272 plasma gasification Methods 0.000 claims abstract description 20
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 16
- 238000003786 synthesis reaction Methods 0.000 claims abstract description 10
- 230000015572 biosynthetic process Effects 0.000 claims abstract description 9
- 238000001816 cooling Methods 0.000 claims abstract description 3
- 239000003034 coal gas Substances 0.000 claims description 20
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 claims description 9
- 238000002309 gasification Methods 0.000 claims description 9
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims description 7
- 229910052760 oxygen Inorganic materials 0.000 claims description 7
- 239000000203 mixture Substances 0.000 claims description 6
- 239000002918 waste heat Substances 0.000 claims description 6
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 4
- 238000003763 carbonization Methods 0.000 claims description 4
- 239000003795 chemical substances by application Substances 0.000 claims description 4
- 239000001301 oxygen Substances 0.000 claims description 4
- 229910021529 ammonia Inorganic materials 0.000 claims description 3
- 229910052739 hydrogen Inorganic materials 0.000 claims description 3
- 229910052757 nitrogen Inorganic materials 0.000 claims description 3
- 230000003993 interaction Effects 0.000 claims description 2
- 230000000630 rising effect Effects 0.000 claims description 2
- 239000003054 catalyst Substances 0.000 abstract description 6
- 229910052799 carbon Inorganic materials 0.000 abstract description 5
- 239000000126 substance Substances 0.000 abstract description 5
- 239000003245 coal Substances 0.000 abstract description 4
- 208000008316 Arsenic Poisoning Diseases 0.000 abstract description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 abstract description 2
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 abstract description 2
- 238000004939 coking Methods 0.000 abstract description 2
- 238000003912 environmental pollution Methods 0.000 abstract description 2
- 239000002737 fuel gas Substances 0.000 abstract description 2
- 229910052736 halogen Inorganic materials 0.000 abstract description 2
- 150000002367 halogens Chemical class 0.000 abstract description 2
- 238000004519 manufacturing process Methods 0.000 abstract description 2
- 229910052717 sulfur Inorganic materials 0.000 abstract description 2
- 239000011593 sulfur Substances 0.000 abstract description 2
- 238000001556 precipitation Methods 0.000 abstract 1
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 6
- 239000011269 tar Substances 0.000 description 6
- 238000006243 chemical reaction Methods 0.000 description 4
- 229930195733 hydrocarbon Natural products 0.000 description 4
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 4
- 239000000498 cooling water Substances 0.000 description 3
- 239000002245 particle Substances 0.000 description 3
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical group O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 2
- LCGLNKUTAGEVQW-UHFFFAOYSA-N Dimethyl ether Chemical compound COC LCGLNKUTAGEVQW-UHFFFAOYSA-N 0.000 description 2
- 230000005540 biological transmission Effects 0.000 description 2
- 239000002994 raw material Substances 0.000 description 2
- 238000005406 washing Methods 0.000 description 2
- 239000002699 waste material Substances 0.000 description 2
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 description 1
- 208000005374 Poisoning Diseases 0.000 description 1
- UCKMPCXJQFINFW-UHFFFAOYSA-N Sulphide Chemical compound [S-2] UCKMPCXJQFINFW-UHFFFAOYSA-N 0.000 description 1
- 239000011282 acid tar Substances 0.000 description 1
- 230000004913 activation Effects 0.000 description 1
- 239000003570 air Substances 0.000 description 1
- 235000011114 ammonium hydroxide Nutrition 0.000 description 1
- 229910002092 carbon dioxide Inorganic materials 0.000 description 1
- 239000001569 carbon dioxide Substances 0.000 description 1
- 230000003197 catalytic effect Effects 0.000 description 1
- 239000002817 coal dust Substances 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 238000007796 conventional method Methods 0.000 description 1
- 239000000112 cooling gas Substances 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 230000008021 deposition Effects 0.000 description 1
- 238000006477 desulfuration reaction Methods 0.000 description 1
- 230000023556 desulfurization Effects 0.000 description 1
- 230000018109 developmental process Effects 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 230000005281 excited state Effects 0.000 description 1
- 150000002366 halogen compounds Chemical class 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 150000002430 hydrocarbons Chemical class 0.000 description 1
- 239000012774 insulation material Substances 0.000 description 1
- 150000002500 ions Chemical class 0.000 description 1
- 239000010808 liquid waste Substances 0.000 description 1
- 239000007800 oxidant agent Substances 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 231100000572 poisoning Toxicity 0.000 description 1
- 230000000607 poisoning effect Effects 0.000 description 1
- 239000000376 reactant Substances 0.000 description 1
- 238000002407 reforming Methods 0.000 description 1
- 230000008929 regeneration Effects 0.000 description 1
- 238000011069 regeneration method Methods 0.000 description 1
- 238000000629 steam reforming Methods 0.000 description 1
- 230000002194 synthesizing effect Effects 0.000 description 1
- 239000011273 tar residue Substances 0.000 description 1
- 239000002912 waste gas Substances 0.000 description 1
- 239000002351 wastewater Substances 0.000 description 1
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
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Abstract
本发明等离子体气化焦炉荒煤气的方法公开了一种高温炼焦荒煤气在等离子体辅助下制合成气的方法，其特征在于炼焦炉生成含有大量水蒸气、焦油蒸汽的荒煤气不经过冷却处理，直接进入等离子气化反应器与等离子发生器产生的等离子体相作用，生成以H2、CO为主的合成气、还原气、燃气。本发明适用于煤化工领域与等离子化工领域。该工艺流程短、方法操作简单、热效率高，环境污染小，同时克服了传统工艺需要催化剂，催化剂易发生析碳，硫、卤素、砷中毒的难题，为焦炉荒煤气综合利用开辟了新的途径。The method for plasma gasification of coke oven raw gas according to the invention discloses a method for producing synthesis gas from high-temperature coking raw gas under the assistance of plasma, which is characterized in that the coke oven generates raw gas containing a large amount of water vapor and tar vapor without cooling Treatment, directly enter the plasma gasification reactor and interact with the plasma generated by the plasma generator to generate synthesis gas, reducing gas and fuel gas mainly composed of H 2 and CO. The invention is applicable to the fields of coal chemical industry and plasma chemical industry. The process is short, the method is simple to operate, high thermal efficiency, and less environmental pollution. At the same time, it overcomes the traditional process that requires a catalyst, and the catalyst is prone to carbon precipitation, sulfur, halogen, and arsenic poisoning. It opens up a new way for the comprehensive utilization of coke oven raw gas way.
Description
技术领域technical field
本发明等离子体气化焦炉荒煤气的方法涉及一种炼焦荒煤气在等离子辅助下制以H2、CO为主的合成气、还原气、燃气的方法，属于煤化工及等离子化工范畴。The method for plasma gasifying raw coke oven gas of the present invention relates to a method for producing synthesis gas, reducing gas and fuel gas mainly composed of H 2 and CO under the assistance of plasma, which belongs to the category of coal chemical industry and plasma chemical industry.
技术背景technical background
处理焦炉荒煤气的常规方法是：650℃～850℃的荒煤气在桥管、集气管喷淋氨水冷却到80℃～85℃，在煤气初冷工段再冷却到25℃～35℃，其间荒煤气大量的显热和其中大量的水蒸汽、焦油蒸汽的潜热被白白浪费，同时还需要消耗大量的冷却水和氨，初冷后的煤气还要经过电捕焦油、除氨、脱萘、洗苯、脱硫等工序，得到的净化煤气才能作为原料生产合成气。在每一工段都有焦化废水产生，此外还有焦油渣、酸焦油和洗油再生残渣生成。大量能量被浪费的同时，造成很大环境污染。The conventional method to deal with raw coke oven gas is: 650℃～850℃ raw coal gas is sprayed with ammonia water in the bridge pipe and gas collecting pipe to cool down to 80℃～85℃, and then cooled to 25℃～35℃ in the initial gas cooling section. A large amount of sensible heat of raw gas and a large amount of latent heat of water vapor and tar vapor are wasted. At the same time, a large amount of cooling water and ammonia are consumed. After benzene washing, desulfurization and other processes, the purified gas obtained can be used as raw material to produce synthesis gas. In each section, coking wastewater is produced, in addition to tar residue, acid tar and washing oil regeneration residue. While a large amount of energy is wasted, it causes great environmental pollution.
我国今年焦炭产量将接近2亿吨，荒煤气产量将超过1000亿m3。仅山西省去年炼焦8000万吨，产生焦炉煤气约304亿立方米，是国家西气东输工程年输气量的2.53倍，够山西城乡居民燃用8年，但是焦炉煤气合理利用率仅为8.86％，其余的直接排放大量浪费，相当于每年损失约2000万吨煤，造成经济损失上百亿元。随着“西气东输”工程的进展，焦炉气将很快退出城市燃气领域，必将造成焦炉气的大量过剩，如何合理、有效地利用大量焦炉气，是解决资源浪费，环境污染，与社会经济发展密切相关的一个大课题。China's coke output will be close to 200 million tons this year, and raw gas output will exceed 100 billion m 3 . Shanxi Province alone made 80 million tons of coke last year, producing about 30.4 billion cubic meters of coke oven gas, which is 2.53 times the annual gas transmission volume of the national west-to-east gas transmission project, enough for urban and rural residents in Shanxi to burn for 8 years, but the reasonable utilization rate of coke oven gas It is only 8.86%, and the rest is directly discharged into a large amount of waste, which is equivalent to an annual loss of about 20 million tons of coal, causing economic losses of tens of billions of dollars. With the progress of the "West-to-East Gas Pipeline" project, coke oven gas will soon withdraw from the city gas field, which will inevitably cause a large surplus of coke oven gas. How to use a large amount of coke oven gas rationally and effectively is a solution to waste of resources and the environment. Pollution is a major issue closely related to social and economic development.
目前，以焦炉煤气为原料生产合成气来合成氨、甲醇、二甲醚被认为是一条很好的出路。由焦炉煤气生产合成气的路线大致有三条，一是部分氧化工艺，二是水蒸汽重整，三是二氧化碳重整，三条工艺路线都需要催化系统。不管哪一条线路都需要将荒煤气净化，使净化后煤气中硫化物、卤素化合物、焦油等降至相等低的水平。以防止催化剂发生析碳，硫、卤素、砷中毒。净焦炉煤气合成气合成甲醇f＝(H2-CO)/(CO+CO2)高于合成甲醇的理想条件为f＝2.10，荒煤气中焦油蒸气和低碳烃在等离子作用下可转化为CO可得到合理的f值。此外，无论那种工艺均存在工艺流程长，设备投资大，操作费用高、能量利用效率低的缺点。At present, using coke oven gas as raw material to produce synthetic gas to synthesize ammonia, methanol and dimethyl ether is considered to be a good way out. There are roughly three routes for producing synthesis gas from coke oven gas, one is partial oxidation process, the other is steam reforming, and the third is carbon dioxide reforming, all of which require catalytic systems. No matter which line it is necessary to purify the raw gas, so that the sulfide, halogen compound, tar, etc. in the purified gas can be reduced to a very low level. To prevent the catalyst from carbonization, sulfur, halogen, and arsenic poisoning. The ideal condition for synthesizing methanol from clean coke oven gas syngas f=(H 2 -CO)/(CO+CO 2 ) is higher than f=2.10, and tar vapor and low-carbon hydrocarbons in raw coal gas can be converted under the action of plasma A reasonable f value can be obtained for CO. In addition, no matter what kind of process, there are disadvantages such as long process flow, large equipment investment, high operating cost and low energy utilization efficiency.
本发明等离子体气化焦炉荒煤气的方法，不仅可以利用直接利用650℃～850℃的荒煤气的显热和其中蒸汽潜热，而且富含大量高能量的活性粒子(离子、电子、原子、激发态的分子等)参与化学反应，可以获得化学燃烧更高的温度、加热速率和气化速率，生成CO/H2比合适的合成气。因此本发明具有能量集中、气化速率快、气化强度高、流程短、设备紧凑、易于实现高度自动化、且污染小、没有液体废物产生，不需要催化剂，常压操作等特点。The method for plasma gasifying coke oven raw gas of the present invention not only can directly utilize the sensible heat of raw coal gas at 650°C to 850°C and the latent heat of steam therein, but also is rich in a large number of high-energy active particles (ions, electrons, atoms, Molecules in the excited state, etc.) participate in the chemical reaction, which can obtain higher temperature, heating rate and gasification rate of chemical combustion, and generate syngas with appropriate CO/ H2 ratio. Therefore, the present invention has the characteristics of concentrated energy, fast gasification rate, high gasification intensity, short process, compact equipment, high automation, low pollution, no liquid waste, no catalyst, and normal pressure operation.
发明内容Contents of the invention
本发明等离子体气化焦炉荒煤气的方法的目的在于克服现有技术的不足，提高焦炉煤气的能量利用效率，解决现有煤制合成气技术需要高压、催化剂且催化剂易积碳、中毒等问题。公开了一种利用等离子体将荒煤气高效、洁净、方便地转化为合成气的方法。The purpose of the method for plasma gasifying coke oven raw gas of the present invention is to overcome the deficiencies of the prior art, improve the energy utilization efficiency of coke oven gas, and solve the problem that the existing coal-to-synthesis gas technology needs high pressure, catalyst and the catalyst is prone to carbon deposition and poisoning And other issues. Disclosed is a method for efficiently, cleanly and conveniently converting raw coal gas into synthesis gas by using plasma.
由炼焦炉炭化室炉顶空间经上升管出来的荒煤气主要组成(质量百分比)为：焦油蒸汽9％～14％、水蒸汽30％～36％、粗苯2.5％～4.3％、氨气0.7％～1.1％，H24％～10％、CH4 17％～31％、CO7％～12％、N21％～10％、CO22％～7％。The main composition (mass percentage) of the raw coal gas coming out of the top space of the carbonization chamber of the coke oven through the riser is: tar vapor 9%-14%, water vapor 30%-36%, crude benzene 2.5%-4.3%, ammonia gas 0.7% %~1.1%, H 2 4%~10%, CH 4 17%~31%, CO 7%~12%, N 2 1%~10%, CO 2 2%~7%.
从中可以看出荒煤气中含有大量的水蒸汽，从热力学的角度分析，650～850℃荒煤气中的水蒸汽和甲烷、低碳烃、焦油蒸汽具有生成较高浓度合成气的能力；从动力学的角度说，反应速率很慢。水蒸汽和甲烷、低碳烃、焦油蒸汽在富含活性粒子的等离子体作用下，和水蒸气等含氧气化剂反应的活化能大幅度降低，气化反应以极快的速率进行，生成高浓度的H2、CO。It can be seen that raw coal gas contains a large amount of water vapor. From a thermodynamic point of view, water vapor, methane, low-carbon hydrocarbons, and tar steam in raw coal gas at 650-850 °C have the ability to generate relatively high-concentration syngas; From a scientific point of view, the reaction rate is very slow. Under the action of plasma rich in active particles, the activation energy of water vapor, methane, low-carbon hydrocarbons, and tar vapor reacting with oxygen-containing oxidizing agents such as water vapor is greatly reduced, and the gasification reaction proceeds at an extremely fast rate, generating high concentration of H 2 , CO.
基于以上思路，荒煤气经上升管、桥管、集气管进入等离子气化反应器。等离子发生器采用空气、氧气、氮气、水蒸汽等气体或它们的混合气体作为工作气体，也可以将荒煤气直接作为工作气体，工作时首先向等离子发生器及等离子气化反应器内供入冷却水、工作气体、气化剂(水蒸汽、含氧气体)和荒煤气，等离子发生器的工作气体是H2、Ar、O2、N2、空气等气体及其混合气，或只供荒煤气和冷却水，然后点燃电弧，便形成了具有高能活性粒子的高温等离子体，荒煤气中的成分和等离子体作用，在等离子气化反应器内被活化，在常压下瞬间反应气化生成H2、CO。同时气体温度上升到1500℃以上，合成气热量由废热锅炉回收。Based on the above ideas, raw coal gas enters the plasma gasification reactor through the riser pipe, bridge pipe, and gas collecting pipe. The plasma generator uses air, oxygen, nitrogen, water vapor and other gases or their mixed gases as the working gas, and raw coal gas can also be directly used as the working gas. When working, the cooling gas is first supplied to the plasma generator and the plasma gasification reactor. Water, working gas, gasification agent (water vapor, oxygen-containing gas) and raw coal gas, the working gas of the plasma generator is H 2 , Ar, O 2 , N 2 , air and other gases and their mixtures, or only for waste gas Coal gas and cooling water, and then ignite the arc to form a high-temperature plasma with high-energy active particles. The components in the raw coal gas and the plasma action are activated in the plasma gasification reactor, and they react and gasify instantly under normal pressure. H2 , CO. At the same time, the gas temperature rises above 1500°C, and the heat of the syngas is recovered by the waste heat boiler.
上述等离子发生器产生的等离子体为电弧等离子体。The plasma generated by the above-mentioned plasma generator is arc plasma.
上述等离子体是移动型电弧等离子体或非移动型电弧等离子体。The aforementioned plasma is moving arc plasma or non-moving arc plasma.
上述等离子体是直流电弧等离子体或交流电弧等离子体。。The aforementioned plasma is DC arc plasma or AC arc plasma. .
上述等离子发生器的工作气体是H2、Ar、O2、N2、空气等气体及其混合气。The working gas of the above plasma generator is H 2 , Ar, O 2 , N 2 , air and other gases and their mixtures.
具体实施方式Detailed ways
实施方式1Embodiment 1
将压缩空气和冷却水送至等离子发生器，启动等离子发生器点燃电弧，荒煤气由炭化室经上升管、桥管、集气管(管路外覆保温材料)进入等离子气化反应器，荒煤气中的碳氢化合物、装煤过程进入上升管的煤尘及水蒸气与空气等离子体接触活化，快速反应生成CO、H2，及少量的N2、CO2等气体的混合物。混合气体温度在1500℃，然后进入废热锅炉回收热量，产生的高压蒸气，一部分供给工厂动力系统使用，一部分也可以进入等离子气化系统作为气化剂使用。Send compressed air and cooling water to the plasma generator, start the plasma generator to ignite the arc, and the raw coal gas enters the plasma gasification reactor from the carbonization chamber through the rising pipe, bridge pipe, and gas collection pipe (pipelines are covered with insulation materials), and the raw coal gas The hydrocarbons in the gas, the coal dust and water vapor entering the riser during the coal charging process are activated by contact with the air plasma, and quickly react to generate CO, H 2 , and a small amount of N 2 , CO 2 and other gas mixtures. The temperature of the mixed gas is 1500°C, and then enters the waste heat boiler to recover heat, and the high-pressure steam generated is partly supplied to the power system of the factory, and part of it can also enter the plasma gasification system as a gasification agent.
实施方式2Embodiment 2
荒煤气经过一系列管路沿反应器切线进入等离子气化反应器，同时沿反应器切线方向通入高压蒸气(废热锅炉产生)，然后点燃等离子电弧，在等离子气化反应器外部放置一个电磁线圈，对等离子电弧压缩和控制，使等离子电弧以一定频率以气流同方向旋转。其加强了等离子体与反应物的作用，加快了反应速率，生成了高质量的合成气。2500℃的合成气进入废热锅炉，产生高压水蒸气，供给工厂动力系统使用。一部分也可以进入等离子气化系统作为气化剂使用。Raw coal gas enters the plasma gasification reactor through a series of pipelines along the tangent of the reactor, and at the same time, high-pressure steam (produced by the waste heat boiler) is introduced along the tangential direction of the reactor, and then the plasma arc is ignited, and an electromagnetic coil is placed outside the plasma gasification reactor , to compress and control the plasma arc, so that the plasma arc rotates in the same direction as the airflow at a certain frequency. It strengthens the interaction between plasma and reactants, accelerates the reaction rate, and generates high-quality synthesis gas. Syngas at 2500°C enters the waste heat boiler to generate high-pressure steam, which is supplied to the power system of the factory. Part of it can also enter the plasma gasification system and be used as a gasification agent.
Claims (7)
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| CNB2004100924203A CN1262627C (en) | 2004-12-16 | 2004-12-16 | Oven gas generation of plasma gasified coke oven |
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| CNB2004100924203A CN1262627C (en) | 2004-12-16 | 2004-12-16 | Oven gas generation of plasma gasified coke oven |
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| CN1262627C CN1262627C (en) | 2006-07-05 |
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| Application Number | Title | Priority Date | Filing Date |
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| CNB2004100924203A Expired - Fee Related CN1262627C (en) | 2004-12-16 | 2004-12-16 | Oven gas generation of plasma gasified coke oven |
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Cited By (13)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US8070863B2 (en) | 2006-05-05 | 2011-12-06 | Plasco Energy Group Inc. | Gas conditioning system |
| US8128728B2 (en) | 2006-05-05 | 2012-03-06 | Plasco Energy Group, Inc. | Gas homogenization system |
| US8306665B2 (en) | 2006-05-05 | 2012-11-06 | Plasco Energy Group Inc. | Control system for the conversion of carbonaceous feedstock into gas |
| US8372169B2 (en) | 2006-05-05 | 2013-02-12 | Plasco Energy Group Inc. | Low temperature gasification facility with a horizontally oriented gasifier |
| US8435315B2 (en) | 2006-05-05 | 2013-05-07 | Plasco Energy Group Inc. | Horizontally-oriented gasifier with lateral transfer system |
| US8475551B2 (en) | 2006-05-05 | 2013-07-02 | Plasco Energy Group Inc. | Gas reformulating system using plasma torch heat |
| US8690975B2 (en) | 2007-02-27 | 2014-04-08 | Plasco Energy Group Inc. | Gasification system with processed feedstock/char conversion and gas reformulation |
| CN104629779A (en) * | 2014-12-12 | 2015-05-20 | 中山大学 | Process for producing synthetic gas from urban garbage by virtue of combination of pyrolysis and plasma |
| US9321640B2 (en) | 2010-10-29 | 2016-04-26 | Plasco Energy Group Inc. | Gasification system with processed feedstock/char conversion and gas reformulation |
| WO2018072865A1 (en) * | 2016-10-18 | 2018-04-26 | Linde Aktiengesellschaft | Method and installation for obtaining hydrogen |
| CN109485016A (en) * | 2019-01-17 | 2019-03-19 | 河北科技大学 | A kind of system and method for the direct steam reformation hydrogen making of coal oven dithio-gas or ammonia |
| CN109553508A (en) * | 2019-01-17 | 2019-04-02 | 河北科技大学 | A kind of device and method of the direct steam reformation production methanol of coal oven dithio-gas |
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2004
- 2004-12-16 CN CNB2004100924203A patent/CN1262627C/en not_active Expired - Fee Related
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| US9109172B2 (en) | 2006-05-05 | 2015-08-18 | Plasco Energy Group Inc. | Low temperature gasification facility with a horizontally oriented gasifier |
| US8306665B2 (en) | 2006-05-05 | 2012-11-06 | Plasco Energy Group Inc. | Control system for the conversion of carbonaceous feedstock into gas |
| US8372169B2 (en) | 2006-05-05 | 2013-02-12 | Plasco Energy Group Inc. | Low temperature gasification facility with a horizontally oriented gasifier |
| US8435315B2 (en) | 2006-05-05 | 2013-05-07 | Plasco Energy Group Inc. | Horizontally-oriented gasifier with lateral transfer system |
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| US8070863B2 (en) | 2006-05-05 | 2011-12-06 | Plasco Energy Group Inc. | Gas conditioning system |
| US8690975B2 (en) | 2007-02-27 | 2014-04-08 | Plasco Energy Group Inc. | Gasification system with processed feedstock/char conversion and gas reformulation |
| US9321640B2 (en) | 2010-10-29 | 2016-04-26 | Plasco Energy Group Inc. | Gasification system with processed feedstock/char conversion and gas reformulation |
| CN104629779A (en) * | 2014-12-12 | 2015-05-20 | 中山大学 | Process for producing synthetic gas from urban garbage by virtue of combination of pyrolysis and plasma |
| WO2018072865A1 (en) * | 2016-10-18 | 2018-04-26 | Linde Aktiengesellschaft | Method and installation for obtaining hydrogen |
| CN109843791A (en) * | 2016-10-18 | 2019-06-04 | 林德股份公司 | Method and apparatus for obtaining hydrogen |
| RU2739072C2 (en) * | 2016-10-18 | 2020-12-21 | Линде Акциенгезельшафт | Method and apparatus for producing hydrogen |
| US11298648B2 (en) | 2016-10-18 | 2022-04-12 | Linde Aktiengesellschaft | Method and installation for obtaining hydrogen |
| CN109485016A (en) * | 2019-01-17 | 2019-03-19 | 河北科技大学 | A kind of system and method for the direct steam reformation hydrogen making of coal oven dithio-gas or ammonia |
| CN109553508A (en) * | 2019-01-17 | 2019-04-02 | 河北科技大学 | A kind of device and method of the direct steam reformation production methanol of coal oven dithio-gas |
| CN109553508B (en) * | 2019-01-17 | 2024-03-29 | 河北科技大学 | Device and method for producing methanol by directly reforming raw coke oven gas with water vapor |
| CN115044718A (en) * | 2022-06-10 | 2022-09-13 | 中钢设备有限公司 | Method and device for heating coal gas by plasma torch and application |
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| Publication number | Publication date |
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| CN1262627C (en) | 2006-07-05 |
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