CN104129757A - Catalytic gasification method of supercritical water system organic matter Ru/CeO2 - Google Patents
Catalytic gasification method of supercritical water system organic matter Ru/CeO2 Download PDFInfo
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- CN104129757A CN104129757A CN201410397793.5A CN201410397793A CN104129757A CN 104129757 A CN104129757 A CN 104129757A CN 201410397793 A CN201410397793 A CN 201410397793A CN 104129757 A CN104129757 A CN 104129757A
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- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 title claims abstract description 66
- 238000002309 gasification Methods 0.000 title claims abstract description 25
- 238000000034 method Methods 0.000 title claims abstract description 22
- 230000003197 catalytic effect Effects 0.000 title claims abstract description 10
- CETPSERCERDGAM-UHFFFAOYSA-N ceric oxide Chemical compound O=[Ce]=O CETPSERCERDGAM-UHFFFAOYSA-N 0.000 title abstract description 5
- 229910000422 cerium(IV) oxide Inorganic materials 0.000 title abstract description 5
- 239000005416 organic matter Substances 0.000 title abstract 6
- 238000006243 chemical reaction Methods 0.000 claims abstract description 65
- 239000003054 catalyst Substances 0.000 abstract description 19
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 abstract description 16
- 239000001257 hydrogen Substances 0.000 abstract description 10
- 229910052739 hydrogen Inorganic materials 0.000 abstract description 10
- 238000004519 manufacturing process Methods 0.000 abstract description 6
- 230000035484 reaction time Effects 0.000 abstract description 6
- 239000000126 substance Substances 0.000 abstract description 5
- 230000015556 catabolic process Effects 0.000 abstract description 3
- 238000006731 degradation reaction Methods 0.000 abstract description 3
- 238000004064 recycling Methods 0.000 abstract description 2
- 230000004888 barrier function Effects 0.000 abstract 1
- 238000001833 catalytic reforming Methods 0.000 abstract 1
- 230000018044 dehydration Effects 0.000 abstract 1
- 238000006297 dehydration reaction Methods 0.000 abstract 1
- 125000004435 hydrogen atom Chemical class [H]* 0.000 abstract 1
- 239000007788 liquid Substances 0.000 description 52
- 239000000047 product Substances 0.000 description 32
- ISWSIDIOOBJBQZ-UHFFFAOYSA-N Phenol Chemical compound OC1=CC=CC=C1 ISWSIDIOOBJBQZ-UHFFFAOYSA-N 0.000 description 25
- 239000007789 gas Substances 0.000 description 17
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 8
- 239000002894 chemical waste Substances 0.000 description 8
- 238000004939 coking Methods 0.000 description 8
- 239000002994 raw material Substances 0.000 description 8
- 238000010438 heat treatment Methods 0.000 description 6
- 239000000203 mixture Substances 0.000 description 5
- 238000002360 preparation method Methods 0.000 description 5
- 239000007795 chemical reaction product Substances 0.000 description 4
- 239000004615 ingredient Substances 0.000 description 4
- 239000002028 Biomass Substances 0.000 description 3
- 230000000694 effects Effects 0.000 description 2
- 239000012530 fluid Substances 0.000 description 2
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 235000011089 carbon dioxide Nutrition 0.000 description 1
- 230000000052 comparative effect Effects 0.000 description 1
- 230000008034 disappearance Effects 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 150000002431 hydrogen Chemical class 0.000 description 1
- 239000007791 liquid phase Substances 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 125000001997 phenyl group Chemical group [H]C1=C([H])C([H])=C(*)C([H])=C1[H] 0.000 description 1
- 238000005554 pickling Methods 0.000 description 1
- 239000011148 porous material Substances 0.000 description 1
- 239000000843 powder Substances 0.000 description 1
- 238000002203 pretreatment Methods 0.000 description 1
- 230000000750 progressive effect Effects 0.000 description 1
- 230000009466 transformation Effects 0.000 description 1
Classifications
-
- 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
- Y02P20/54—Improvements relating to the production of bulk chemicals using solvents, e.g. supercritical solvents or ionic liquids
-
- 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
- Y02P20/584—Recycling of catalysts
Abstract
The invention discloses a catalytic gasification method of supercritical water system organic matter Ru/CeO2, belonging to the field of supercritical energy. According to the method, an organic matter is subjected to catalytic gasification underwater mainly by applying a catalyst under a supercritical condition, the applied catalyst is Ru/CeO2, and by utilizing the supercritical water condition, the mass transfer barriers of the reaction are fewer, water can participate in the reaction, and reacting organic matter is not required for dehydration pretreatment; the catalyst is applied during the gasification of the organic matter under the supercritical water condition, so that not only can catalytic reforming reaction of water vapor be promoted to improve the yield of hydrogen, but also the degradation of the organic matter can be accelerated to produce an energy substance, namely methane, the reaction time is greatly shortened, the conversion efficiency is high, the recycling of the catalyst has less impact on the efficiency, and no secondary pollution is generated during production.
Description
Technical field
The present invention relates to a kind of supercritical water system organism Ru/CeO
2the method of catalytic gasification, belongs to overcritical energy field.
Technical background
Along with energy dilemma is on the rise; exploitation for new forms of energy more and more comes into one's own; and wherein the gasification hydrogen-producing methane equal energy source processed gas under organic condition of supercritical water just gains great popularity; because the disappearance at liquid phase mass transfer interface under super critical condition; make rate of mass transfer increase; the efficiency of reaction is improved greatly; simultaneously because water itself is exactly conventional supercritical medium; thereby the reaction of supercritical water system, thereby raw material can not need to dewater, pre-treatment directly utilizes save energy.There is at present the much research about gasifying under super critical condition biomass as raw material, but because the essentially consist of biomass is mostly the larger molecular organics that contains phenyl ring, even in overcritical that extreme condition, the speed of reaction is still comparatively slow, therefore in order to improve the efficiency of reaction, increasing investigator converges in sight in the selection and preparation of catalyzer.
The at present comparatively common catalyzer for supercritical gasification is better with the effect of Ru system and Ni series catalysts, increasing Ru system and Ni series catalysts are applied on the hydrogen manufacturing methane processed of condition of supercritical water, but this wherein many catalyzer under super critical condition, easily lose activity, therefore cannot use continuously, carrier that can tolerate super critical condition is used for support catalyst and is absolutely necessary.
Mesoporous ceria is because it has the advantage existence of larger specific surface area and more regular pore passage structure, thereby in the preparation of a lot of catalyzer, be selected as the carrier of catalyzer, cerium dioxide can tolerate the high temperature on 2000 ℃ simultaneously, therefore can regard carrier comparatively suitable under super critical condition as.
The catalyzer of stability and high efficiency and condition of supercritical water are combined, just have and realize the possibility that organic high-efficiency and continuous is prepared hydrogen, methane equal energy source material.
Summary of the invention
The object of the invention is for the not long situation of catalyst life under supercritical fluids system provide a kind of can be for improving organism gasification efficiency and catalyzer---Ru/CeO that can repeatedly reuse under condition of supercritical water
2thereby realize the Efficient Conversion of organism under supercritical water system, traditional catalyzing manufacturing of hydrogen and supercritical gasification are combined, can be so that improve the efficiency that organism is converted into hydrogen and methane in supercritical water system, after reusing, loss in efficiency is no more than 10% simultaneously.
Described catalyzer is with RuCl
3and Ce (NO
3)
36H
2o adopts pickling process to be prepared as raw material, and catalyzer is the powder of black in appearance, and the charge capacity of Ru is 5wt%, the support C eO of preparation
2for meso-hole structure, water hole volume is 0.35mL/g.
Described supercritical gasification reaction comprises following step, determines the add-on of water according to the residing temperature of reaction and calculation of pressure; The catalyzer that then adds organism, water and the preparation of reaction in reactor, the 1wt%-10wt% that organic add-on is water, catalyzer add-on is organic 10wt%-100wt%; Closed reactor, replaces the air in reactor emptying, and the oxygen in excluding air makes product oxidized in order to avoid it participates in gasification, then with heat source, carry out reacting by heating, wherein the reaction times is 0.5-40min, and pressure is 20-29.6MPa, and temperature is 450-550 ℃.
Realize useless its reaction unit of transformation vapour oil treatment process of the present invention, comprise water tank 1, high-pressure metering pump 2, pre-heaters 3, supercritical reaction device 4, high-pressure metering pump 5, surge tank 6, gas-liquid separator 7, collection and confinement of gases tank 8, liquid collection tank 9, water tank 1 is connected with pre-heaters 3 by high-pressure metering pump 2, pre-heaters 3, supercritical reaction device 4, high-pressure metering pump 5, surge tank 6 connects successively, pre-heaters 3 is connected with gas-liquid separator 7, and gas-liquid separator 7 is connected with liquid collection tank 9 with collection and confinement of gases tank 8 respectively.
Between each parts of the present invention, by pipeline, connect, valve is controlled.
The method of the invention is when association reaction device is used, first by reaction mass and catalyzer Ru/CeO
2insert in supercritical reaction device 4, tighten valve I, water in water tank 1 is after high-pressure metering pump 2 is extracted out, after pre-heaters 3 preheatings, squeeze in supercritical reaction device 4 and catalyst mix reacting by heating, after reaction finishes, open valve I, by high-pressure metering pump 5, gas-liquid mixed product is squeezed in surge tank 6, and after product enters into gas-liquid separator 7 after pre-heaters 3 decrease temperature and pressure, product also can in pre-heaters 3, continue by the mode of pump around circuit preheating laggard enter in supercritical reaction device 4 repeatedly react, gaseous product CO in gas-liquid separator 7
2, H
2, CH
4deng being stored in collection and confinement of gases tank 8, product liquid enters into liquid collection tank 9 and reclaims.
Supercritical reaction device of the present invention improves gained for the component such as supercritical reaction device of commercially available high temperature high voltage resistant are assembled.
Positive progressive effect of the present invention is:
(1) method of the present invention combines conventional catalyst hydrogen manufacturing with the organism gasification under supercritical water system, can improve organic degradation rate, and the production rate that improves hydrogen and methane impels whole reaction forward significantly to advance;
(2) method of the present invention catalyzer used is still stablized under postcritical extreme condition, reuses decrease in efficiency not remarkable, can repeatedly reuse;
(3) method of the present invention supercritical fluids system used to gasified raw material require low, applicable equally for the biomass that a lot of water content are large, and the height under super critical condition reaches ability and also can improve organic gasification efficiency;
(4) method of the present invention can, for the pollutent of some difficult degradations, have promoter action to realizing the recycling of pollutent equally;
(5) product of method reaction gained of the present invention mainly only has hydrogen and methane and a small amount of carbonic acid gas, and product environmental protection is pollution-free;
In a word, by the Ru/CeO of this preparation
2catalyzer combines with supercritical water gasification, and the two can be mutually promoted, and makes whole technique suitability wide, reaction process time shorten, the productive rate of raising hydrogen and methane, production process non-secondary pollution.
Accompanying drawing explanation
Fig. 1 is the structural representation of reaction unit of the present invention;
In figure: water tank 1, high-pressure metering pump 2, pre-heaters 3, supercritical reaction device 4, high-pressure metering pump 5, surge tank 6, gas-liquid separator 7, collection and confinement of gases tank 8, liquid collection tank 9.
Embodiment
Below in conjunction with the drawings and specific embodiments, the present invention is described in further detail, but protection domain of the present invention is not limited to described content.
Embodiment 1
Described in the present embodiment, for the organic substance that gasifies, be phenol, comprise the steps: to add 0.0138g phenol in reactor, 0.0069g catalyzer Ru/CeO
2and 276 μ L water, get rid of inner air after tightening reactor, reactor is placed in to sand-bath and carries out reacting under super critical condition, reaction times is 20min, and pressure is 20MPa, and temperature is 500 ℃, phenol quality is the 5wt% of water, the 50wt% that catalyst quality is phenol.
Realize the reaction unit of the treatment process of the coking chemical waste water described in the present embodiment, comprise water tank 1, high-pressure metering pump 2, pre-heaters 3, supercritical reaction device 4, high-pressure metering pump 5, surge tank 6, gas-liquid separator 7, collection and confinement of gases tank 8, liquid collection tank 9, water tank 1 is connected with pre-heaters 3 by high-pressure metering pump 2, pre-heaters 3, supercritical reaction device 4, high-pressure metering pump 5, surge tank 6 connects successively, pre-heaters 3 is connected with gas-liquid separator 7, gas-liquid separator 7 is connected with liquid collection tank 9 with collection and confinement of gases tank 8 respectively, as shown in Figure 1, described in the present embodiment, between each parts, by pipeline, connect, valve is controlled.
It is raw material that the present embodiment be take the phenol of one of coking chemical waste water major ingredient, and before reaction, the concentration of phenol is 50.00g/L
When described in the present embodiment, supercritical gasification device is used, first by reaction mass and catalyzer Ru/CeO
2insert in supercritical reaction device 4, tighten valve I, water in water tank 1 is after high-pressure metering pump 2 is extracted out, after pre-heaters 3 preheatings, squeeze in supercritical reaction device 4 and catalyst mix reacting by heating, after reaction finishes, open valve I, by high-pressure metering pump 5, gas-liquid mixed product is squeezed in surge tank 6, and after product enters into gas-liquid separator 7 after pre-heaters 3 decrease temperature and pressure, product also can in pre-heaters 3, continue by the mode of pump around circuit preheating laggard enter in supercritical reaction device 4 repeatedly react, gaseous product CO in gas-liquid separator 7
2, H
2, CH
4deng being stored in collection and confinement of gases tank 8, product liquid enters into liquid collection tank 9 and reclaims, and the productive rate of the gaseous product of the present embodiment gained and indices are listed in table one:
The indices of table 1 reaction product
Embodiment 2
Described in the present embodiment, for the organic substance that gasifies, be phenol, comprise the steps: to add 0.0039g phenol in reactor, 0.0039g catalyzer Ru/CeO
2and 391 μ L water, get rid of inner air after tightening reactor, reactor is placed in to sand-bath and carries out reacting under super critical condition, reaction times is 30min, and pressure is 23.00MPa, and temperature is 450 ℃, phenol quality is the 1wt% of water, the 100wt% that catalyst quality is phenol.
Realize the reaction unit of the treatment process of the coking chemical waste water described in the present embodiment, comprise water tank 1, high-pressure metering pump 2, pre-heaters 3, supercritical reaction device 4, high-pressure metering pump 5, surge tank 6, gas-liquid separator 7, collection and confinement of gases tank 8, liquid collection tank 9, water tank 1 is connected with pre-heaters 3 by high-pressure metering pump 2, pre-heaters 3, supercritical reaction device 4, high-pressure metering pump 5, surge tank 6 connects successively, pre-heaters 3 is connected with gas-liquid separator 7, gas-liquid separator 7 is connected with liquid collection tank 9 with collection and confinement of gases tank 8 respectively, as shown in Figure 1, described in the present embodiment, between each parts, by pipeline, connect, valve is controlled.
It is raw material that the present embodiment be take the phenol of one of coking chemical waste water major ingredient, and before reaction, the concentration of phenol is 9.97g/L.
When described in the present embodiment, supercritical gasification device is used, first by reaction mass and catalyzer Ru/CeO
2insert in supercritical reaction device 4, tighten valve I, water in water tank 1 is after high-pressure metering pump 2 is extracted out, after pre-heaters 3 preheatings, squeeze in supercritical reaction device 4 and catalyst mix reacting by heating, after reaction finishes, open valve I, by high-pressure metering pump 5, gas-liquid mixed product is squeezed in surge tank 6, and after product enters into gas-liquid separator 7 after pre-heaters 3 decrease temperature and pressure, product also can in pre-heaters 3, continue by the mode of pump around circuit preheating laggard enter in supercritical reaction device 4 repeatedly react, gaseous product CO in gas-liquid separator 7
2, H
2, CH
4deng being stored in collection and confinement of gases tank 8, product liquid enters into liquid collection tank 9 and reclaims, and the productive rate of the gaseous product of the present embodiment gained and indices are listed in table two:
The indices of table 2 reaction product
Embodiment 3
Described in the present embodiment, for the organic substance that gasifies, be phenol, comprise the steps: to add 0.0391g phenol in reactor, 0.0004g catalyzer Ru/CeO
2and 391 μ L water, get rid of inner air after tightening reactor, reactor is placed in to sand-bath and carries out reacting under super critical condition, reaction times is 0.5min, and pressure is 29.60MPa, and temperature is 550 ℃, phenol quality is the 10wt% of water, the 10wt% that catalyst quality is phenol.
Realize the reaction unit of the treatment process of the coking chemical waste water described in the present embodiment, comprise water tank 1, high-pressure metering pump 2, pre-heaters 3, supercritical reaction device 4, high-pressure metering pump 5, surge tank 6, gas-liquid separator 7, collection and confinement of gases tank 8, liquid collection tank 9, water tank 1 is connected with pre-heaters 3 by high-pressure metering pump 2, pre-heaters 3, supercritical reaction device 4, high-pressure metering pump 5, surge tank 6 connects successively, pre-heaters 3 is connected with gas-liquid separator 7, gas-liquid separator 7 is connected with liquid collection tank 9 with collection and confinement of gases tank 8 respectively, as shown in Figure 1.Described in the present embodiment, between each parts, by pipeline, connect, valve is controlled.
It is raw material that the present embodiment be take the phenol of one of coking chemical waste water major ingredient, and before reaction, the concentration of phenol is 100.00g/L.
When described in the present embodiment, supercritical gasification device is used, first by reaction mass and catalyzer Ru/CeO
2insert in supercritical reaction device 4, tighten valve I, water in water tank 1 is after high-pressure metering pump 2 is extracted out, after pre-heaters 3 preheatings, squeeze in supercritical reaction device 4 and catalyst mix reacting by heating, after reaction finishes, open valve I, by high-pressure metering pump 5, gas-liquid mixed product is squeezed in surge tank 6, and after product enters into gas-liquid separator 7 after pre-heaters 3 decrease temperature and pressure, product also can in pre-heaters 3, continue by the mode of pump around circuit preheating laggard enter in supercritical reaction device 4 repeatedly react, gaseous product CO in gas-liquid separator 7
2, H
2, CH
4deng being stored in collection and confinement of gases tank 8, product liquid enters into liquid collection tank 9 and reclaims, and the productive rate of the gaseous product of the present embodiment gained and indices are listed in table three:
The indices of table 3 reaction product
Embodiment 4
Described in the present embodiment, for the organic substance that gasifies, be phenol, comprise the steps: to add 0.0196g phenol, Ru/CeO in reactor
2and 391 μ L water, get rid of inner air after tightening reactor, reactor is placed in to sand-bath and carries out reacting under super critical condition, reaction times is 40min, and pressure is 28MPa, and temperature is 530 ℃, phenol quality is the 5wt% of water, the 30wt% that catalyst quality is phenol.
The present embodiment does not add Ru/CeO
2catalyzer is only the gasification of the phenol under conventional super critical condition, for comparative catalyst Ru/CeO
2effect.
Realize the reaction unit of the treatment process of the coking chemical waste water described in the present embodiment, comprise water tank 1, high-pressure metering pump 2, pre-heaters 3, supercritical reaction device 4, high-pressure metering pump 5, surge tank 6, gas-liquid separator 7, collection and confinement of gases tank 8, liquid collection tank 9, water tank 1 is connected with pre-heaters 3 by high-pressure metering pump 2, pre-heaters 3, supercritical reaction device 4, high-pressure metering pump 5, surge tank 6 connects successively, pre-heaters 3 is connected with gas-liquid separator 7, gas-liquid separator 7 is connected with liquid collection tank 9 with collection and confinement of gases tank 8 respectively, as shown in Figure 1.Described in the present embodiment, between each parts, by pipeline, connect, valve is controlled.
It is raw material that the present embodiment be take the phenol of one of coking chemical waste water major ingredient, and before reaction, the concentration of phenol is 50.13g/L.
When described in the present embodiment, supercritical gasification device is used, first reaction mass is inserted in supercritical reaction device 4, tighten valve I, water in water tank 1 is after high-pressure metering pump 2 is extracted out, after pre-heaters 3 preheatings, squeeze in supercritical reaction device 4 and catalyst mix reacting by heating, after reaction finishes, open valve I, by high-pressure metering pump 5, gas-liquid mixed product is squeezed in surge tank 6, and after product enters into gas-liquid separator 7 after pre-heaters 3 decrease temperature and pressure, product also can in pre-heaters 3, continue by the mode of pump around circuit preheating laggard enter in supercritical reaction device 4 repeatedly react, gaseous product CO in gas-liquid separator 7
2, H
2, CH
4deng being stored in collection and confinement of gases tank 8, product liquid enters into liquid collection tank 9 and reclaims, and the productive rate of the gaseous product of the present embodiment gained and indices are listed in table four:
The indices of table 4 reaction product
Claims (4)
1. a supercritical water system organism Ru/CeO
2the method of catalytic gasification, is characterized in that: under supercritical state, under condition of supercritical water, add Ru/CeO
2catalyzer carries out catalytic gasification to organism, reaction 0.5-40min.
2. supercritical water system organism Ru/CeO according to claim 1
2the method of catalytic gasification, is characterized in that: 450 ℃-550 ℃ of described supercritical state temperature, pressure 20-29.6MPa.
3. supercritical water system organism Ru/CeO according to claim 1
2the method of catalytic gasification, is characterized in that: the 1wt%-10wt% that described organic add-on is water, catalyzer add-on is organic 10wt%-100wt%.
4. supercritical water system organism Ru/CeO according to claim 1
2the method of catalytic gasification, is characterized in that: described Ru/CeO
2in catalyzer, the charge capacity of Ru is 5wt%.
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN104959139A (en) * | 2015-06-15 | 2015-10-07 | 昆明理工大学 | Catalyst and application thereof |
| CN109928417A (en) * | 2019-02-28 | 2019-06-25 | 昆明理工大学 | A kind of preparation method of white pure zirconia cerium |
| CN113060703A (en) * | 2021-04-27 | 2021-07-02 | 西安热工研究院有限公司 | Novel system and method for catalytic hydrogen production by steam under high-temperature and high-pressure working conditions |
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| CN102101715A (en) * | 2009-12-18 | 2011-06-22 | 中国科学院兰州化学物理研究所 | Treatment method of organic waste water |
| CN103073103A (en) * | 2012-12-28 | 2013-05-01 | 新奥科技发展有限公司 | Method for treating carbon-containing organic matter by supercritical water oxidation |
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2014
- 2014-08-14 CN CN201410397793.5A patent/CN104129757A/en active Pending
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN102101715A (en) * | 2009-12-18 | 2011-06-22 | 中国科学院兰州化学物理研究所 | Treatment method of organic waste water |
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104959139A (en) * | 2015-06-15 | 2015-10-07 | 昆明理工大学 | Catalyst and application thereof |
| CN109928417A (en) * | 2019-02-28 | 2019-06-25 | 昆明理工大学 | A kind of preparation method of white pure zirconia cerium |
| CN109928417B (en) * | 2019-02-28 | 2022-03-22 | 昆明理工大学 | Preparation method of white pure cerium oxide |
| CN113060703A (en) * | 2021-04-27 | 2021-07-02 | 西安热工研究院有限公司 | Novel system and method for catalytic hydrogen production by steam under high-temperature and high-pressure working conditions |
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