CN203159209U - Carbon dioxide-methane self-heating reforming reactor - Google Patents
Carbon dioxide-methane self-heating reforming reactor Download PDFInfo
- Publication number
- CN203159209U CN203159209U CN2013200237963U CN201320023796U CN203159209U CN 203159209 U CN203159209 U CN 203159209U CN 2013200237963 U CN2013200237963 U CN 2013200237963U CN 201320023796 U CN201320023796 U CN 201320023796U CN 203159209 U CN203159209 U CN 203159209U
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- reforming reactor
- reactor according
- methane
- burner
- mixing tank
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- OWQNOTOYTSUHNE-UHFFFAOYSA-N carbon dioxide methane Chemical compound C.C(=O)=O.C OWQNOTOYTSUHNE-UHFFFAOYSA-N 0.000 title claims abstract description 17
- 238000002407 reforming Methods 0.000 title claims abstract description 15
- 238000010438 heat treatment Methods 0.000 title abstract description 3
- 238000006243 chemical reaction Methods 0.000 claims abstract description 25
- 238000002485 combustion reaction Methods 0.000 claims abstract description 18
- 238000006555 catalytic reaction Methods 0.000 claims abstract description 13
- 238000002156 mixing Methods 0.000 claims description 16
- 238000002453 autothermal reforming Methods 0.000 claims description 12
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 12
- 238000001816 cooling Methods 0.000 claims description 5
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 abstract description 45
- 239000007789 gas Substances 0.000 abstract description 33
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 abstract description 9
- 229910052760 oxygen Inorganic materials 0.000 abstract description 9
- 239000001301 oxygen Substances 0.000 abstract description 9
- 238000000034 method Methods 0.000 abstract description 6
- 238000006057 reforming reaction Methods 0.000 abstract description 5
- 230000003647 oxidation Effects 0.000 abstract description 2
- 238000007254 oxidation reaction Methods 0.000 abstract description 2
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 5
- 235000011089 carbon dioxide Nutrition 0.000 description 5
- 239000000126 substance Substances 0.000 description 5
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 4
- 229910052799 carbon Inorganic materials 0.000 description 4
- 238000010586 diagram Methods 0.000 description 4
- 238000005516 engineering process Methods 0.000 description 4
- 238000000629 steam reforming Methods 0.000 description 4
- 230000009466 transformation Effects 0.000 description 4
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 3
- 230000003197 catalytic effect Effects 0.000 description 3
- 238000007599 discharging Methods 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 239000005431 greenhouse gas Substances 0.000 description 3
- 230000008901 benefit Effects 0.000 description 2
- 239000003245 coal Substances 0.000 description 2
- 238000009826 distribution Methods 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 238000002360 preparation method Methods 0.000 description 2
- 239000007921 spray Substances 0.000 description 2
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 description 1
- 238000010521 absorption reaction Methods 0.000 description 1
- 238000004458 analytical method Methods 0.000 description 1
- 230000000712 assembly Effects 0.000 description 1
- 238000000429 assembly Methods 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000002146 bilateral effect Effects 0.000 description 1
- KDRIEERWEFJUSB-UHFFFAOYSA-N carbon dioxide;methane Chemical compound C.O=C=O KDRIEERWEFJUSB-UHFFFAOYSA-N 0.000 description 1
- 239000003610 charcoal Substances 0.000 description 1
- 239000000571 coke Substances 0.000 description 1
- 235000009508 confectionery Nutrition 0.000 description 1
- 208000012839 conversion disease Diseases 0.000 description 1
- 239000002826 coolant Substances 0.000 description 1
- 235000019628 coolness Nutrition 0.000 description 1
- 230000002950 deficient Effects 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 238000002309 gasification Methods 0.000 description 1
- 230000002779 inactivation Effects 0.000 description 1
- 239000003317 industrial substance Substances 0.000 description 1
- CSJDCSCTVDEHRN-UHFFFAOYSA-N methane;molecular oxygen Chemical compound C.O=O CSJDCSCTVDEHRN-UHFFFAOYSA-N 0.000 description 1
- 239000003345 natural gas Substances 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 238000005096 rolling process Methods 0.000 description 1
- 230000000930 thermomechanical effect Effects 0.000 description 1
Images
Classifications
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- 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
- C01B3/38—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 catalysts
- C01B3/382—Multi-step processes
-
- 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
- C01B2203/02—Processes for making hydrogen or synthesis gas
- C01B2203/0205—Processes for making hydrogen or synthesis gas containing a reforming step
- C01B2203/0227—Processes for making hydrogen or synthesis gas containing a reforming step containing a catalytic reforming step
- C01B2203/0238—Processes for making hydrogen or synthesis gas containing a reforming step containing a catalytic reforming step the reforming step being a carbon dioxide reforming step
-
- 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
- C01B2203/02—Processes for making hydrogen or synthesis gas
- C01B2203/0205—Processes for making hydrogen or synthesis gas containing a reforming step
- C01B2203/0227—Processes for making hydrogen or synthesis gas containing a reforming step containing a catalytic reforming step
- C01B2203/0244—Processes for making hydrogen or synthesis gas containing a reforming step containing a catalytic reforming step the reforming step being an autothermal reforming step, e.g. secondary reforming processes
-
- 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
- C01B2203/02—Processes for making hydrogen or synthesis gas
- C01B2203/025—Processes for making hydrogen or synthesis gas containing a partial oxidation step
- C01B2203/0255—Processes for making hydrogen or synthesis gas containing a partial oxidation step containing a non-catalytic partial oxidation step
-
- 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
- C01B2203/10—Catalysts for performing the hydrogen forming reactions
- C01B2203/1041—Composition of the catalyst
- C01B2203/1047—Group VIII metal catalysts
- C01B2203/1052—Nickel or cobalt catalysts
- C01B2203/1058—Nickel catalysts
-
- 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
- C01B2203/12—Feeding the process for making hydrogen or synthesis gas
- C01B2203/1205—Composition of the feed
- C01B2203/1211—Organic compounds or organic mixtures used in the process for making hydrogen or synthesis gas
- C01B2203/1235—Hydrocarbons
- C01B2203/1241—Natural gas or methane
-
- 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
- C01B2203/12—Feeding the process for making hydrogen or synthesis gas
- C01B2203/1276—Mixing of different feed components
- C01B2203/1282—Mixing of different feed components using static mixers
-
- 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
- C01B2203/14—Details of the flowsheet
- C01B2203/142—At least two reforming, decomposition or partial oxidation steps in series
-
- 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
- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/52—Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts
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- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Organic Chemistry (AREA)
- Health & Medical Sciences (AREA)
- General Health & Medical Sciences (AREA)
- Engineering & Computer Science (AREA)
- Combustion & Propulsion (AREA)
- Inorganic Chemistry (AREA)
- Hydrogen, Water And Hydrids (AREA)
Abstract
The utility model discloses a carbon dioxide-methane self-heating reforming reactor which comprises a furnace body, a burner, a gas distributor, a mixer, a combustion chamber, a catalytic reaction bed and a gas collection chamber, wherein the burner is inserted into the mixer through the top of the furnace body; the gas distributor is arranged in front of the end part of the burner; and the mixer, the combustion chamber, the catalytic reaction bed and the gas collection chamber are sequentially arranged inside the furnace body from top to bottom. The reforming reactor realizes the self heat supply in carbon dioxide-methane reforming reaction by using heat generated in the oxidation process of oxygen and methane, thus lowering the investment and operating cost, and improving the methane conversion efficiency.
Description
Technical field
The utility model relates to carbon one chemical field, particularly relates to a kind of carbon dioxide-methane autothermal reforming reaction device.
Background technology
Fossil energy worsening shortages and environmental pollution seriously are the two big crisis difficult problems that the world today faces, and Greenhouse effect make people's growing interest CO to having a strong impact on of climatope
2The reduction of discharging problem is with CO
2Transforming the preparation synthetic gas as carbon oxygen resource through high-temperature catalytic is CO
2Extensive chemical utilization give priority to direction.With CO
2Be raw material, can realize CO with the methane of Coal Chemical Industry, the discharging of gas utilization process by the conversion preparation synthetic gas process of reforming
2And CH
4Efficiently utilize in the time of two kinds of greenhouse gases, and reduced discharging greenhouse gases, realized the carbon resource recycle of energy chemical, have huge economic benefit, so CH
4-CO
2Reforming reaction is considered to the core technology that following Coal Chemical Industry carbon resource effectively utilizes.
Methane and the industrialized example of CO 2 reformation preparing synthetic gas are not arranged at present as yet, and its emphasis and difficult point mainly are to lack catalyzer and safe and reliable, easy to operate, the reactor assemblies reasonable in design such as the start-stop car flexible, long service life that are difficult for carbon distribution, are difficult for stopping up, being difficult for excellent performances such as inactivation, transformation efficiency height, good stability.According to " thermodynamics of gasification and gas building-up reactions " (work such as [Soviet Union] pressgang Lip river husband, Wu Yueyi) heating power in the book calculates as can be known, the methane carbon dioxide reformation reaction is a strong endothermic reaction, from the thermomechanical analysis process, temperature is up to synthetic gas production is just arranged more than 600 ℃, raise with temperature of reaction, reaction conversion ratio increases, the synthetic gas gain in yield.Like this source of heat under the hot conditions also is one of the emphasis of technological process and difficult point.
Present pure oxygen converter both domestic and external all is the converter (being also referred to as secondary reformer) at methane and steam reforming reaction, does not appear in the newspapers and use at the converter of carbonic acid gas and methane reforming reaction.
Present methane and the converter of steam reforming reaction have following defective:
1. transformation efficiency is low, and 30%～90% methane conversion need rely on the primary reformer that the secondary reformer leading portion arranges.
2. methane and steam reforming stove all need to replenish a large amount of water vapour, except the needs that satisfy methane and steam reforming reaction, also need the extra water vapour charcoal that disappears, increased running cost, also increased running cost for follow-up water vapour separates, and only be not the converter that methane and CO 2 reformation do not need the make up water steam.
3. in traditional secondary reformer, methane and oxygen is as easy as rolling off a log to be mixed inhomogeneously, causes oxygen not to be exhausted at burning zone, enters that the catalyzer to catalytic section damages after the catalytic section.
The utility model content
The technical problems to be solved in the utility model provides a kind of carbon dioxide-methane autothermal reforming reaction device, and it can improve the transformation efficiency of methane, and can reduce production costs.
For solving the problems of the technologies described above, carbon dioxide-methane autothermal reforming reaction device of the present utility model mainly comprises body of heater, burner, gas distributor, mixing tank, combustion chamber, catalyzed reaction bed and collection chamber; Described burner inserts mixing tank by the body of heater top; Before described gas distributor is arranged on the burner end; Described mixing tank, combustion chamber, catalyzed reaction bed and collection chamber are arranged on body of heater inside successively from top to bottom.
Preferable, this carbon dioxide-methane autothermal reforming reaction device can also arrange cooling system, for example water jacket in place, burner end outside body of heater.
The described catalyzed reaction bed outside and collection chamber outlet can be installed a plurality of temperature elements, for example thermocouple thermometer.
Compare with secondary reformer, carbon dioxide-methane autothermal reforming reaction device of the present utility model has the following advantages and beneficial effect:
1. be at carbonic acid gas and methane reforming reaction and the reactor apparatus that designs, " greenhouse gases " carbonic acid gas can be transformed into industrial chemicals and the energy with added value, and can not add water vapour or add a spot of water vapour according to arts demand.
2. utilize the heat that produces in oxygen and the methane oxidation process to realize the heat supply certainly of strong heat absorption reforming reaction under the hot conditions, do not need additionally to provide outside heat.
3. adopting single reaction vessel can be 0.1～2% synthetic gas with methane conversion to methane content, transformation efficiency height not only, and can reduce and invest and running cost.
4. adopted mixing tank, gas distributor and combustion chamber, and the combustion chamber has enough spaces, make the oxygen can be in the combustion chamber internal combustion totally, and beds ingress gas distribution be even.
Description of drawings
Fig. 1 is carbon dioxide-methane autothermal reforming reaction apparatus synoptic diagram of the present utility model.
Fig. 2 is gas distributor synoptic diagram in the carbon dioxide-methane autothermal reforming reaction device of the present utility model.
Fig. 3 is unstripped gas single passage synoptic diagram in the carbon dioxide-methane autothermal reforming reaction device of the present utility model.
Fig. 4 is unstripped gas two channels synoptic diagram in the carbon dioxide-methane autothermal reforming reaction device of the present utility model.
Description of reference numerals is as follows among the figure:
1: body of heater
2: gas distributor
3: refractory liner
4: water jacket
5: mixing tank
6: the combustion chamber
7: the catalyzed reaction bed
8: collection chamber
9,10: thermocouple thermometer
11: burner
Embodiment
Understand for technology contents of the present utility model, characteristics and effect being had more specifically, existing in conjunction with illustrated embodiment, details are as follows:
As shown in Figure 1, the carbon dioxide-methane autothermal reforming reaction device of present embodiment comprises body of heater 1, gas distributor 2, refractory liner 3, water jacket 4, mixing tank 5, combustion chamber 6, catalyzed reaction bed 7, collection chamber 8, a plurality of thermocouple thermometer 9,10 and burner 11.Wherein:
Gas distributor 2 is rounded, be arranged on the end of burner 11 before, anisotropically offer a plurality of manholes on the gas distributor 2, these holes are coaxial circular permutation, and interior ring perforate density is greater than outer shroud perforate density, as shown in Figure 2.
Refractory liner 3 is filled in the inwall of body of heater 1.
Water jacket 4 is coated on outside the body of heater 1.Because oxygen and methyl hydride combustion can produce high temperature, therefore, a forced convection cooling system need be set in burner 11 ends, give burner 11 coolings with the water coolant of the burner 11 of flowing through.
When carrying out the reforming carbon dioxide-methane reaction, oxygen enters burner 11 from oxygen channel, flows to the end of burner 11 vertically; The unstripped gas that is rich in carbonic acid gas and methane (can be the gas that is rich in methane, also can be the gas that is rich in methane and carbonic acid gas simultaneously, any that for example Sweet natural gas, coke(oven)gas, oil field gas, refinery gas, coal-seam gas, methyl alcohol syntheticly speed to exit, Fischer-Tropsch is synthetic in speeding to exit or several combinations.) then (can adopt one-sided or the air inlet of bilateral tangent line along the direction perpendicular to mixing tank 5 top tangent lines, shown in Fig. 3,4) enter gas distributor 2, the high speed oxygen that sprays with average flow velocity and burner 11 ends evenly mixes in elongated mixing tank 5, and in the instantaneous generation combustion reactions that mixes, spray the into top of conical combustor 6 by a single hole then.
Unstripped gas after the burning 6 enters beds 7 from the combustion chamber, under the effect of Ni-Ca-Zr catalyzer, carries out the reforming carbon dioxide-methane reaction, and reaction velocity is 1000～50000h
-1, preferred 5000～20000h
-1The synthetic gas that the reaction back produces enters collection chamber 8, flows out from the outlet of collection chamber 8, and its methane content is 0.1～2%.
Claims (10)
1. carbon dioxide-methane autothermal reforming reaction device is characterized in that, comprises body of heater, burner, gas distributor, mixing tank, combustion chamber, catalyzed reaction bed and collection chamber; Described burner inserts mixing tank by the body of heater top; Before described gas distributor is arranged on the burner end; Described mixing tank, combustion chamber, catalyzed reaction bed and collection chamber are arranged on body of heater inside successively from top to bottom.
2. reforming reactor according to claim 1 is characterized in that, described inboard wall of furnace body is filled with refractory liner.
3. reforming reactor according to claim 1 is characterized in that, also includes cooling system, is installed in place, the outer burner end of body of heater.
4. reforming reactor according to claim 3 is characterized in that, described cooling system is water jacket.
5. reforming reactor according to claim 1 is characterized in that, described gas distributor is rounded, and anisotropically offers a plurality of through holes.
6. reforming reactor according to claim 5 is characterized in that, the through hole on the gas distributor is coaxial circular permutation, and interior ring perforate density is greater than outer shroud perforate density.
7. reforming reactor according to claim 1 is characterized in that, the aspect ratio of described mixing tank is 2～3.
8. reforming reactor according to claim 1 is characterized in that, described combustion chamber is tapered, highly is 3～5 times of mixing tank diameter.
9. reforming reactor according to claim 1 is characterized in that, filling Ni-Ca-Zr catalyzer in the described catalyzed reaction bed.
10. reforming reactor according to claim 1 is characterized in that, the described catalyzed reaction bed outside and collection chamber outlet installing temperature element.
Priority Applications (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2013200237963U CN203159209U (en) | 2013-01-17 | 2013-01-17 | Carbon dioxide-methane self-heating reforming reactor |
| PCT/EP2014/050396 WO2014111315A1 (en) | 2013-01-17 | 2014-01-10 | Auto-thermal reforming reactor |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2013200237963U CN203159209U (en) | 2013-01-17 | 2013-01-17 | Carbon dioxide-methane self-heating reforming reactor |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN203159209U true CN203159209U (en) | 2013-08-28 |
Family
ID=49020412
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2013200237963U Expired - Lifetime CN203159209U (en) | 2013-01-17 | 2013-01-17 | Carbon dioxide-methane self-heating reforming reactor |
Country Status (2)
| Country | Link |
|---|---|
| CN (1) | CN203159209U (en) |
| WO (1) | WO2014111315A1 (en) |
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104525054A (en) * | 2014-12-26 | 2015-04-22 | 北京神雾环境能源科技集团股份有限公司 | Oxygen feeding device, and corresponding methane tri-reforming reaction device and method |
| CN107243265A (en) * | 2017-07-25 | 2017-10-13 | 天津阿奇森环保技术有限公司 | A kind of ammonia blender |
| CN111137860A (en) * | 2019-12-31 | 2020-05-12 | 太原理工大学 | Methane carbon dioxide dry reforming reaction furnace |
| CN111871336A (en) * | 2020-08-21 | 2020-11-03 | 中国海洋石油集团有限公司 | Low-carbon alkane reforming reaction device and synthesis gas equipment |
| CN113795330A (en) * | 2019-04-23 | 2021-12-14 | 托普索公司 | High temperature reactor vessel, apparatus and method |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US10370298B2 (en) * | 2017-04-10 | 2019-08-06 | O'brien Asset Management, Llc | Target tiles for an autothermal reformation/secondary reformation unit |
Family Cites Families (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP1531147A1 (en) * | 2003-11-06 | 2005-05-18 | CASALE ChEMICALS S.A. | Catalytic secondary reforming process and reactor for said process |
| GB201105131D0 (en) * | 2011-03-28 | 2011-05-11 | Johnson Matthey Plc | Steam reforming |
-
2013
- 2013-01-17 CN CN2013200237963U patent/CN203159209U/en not_active Expired - Lifetime
-
2014
- 2014-01-10 WO PCT/EP2014/050396 patent/WO2014111315A1/en active Application Filing
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104525054A (en) * | 2014-12-26 | 2015-04-22 | 北京神雾环境能源科技集团股份有限公司 | Oxygen feeding device, and corresponding methane tri-reforming reaction device and method |
| CN107243265A (en) * | 2017-07-25 | 2017-10-13 | 天津阿奇森环保技术有限公司 | A kind of ammonia blender |
| CN107243265B (en) * | 2017-07-25 | 2023-08-01 | 天津阿奇森环保技术有限公司 | Ammonia mixer |
| CN113795330A (en) * | 2019-04-23 | 2021-12-14 | 托普索公司 | High temperature reactor vessel, apparatus and method |
| CN111137860A (en) * | 2019-12-31 | 2020-05-12 | 太原理工大学 | Methane carbon dioxide dry reforming reaction furnace |
| CN111137860B (en) * | 2019-12-31 | 2023-03-10 | 太原理工大学 | Methane carbon dioxide dry reforming reaction furnace |
| CN111871336A (en) * | 2020-08-21 | 2020-11-03 | 中国海洋石油集团有限公司 | Low-carbon alkane reforming reaction device and synthesis gas equipment |
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| Publication number | Publication date |
|---|---|
| WO2014111315A1 (en) | 2014-07-24 |
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|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| ASS | Succession or assignment of patent right |
Owner name: SHANGHAI ADVANCED RESEARCH INSTITUTE, CHINESE ACAD Free format text: FORMER OWNER: SHANGHAI ZHONGKE INSTITUTE FOR ADVANCED STUDY Effective date: 20140130 |
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Effective date of registration: 20140130 Address after: 201210 Shanghai city Pudong New Area Hartcourt Road No. 99 Patentee after: SHANGHAI ADVANCED Research Institute CHINESE ACADEMY OF SCIENCES Patentee after: SHANXI LU'AN ENVIRONMENTAL ENERGY DEVELOPMENT Co.,Ltd. Address before: 201210 Shanghai city Pudong New Area Hartcourt Road No. 99 Patentee before: SHANGHAI ADVANCED Research Institute CHINESE ACADEMY OF SCIENCES Patentee before: SHANXI LU'AN ENVIRONMENTAL ENERGY DEVELOPMENT Co.,Ltd. |
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Effective date of registration: 20171024 Address after: 201210 Shanghai city Pudong New Area Hartcourt Road No. 99 Co-patentee after: SHANXI LU'AN MINING INDUSTRY GROUP Co.,Ltd. Patentee after: SHANGHAI ADVANCED Research Institute CHINESE ACADEMY OF SCIENCES Address before: 201210 Shanghai city Pudong New Area Hartcourt Road No. 99 Co-patentee before: SHANXI LU'AN ENVIRONMENTAL ENERGY DEVELOPMENT Co.,Ltd. Patentee before: SHANGHAI ADVANCED Research Institute CHINESE ACADEMY OF SCIENCES |
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Effective date of registration: 20191127 Address after: 201210 Shanghai city Pudong New Area Hartcourt Road No. 99 Co-patentee after: SHANXI LU'AN MINING INDUSTRY GROUP Co.,Ltd. Patentee after: SHANGHAI ADVANCED Research Institute CHINESE ACADEMY OF SCIENCES Co-patentee after: Shanghai Shao Rui Low Carbon Energy Partnership (L.P.) Address before: 201210 Shanghai city Pudong New Area Hartcourt Road No. 99 Co-patentee before: SHANXI LU'AN MINING INDUSTRY GROUP Co.,Ltd. Patentee before: SHANGHAI ADVANCED Research Institute CHINESE ACADEMY OF SCIENCES |
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Effective date of registration: 20210429 Address after: 201616 Room 501, 5th floor, building 11, 300 Dingyuan Road, Songjiang District, Shanghai Patentee after: Gaolu air chemical products (Shanghai) Energy Technology Co.,Ltd. Address before: 201210 Shanghai city Pudong New Area Hartcourt Road No. 99 Patentee before: SHANGHAI ADVANCED Research Institute CHINESE ACADEMY OF SCIENCES Patentee before: SHANXI LU'AN MINING INDUSTRY GROUP Co.,Ltd. Patentee before: Shanghai Shao Rui Low Carbon Energy Partnership (L.P.) |
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Granted publication date: 20130828 |