CN111889116A - Catalytic combustion catalyst and preparation method thereof - Google Patents
Catalytic combustion catalyst and preparation method thereof Download PDFInfo
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- CN111889116A CN111889116A CN201910365847.2A CN201910365847A CN111889116A CN 111889116 A CN111889116 A CN 111889116A CN 201910365847 A CN201910365847 A CN 201910365847A CN 111889116 A CN111889116 A CN 111889116A
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- zinc
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- molybdenum
- sulfate
- aluminum oxide
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- 239000003054 catalyst Substances 0.000 title claims abstract description 53
- 238000007084 catalytic combustion reaction Methods 0.000 title claims abstract description 20
- 238000002360 preparation method Methods 0.000 title abstract description 15
- ZOKXTWBITQBERF-UHFFFAOYSA-N Molybdenum Chemical compound [Mo] ZOKXTWBITQBERF-UHFFFAOYSA-N 0.000 claims abstract description 42
- 229910052750 molybdenum Inorganic materials 0.000 claims abstract description 42
- 239000011733 molybdenum Substances 0.000 claims abstract description 42
- HCHKCACWOHOZIP-UHFFFAOYSA-N Zinc Chemical compound [Zn] HCHKCACWOHOZIP-UHFFFAOYSA-N 0.000 claims abstract description 40
- 229910052725 zinc Inorganic materials 0.000 claims abstract description 40
- 239000011701 zinc Substances 0.000 claims abstract description 40
- 239000003245 coal Substances 0.000 claims abstract description 37
- 238000001035 drying Methods 0.000 claims abstract description 25
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 claims abstract description 23
- TWNQGVIAIRXVLR-UHFFFAOYSA-N oxo(oxoalumanyloxy)alumane Chemical compound O=[Al]O[Al]=O TWNQGVIAIRXVLR-UHFFFAOYSA-N 0.000 claims abstract description 18
- VZDYWEUILIUIDF-UHFFFAOYSA-J cerium(4+);disulfate Chemical compound [Ce+4].[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O VZDYWEUILIUIDF-UHFFFAOYSA-J 0.000 claims abstract description 17
- 229910000355 cerium(IV) sulfate Inorganic materials 0.000 claims abstract description 17
- 238000004898 kneading Methods 0.000 claims abstract description 15
- 239000002131 composite material Substances 0.000 claims abstract description 3
- 239000007789 gas Substances 0.000 claims description 54
- 238000000034 method Methods 0.000 claims description 29
- OYFRNYNHAZOYNF-UHFFFAOYSA-N 2,5-dihydroxyterephthalic acid Chemical compound OC(=O)C1=CC(O)=C(C(O)=O)C=C1O OYFRNYNHAZOYNF-UHFFFAOYSA-N 0.000 claims description 12
- QMKYBPDZANOJGF-UHFFFAOYSA-N benzene-1,3,5-tricarboxylic acid Chemical compound OC(=O)C1=CC(C(O)=O)=CC(C(O)=O)=C1 QMKYBPDZANOJGF-UHFFFAOYSA-N 0.000 claims description 12
- ONDPHDOFVYQSGI-UHFFFAOYSA-N zinc nitrate Chemical compound [Zn+2].[O-][N+]([O-])=O.[O-][N+]([O-])=O ONDPHDOFVYQSGI-UHFFFAOYSA-N 0.000 claims description 10
- -1 ceryl sulfate Chemical compound 0.000 claims description 9
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 9
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 8
- 229910052684 Cerium Inorganic materials 0.000 claims description 8
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 claims description 8
- GWXLDORMOJMVQZ-UHFFFAOYSA-N cerium Chemical compound [Ce] GWXLDORMOJMVQZ-UHFFFAOYSA-N 0.000 claims description 8
- 238000005516 engineering process Methods 0.000 claims description 8
- 125000002252 acyl group Chemical group 0.000 claims description 7
- OZECDDHOAMNMQI-UHFFFAOYSA-H cerium(3+);trisulfate Chemical compound [Ce+3].[Ce+3].[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O OZECDDHOAMNMQI-UHFFFAOYSA-H 0.000 claims description 7
- 230000008569 process Effects 0.000 claims description 7
- 229910000333 cerium(III) sulfate Inorganic materials 0.000 claims description 6
- 239000003795 chemical substances by application Substances 0.000 claims description 4
- 229910052757 nitrogen Inorganic materials 0.000 claims description 4
- 150000003751 zinc Chemical class 0.000 claims description 4
- VNDYJBBGRKZCSX-UHFFFAOYSA-L zinc bromide Chemical compound Br[Zn]Br VNDYJBBGRKZCSX-UHFFFAOYSA-L 0.000 claims description 4
- JIAARYAFYJHUJI-UHFFFAOYSA-L zinc dichloride Chemical compound [Cl-].[Cl-].[Zn+2] JIAARYAFYJHUJI-UHFFFAOYSA-L 0.000 claims description 4
- 239000011259 mixed solution Substances 0.000 claims description 3
- 239000012266 salt solution Substances 0.000 claims description 3
- 239000012752 auxiliary agent Substances 0.000 claims description 2
- 229910052751 metal Inorganic materials 0.000 claims description 2
- 239000002184 metal Substances 0.000 claims description 2
- 150000002751 molybdenum Chemical class 0.000 claims description 2
- 229940102001 zinc bromide Drugs 0.000 claims description 2
- 235000005074 zinc chloride Nutrition 0.000 claims description 2
- 239000011592 zinc chloride Substances 0.000 claims description 2
- 229960001939 zinc chloride Drugs 0.000 claims description 2
- NWONKYPBYAMBJT-UHFFFAOYSA-L zinc sulfate Chemical compound [Zn+2].[O-]S([O-])(=O)=O NWONKYPBYAMBJT-UHFFFAOYSA-L 0.000 claims description 2
- 229960001763 zinc sulfate Drugs 0.000 claims description 2
- 229910000368 zinc sulfate Inorganic materials 0.000 claims description 2
- 239000013065 commercial product Substances 0.000 claims 1
- 238000007598 dipping method Methods 0.000 claims 1
- 238000006243 chemical reaction Methods 0.000 abstract description 29
- 230000000694 effects Effects 0.000 abstract description 11
- 238000000465 moulding Methods 0.000 abstract description 6
- 230000008901 benefit Effects 0.000 abstract description 4
- 238000002485 combustion reaction Methods 0.000 abstract description 3
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 46
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 14
- 229910052760 oxygen Inorganic materials 0.000 description 14
- 239000001301 oxygen Substances 0.000 description 14
- 239000000571 coke Substances 0.000 description 9
- 238000004587 chromatography analysis Methods 0.000 description 8
- 239000000523 sample Substances 0.000 description 8
- 229910000510 noble metal Inorganic materials 0.000 description 7
- 230000003197 catalytic effect Effects 0.000 description 5
- 239000007864 aqueous solution Substances 0.000 description 3
- 230000007613 environmental effect Effects 0.000 description 3
- 238000002156 mixing Methods 0.000 description 3
- KDLHZDBZIXYQEI-UHFFFAOYSA-N Palladium Chemical compound [Pd] KDLHZDBZIXYQEI-UHFFFAOYSA-N 0.000 description 2
- 230000004913 activation Effects 0.000 description 2
- 238000007796 conventional method Methods 0.000 description 2
- 239000006185 dispersion Substances 0.000 description 2
- 238000004134 energy conservation Methods 0.000 description 2
- 238000004880 explosion Methods 0.000 description 2
- 238000007254 oxidation reaction Methods 0.000 description 2
- 238000001179 sorption measurement Methods 0.000 description 2
- ZXAUZSQITFJWPS-UHFFFAOYSA-J zirconium(4+);disulfate Chemical compound [Zr+4].[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O ZXAUZSQITFJWPS-UHFFFAOYSA-J 0.000 description 2
- YKVBIIAIQQLEPB-UHFFFAOYSA-L S(=O)(=O)([O-])[O-].[Mo+4].[Ce+3] Chemical compound S(=O)(=O)([O-])[O-].[Mo+4].[Ce+3] YKVBIIAIQQLEPB-UHFFFAOYSA-L 0.000 description 1
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- PTFCDOFLOPIGGS-UHFFFAOYSA-N Zinc dication Chemical compound [Zn+2] PTFCDOFLOPIGGS-UHFFFAOYSA-N 0.000 description 1
- RQYSWULBRFINID-UHFFFAOYSA-N [Mo].[Ce] Chemical compound [Mo].[Ce] RQYSWULBRFINID-UHFFFAOYSA-N 0.000 description 1
- 230000009471 action Effects 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000001354 calcination Methods 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 238000009841 combustion method Methods 0.000 description 1
- 230000000052 comparative effect Effects 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 230000009977 dual effect Effects 0.000 description 1
- 239000000428 dust Substances 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- XMHIUKTWLZUKEX-UHFFFAOYSA-N hexacosanoic acid Chemical compound CCCCCCCCCCCCCCCCCCCCCCCCCC(O)=O XMHIUKTWLZUKEX-UHFFFAOYSA-N 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 238000011031 large-scale manufacturing process Methods 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 230000007246 mechanism Effects 0.000 description 1
- 150000004706 metal oxides Chemical class 0.000 description 1
- 230000008520 organization Effects 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 229910052763 palladium Inorganic materials 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 229910052761 rare earth metal Inorganic materials 0.000 description 1
- 150000002910 rare earth metals Chemical class 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 239000002893 slag Substances 0.000 description 1
- 239000000243 solution Substances 0.000 description 1
- 238000003860 storage Methods 0.000 description 1
- 229910052717 sulfur Inorganic materials 0.000 description 1
- 239000011593 sulfur Substances 0.000 description 1
- 150000003568 thioethers Chemical class 0.000 description 1
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J27/00—Catalysts comprising the elements or compounds of halogens, sulfur, selenium, tellurium, phosphorus or nitrogen; Catalysts comprising carbon compounds
- B01J27/02—Sulfur, selenium or tellurium; Compounds thereof
- B01J27/053—Sulfates
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
- C10L3/06—Natural gas; Synthetic natural gas obtained by processes not covered by C10G, C10K3/02 or C10K3/04
- C10L3/10—Working-up natural gas or synthetic natural gas
- C10L3/101—Removal of contaminants
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
- C10L2290/02—Combustion or pyrolysis
Abstract
The invention discloses a catalytic combustion catalyst and a preparation method thereof, wherein the catalyst contains a composite oxide of zinc-loaded alumina and molybdenum-loaded ceric sulfate, the weight ratio of the zinc-loaded alumina to the molybdenum-loaded ceric sulfate is 10:1-4:1, the content of zinc in oxide is 5-25 wt% based on the weight of the zinc-loaded alumina, and the content of molybdenum in oxide is 0.5-5 wt% based on the weight of the molybdenum-loaded ceric sulfate; the preparation method of the catalyst comprises the following steps: and kneading and molding the zinc-loaded aluminum oxide and the molybdenum-loaded ceric sulfate, drying and roasting to obtain the coal bed gas catalytic combustion catalyst. The catalyst is used for deoxidation combustion of the coal bed gas and has the advantages of high activity, low reaction temperature, simple preparation method, low cost and the like.
Description
Technical Field
The invention relates to a catalytic combustion catalyst and a preparation method thereof, in particular to a low-temperature high-activity coal bed gas catalytic combustion catalyst and a preparation method thereof.
Background
China is a large coal producing country, coal bed gas with different concentrations can be produced due to coal production every year, and developing effective coal bed gas utilization technology and reducing direct emission of methane are a component part for building an energy-saving and environment-friendly sustainable development mode and building a low-carbon economic system in China. The method has the advantages that the low-grade energy source coal bed gas is practically and reasonably developed by combining energy conservation and emission reduction and improvement of the requirement on the environment, the low-grade energy source coal bed gas is well converted into available resources, the application range and the scale of the coal bed gas are expanded, the utilization efficiency of the coal bed gas is improved, the dual meanings of energy conservation and environmental protection are realized, the national planning on energy policies is met, the control of the international environmental protection organization on the greenhouse effect is met, the strong support of China on the development and the use of the low-grade energy source is better met, and the domestic rapid development of the coal bed gas industry.
The key point of the development and utilization of the coal bed gas is to remove oxygen in the coal bed gas, and the existing coal bed gas deoxidation technology mainly comprises a pressure swing adsorption separation method, a coke combustion method, a catalytic deoxidation method and the like. Chinese patent ZL85103557 discloses a method for separating and enriching methane from coal bed gas by using a pressure swing adsorption method. Generally, the oxygen content of the exhaust gas discharged in the concentration and purification process of methane is also concentrated and improved, and the exhaust gas inevitably contains 5-15% of methane, so that the discharged exhaust gas is in the explosion limit range of methane, and explosion danger exists, so that the application of the technology is limited.
The deoxidation method by using coke combustion (ZL 02113627.0, 200610021720.1) is characterized in that oxygen in methane-rich gas reacts with coke under the high-temperature condition, and part of methane reacts with oxygen to achieve the aim of deoxidation. The advantage is that about 70% of the oxygen reacts with coke and 30% of the oxygen reacts with methane, so that methane losses are smaller. But the disadvantage is that the precious coke resource is consumed, and the coke consumption cost accounts for about 50 percent of the whole operation cost. In addition, the coke deoxidation method has high labor intensity during coke feeding and slag discharging, large environmental dust and difficulty in realizing self-control operation and large-scale production, and the coke contains sulfides in various forms, so that the sulfur content in the gas after oxygen removal is increased.
The essence of the catalytic deoxidation process is that methane is catalytically combusted under rich-fuel oxygen-poor atmosphere, and CH is subjected to catalytic oxidation under the action of a proper catalyst4Oxidative conversion to CO2And H2And O, the oxygen content in the coal bed gas can be reduced to be below 0.5 percent in the process, and the potential safety hazard in the operation process is thoroughly eliminated. Meanwhile, the process is simple and convenient to operate, automatic control and large-scale expansion are facilitated, equipment is simple, and the technology has a good commercial value in the aspect of economy. Catalytic deoxidation can be divided into two main categories, namely noble metal catalysts and non-noble metal catalysts according to active components of the catalysts.
The technology for researching the supported noble metal catalyst at home and abroad is mature. For example, rare earth cerium component with oxygen storage and release functions is added into a catalyst system for the large-scale ligation of Chinese academy of sciences to prepare the novel supported palladium noble metal catalyst, and the oxygen concentration in produced gas is within 0.1 percent and the oxygen conversion rate is higher than 96 percent after the deoxidation treatment of coal bed gas with the methane concentration of 39.15 percent and the oxygen concentration of 12.6 percent. Since the noble metal catalyst is expensive and has limited resources, the range of application is limited. And the non-noble metal oxide catalyst has low cost and easy availability, so the catalyst is greatly concerned. However, the non-noble metal is limited by activity, and the reaction needs to be carried out at a higher temperature, so that the energy consumption is higher.
Disclosure of Invention
Aiming at the defects of the prior art, the invention provides a catalytic combustion catalyst and a preparation method thereof. The catalyst is used for coal bed gas combustion and has the advantages of high activity, low reaction temperature, simple preparation method, low cost and the like.
A catalytic combustion catalyst comprises a composite oxide of zinc-supported alumina and molybdenum-supported ceric sulfate, wherein the weight ratio of the zinc-supported alumina to the molybdenum-supported ceric sulfate is 10:1-4:1, preferably 8:1-5:1, the content of zinc in terms of oxide is 5-25 wt%, preferably 10-20 wt%, based on the weight of the zinc-supported alumina, and the content of molybdenum in terms of oxide is 0.5-5 wt%, preferably 1-3 wt%, based on the weight of the molybdenum-supported ceric sulfate.
A preparation method of a coal bed gas catalytic combustion catalyst comprises the following steps: and kneading the zinc-loaded aluminum oxide and the molybdenum-loaded cerium acyl sulfate into a shape, drying and roasting to obtain the coal bed gas catalytic combustion catalyst.
In the above method, the zinc-supported alumina may be commercially available or prepared according to a conventional technique. The conventional technology is to load zinc on alumina, wherein the zinc is derived from one or more of zinc nitrate, zinc sulfate, zinc bromide and zinc chloride.
In the above method, the supported cerium molybdenum sulfate may be prepared by using commercially available products or according to conventional techniques. The conventional technology is that molybdenum is loaded on cerous sulfate, and the molybdenum is derived from molybdenum salt. The ceric acyl sulfate is prepared by adopting the prior art. A specific preparation method of ceryl sulfate, such as the preparation of ceryl sulfate by roasting at 300-500 ℃ for 1-10 h.
In the method, a proper amount of peptizing agent, pore-forming agent, metal auxiliary agent and the like can be added in the kneading process according to the needs.
In the method, the drying time is 1-5h, preferably 2-4h, the drying temperature is 90-150 ℃, preferably 100-; the roasting time is 3-8h, preferably 4-6h, and the temperature is 300-700 ℃, preferably 400-500 ℃.
In the above method, the zinc-loaded alumina is preferably prepared by immersing a zinc salt solution in alumina, and the zinc salt solution further contains at least one of 2, 5-dihydroxy-terephthalic acid and 1,3, 5-benzenetricarboxylic acid, and the mass content of at least one of 2, 5-dihydroxy-terephthalic acid and 1,3, 5-benzenetricarboxylic acid in the solution is 0.5 to 10%, preferably 2 to 7%. The 2, 5-dihydroxy-terephthalic acid or 1,3, 5-benzene tricarboxylic acid added into the mixed solution has stronger coordination effect with zinc ions, can improve the dispersion degree of zinc on alumina, and further improves the activity of the catalyst.
In the method, before kneading, the molybdenum-loaded ceryl sulfate is preferably treated by using a water vapor nitrogen mixed gas with the water vapor volume content of 0.5-5%, more preferably 1-4%, the treatment temperature is 100-. The molybdenum-loaded ceric sulfate treated by water vapor can improve the hydrophilicity of the zirconium sulfate surface, is beneficial to improving the dispersion degree of the zirconium sulfate in the catalyst in the kneading process, and improves the activity of the catalyst.
The research result shows that the coal bed gasThe mechanism of catalytic combustion is that methane is firstly dissociated into CH on the surface of the catalytic combustion catalystxSpecies of which x<4, then carrying out oxidation reaction with the adsorbed oxygen or lattice oxygen. This application will catalyze the burning catalyst and have the acyl cerium sulfate of the load molybdenum that methane activation ability is stronger, methane can activate on the acyl cerium sulfate of load molybdenum, and the methane species after the activation can overflow to the catalytic combustion catalyst on every side and react, burns more easily fast, has showing the activity that has improved the catalyst.
Detailed Description
The following examples are provided to further illustrate the effects and effects of the catalytic deoxidation catalyst for coal bed gas and the preparation method thereof, but the following examples are not intended to limit the invention, and the concentrations in the present application are volume concentrations unless otherwise specified. The ceric acid sulfate referred to in examples and comparative examples was prepared by calcining cerium sulfate at 350 ℃ for 3 hours.
Example 1
Mixing and kneading commercially available zinc-loaded alumina and commercially available molybdenum-loaded cerium acyl sulfate for molding, and drying and roasting to obtain the coal bed gas catalytic combustion catalyst, wherein the drying time is 4 hours and the drying temperature is 100 ℃; the roasting time is 6h, and the temperature is 400 ℃.
The catalyst properties were as follows: the weight ratio of the aluminum oxide loaded with zinc to the ceric sulfate loaded with molybdenum is 7:1, the content of zinc in oxide is 15wt% based on the weight of the aluminum oxide loaded with zinc, and the content of molybdenum in oxide is 2wt% based on the weight of the ceric sulfate loaded with molybdenum.
The catalyst performance is evaluated by taking coal bed methane deoxidation as a probe reaction, and the feed gas comprises the following components: CH (CH)420 vol%，O23vol%, the balance being N2. The reaction temperature is 430 ℃, and the volume space velocity is 16000 h-1After the reaction is stable, detecting O in tail gas at the outlet of the reactor by on-line chromatography2The concentration is 0.72 percent, and O in tail gas at the outlet of the reactor after 500 hours of operation2The concentration was 0.88%.
Example 2
Mixing and kneading commercially available zinc-loaded alumina and commercially available molybdenum-loaded cerium acyl sulfate for molding, and drying and roasting to obtain the coal bed gas catalytic combustion catalyst, wherein the drying time is 4 hours and the drying temperature is 100 ℃; the roasting time is 6h, and the temperature is 400 ℃.
The catalyst properties were as follows: the weight ratio of the aluminum oxide loaded with zinc to the ceric sulfate loaded with molybdenum is 8:1, the content of zinc in oxide is 10 wt% based on the weight of the aluminum oxide loaded with zinc, and the content of molybdenum in oxide is 3wt% based on the weight of the ceric sulfate loaded with molybdenum.
The catalyst performance is evaluated by taking coal bed methane deoxidation as a probe reaction, and the feed gas comprises the following components: CH (CH)420 vol%，O23vol%, the balance being N2. The reaction temperature is 430 ℃, and the volume space velocity is 16000 h-1After the reaction is stable, detecting O in tail gas at the outlet of the reactor by on-line chromatography2The concentration was 0.53%.
Example 3
Mixing and kneading commercially available zinc-loaded alumina and commercially available molybdenum-loaded cerium acyl sulfate for molding, and drying and roasting to obtain the coal bed gas catalytic combustion catalyst, wherein the drying time is 4 hours and the drying temperature is 100 ℃; the roasting time is 6h, and the temperature is 400 ℃.
The catalyst properties were as follows: the weight ratio of the aluminum oxide loaded with zinc to the ceric sulfate loaded with molybdenum is 5:1, the content of zinc in oxide is 20wt% based on the weight of the aluminum oxide loaded with zinc, and the content of molybdenum in oxide is 1wt% based on the weight of the ceric sulfate loaded with molybdenum.
The catalyst performance is evaluated by taking coal bed methane deoxidation as a probe reaction, and the feed gas comprises the following components: CH (CH)420 vol%，O23vol%, the balance being N2. The reaction temperature is 430 ℃, and the volume space velocity is 16000 h-1After the reaction is stable, detecting O in tail gas at the outlet of the reactor by on-line chromatography2The concentration was 0.58%.
Example 4
Kneading and molding self-made zinc-loaded alumina and commercially available molybdenum-loaded cerous sulfate, drying and roasting to obtain the coal bed gas catalytic combustion catalyst, wherein the drying time is 4 hours, and the drying temperature is 100 ℃; the roasting time is 6h, and the temperature is 400 ℃. The preparation process of the zinc-loaded alumina comprises the following steps: preparing a zinc nitrate aqueous solution containing 6 mass% of 2, 5-dihydroxy-terephthalic acid, impregnating the zinc nitrate aqueous solution with alumina, drying the impregnated alumina, and roasting the impregnated alumina, the rest being the same as in example 1.
The catalyst performance is evaluated by taking coal bed methane deoxidation as a probe reaction, and the feed gas comprises the following components: CH (CH)420 vol%，O23vol%, the balance being N2. The reaction temperature is 430 ℃, and the volume space velocity is 16000 h-1After the reaction is stable, detecting O in tail gas at the outlet of the reactor by on-line chromatography2The concentration was 0.08%.
Example 5
Kneading and molding self-made zinc-loaded alumina and commercially available molybdenum-loaded cerous sulfate, drying and roasting to obtain the coal bed gas catalytic combustion catalyst, wherein the drying time is 4 hours, and the drying temperature is 100 ℃; the roasting time is 6h, and the temperature is 400 ℃. The preparation process of the zinc-loaded alumina comprises the following steps: an aqueous solution of zinc nitrate containing 3% by mass of 1,3, 5-benzenetricarboxylic acid was prepared as in example 1.
The catalyst performance is evaluated by taking coal bed methane deoxidation as a probe reaction, and the feed gas comprises the following components: CH (CH)420 vol%，O23vol%, the balance being N2. The reaction temperature is 430 ℃, and the volume space velocity is 16000 h-1After the reaction is stable, detecting O in tail gas at the outlet of the reactor by on-line chromatography2The concentration was 0.15%.
Example 6
Compared with the example 1, the difference is that the commercially available molybdenum-loaded cerium acyl sulfate is treated by adopting a water vapor nitrogen mixed gas with the water vapor volume content of 1 percent before kneading, the treatment temperature is 180 ℃, and the treatment time is 3 min.
The catalyst performance is evaluated by taking coal bed methane deoxidation as a probe reaction, and the feed gas comprises the following components: CH (CH)420 vol%，O23vol%, the balance being N2. The reaction temperature is 430 ℃, and the volume space velocity is 16000 h-1After the reaction is stable, detecting O in tail gas at the outlet of the reactor by on-line chromatography2At a concentration of 0.65%, at the outlet of the reactor after 500h operationO in tail gas2The concentration was 0.68%.
Example 7
Compared with the example 1, the difference is that the commercially available molybdenum-loaded cerium acyl sulfate is treated by adopting a water vapor nitrogen mixed gas with the water vapor volume content of 4 percent before kneading, the treatment temperature is 120 ℃, and the treatment time is 10 min.
The catalyst performance is evaluated by taking coal bed methane deoxidation as a probe reaction, and the feed gas comprises the following components: CH (CH)420 vol%，O23vol%, the balance being N2. The reaction temperature is 430 ℃, and the volume space velocity is 16000 h-1After the reaction is stable, detecting O in tail gas at the outlet of the reactor by on-line chromatography2The concentration is 0.69 percent, and O in tail gas at the outlet of the reactor after 500 hours of operation2The concentration was 0.75%.
Example 8
The same procedure as in example 1 was repeated except that commercially available zinc-supporting alumina and commercially available cerium molybdenum sulfate-supporting were directly mixed. The catalyst performance is evaluated by taking coal bed methane deoxidation as a probe reaction, and the feed gas comprises the following components: CH (CH)420 vol%，O23vol%, the balance being N2. The reaction temperature is 430 ℃, and the volume space velocity is 16000 h-1After the reaction is stable, detecting O in tail gas at the outlet of the reactor by on-line chromatography2The concentration is 0.7 percent, and O in tail gas at the outlet of the reactor after 500 hours of operation2The concentration was 1.2%.
Claims (10)
1. A catalytic combustion catalyst characterized by: the catalyst contains a composite oxide of aluminum oxide loaded with zinc and ceryl sulfate loaded with molybdenum, the weight ratio of the aluminum oxide loaded with zinc to the ceryl sulfate loaded with molybdenum is 10:1-4:1, the content of zinc in oxide is 5-25 wt% based on the weight of the aluminum oxide loaded with zinc, and the content of molybdenum in oxide is 0.5-5 wt% based on the weight of the ceryl sulfate loaded with molybdenum.
2. The catalyst of claim 1, wherein: the weight ratio of the aluminum oxide loaded with zinc to the ceric sulfate loaded with molybdenum is 8:1-5:1, the content of zinc in oxide is 10-20 wt% based on the weight of the aluminum oxide loaded with zinc, and the content of molybdenum in oxide is 1-3 wt% based on the weight of the ceric sulfate loaded with molybdenum.
3. A method for preparing the catalyst of claim 1 or 2, characterized in that: the method comprises the following steps: and kneading the zinc-loaded aluminum oxide and the molybdenum-loaded cerium acyl sulfate into a shape, drying and roasting to obtain the coal bed gas catalytic combustion catalyst.
4. The method of claim 3, wherein: the zinc-loaded alumina or the molybdenum-loaded cerous sulfate is prepared by adopting a commercial product or according to a conventional technology.
5. The method of claim 4, wherein: the zinc-loaded aluminum oxide or molybdenum-loaded cerous sulfate is prepared by loading zinc or molybdenum on the aluminum oxide or the cerous sulfate, wherein the zinc is derived from one or more of zinc nitrate, zinc sulfate, zinc bromide and zinc chloride, and the molybdenum is derived from molybdenum salt.
6. The method of claim 3, wherein: and adding a peptizing agent, a pore-forming agent or a metal auxiliary agent according to the requirement in the kneading process.
7. The method of claim 3, wherein: the drying time is 1-5h, and the drying temperature is 90-150 ℃; the roasting time is 3-8h, and the temperature is 300-700 ℃.
8. The method of claim 7, wherein: the drying time is 2-4h, and the drying temperature is 100-130 ℃; the roasting time is 4-6h, and the temperature is 400-500 ℃.
9. The method of claim 3, wherein: the zinc-loaded aluminum oxide is prepared by dipping a zinc salt solution on aluminum oxide, wherein the zinc salt mixed solution contains at least one of 2, 5-dihydroxy-terephthalic acid or 1,3, 5-benzene tricarboxylic acid, and the mass content of at least one of 2, 5-dihydroxy-terephthalic acid or 1,3, 5-benzene tricarboxylic acid in the mixed solution is 0.5-10%.
10. The method of claim 3, wherein: before kneading, the molybdenum-loaded ceric sulfate is treated by adopting water vapor nitrogen mixed gas with the water vapor volume content of 0.5-5%, the treatment temperature is 100-.
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Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US6811758B1 (en) * | 1999-02-16 | 2004-11-02 | European Community, Represented By The Commision Of The European Communities | Precipitation process |
| CN102784639A (en) * | 2012-08-28 | 2012-11-21 | 新地能源工程技术有限公司 | Coal-bed methane deoxidization catalyst and preparation method and application of coal-bed methane deoxidization catalyst |
| CN103920507A (en) * | 2013-01-15 | 2014-07-16 | 南京工业大学 | Catalyst for oxidation of hydrogen chloride to prepare chlorine and application thereof |
| CN107051439A (en) * | 2017-05-31 | 2017-08-18 | 福州大学 | One kind is used for oil field association exhaust combustion catalyst and its preparation method and application |
| CN108067263A (en) * | 2016-11-11 | 2018-05-25 | 中国石油化工股份有限公司抚顺石油化工研究院 | A kind of catalyst with core-shell structure and its preparation method and application |
-
2019
- 2019-05-05 CN CN201910365847.2A patent/CN111889116B/en active Active
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US6811758B1 (en) * | 1999-02-16 | 2004-11-02 | European Community, Represented By The Commision Of The European Communities | Precipitation process |
| CN102784639A (en) * | 2012-08-28 | 2012-11-21 | 新地能源工程技术有限公司 | Coal-bed methane deoxidization catalyst and preparation method and application of coal-bed methane deoxidization catalyst |
| CN103920507A (en) * | 2013-01-15 | 2014-07-16 | 南京工业大学 | Catalyst for oxidation of hydrogen chloride to prepare chlorine and application thereof |
| CN108067263A (en) * | 2016-11-11 | 2018-05-25 | 中国石油化工股份有限公司抚顺石油化工研究院 | A kind of catalyst with core-shell structure and its preparation method and application |
| CN107051439A (en) * | 2017-05-31 | 2017-08-18 | 福州大学 | One kind is used for oil field association exhaust combustion catalyst and its preparation method and application |
Non-Patent Citations (1)
| Title |
|---|
| 邵芸等: "甲烷制卤代甲烷研究进展", 《工业催化》 * |
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Effective date of registration: 20231110 Address after: 100728 No. 22 North Main Street, Chaoyang District, Beijing, Chaoyangmen Patentee after: CHINA PETROLEUM & CHEMICAL Corp. Patentee after: Sinopec (Dalian) Petrochemical Research Institute Co.,Ltd. Address before: 100728 No. 22 North Main Street, Chaoyang District, Beijing, Chaoyangmen Patentee before: CHINA PETROLEUM & CHEMICAL Corp. Patentee before: DALIAN RESEARCH INSTITUTE OF PETROLEUM AND PETROCHEMICALS, SINOPEC Corp. |