A process for the integrated dehydrogenation of propane coupled with hydrogen combustion
By introducing a hydrophobic catalyst into the propane dehydrogenation process, and combining catalytic dehydrogenation with hydrogen combustion, the problems of short single dehydrogenation cycles and high energy consumption were solved, achieving efficient propane conversion and energy utilization, and improving the economics of the process.
Patent Information
- Authority / Receiving Office
- CN · China
- Patent Type
- Patents(China)
- Current Assignee / Owner
- NINGXIA UNIVERSITY
- Filing Date
- 2022-11-15
- Publication Date
- 2026-07-07
Smart Images
Figure CN115709035B_ABST
Abstract
Description
Technical Field
[0001] This invention relates to propane dehydrogenation, and more specifically to an integrated propane dehydrogenation process that couples catalytic dehydrogenation and hydrogen combustion. Background Technology
[0002] Propylene, as an important petrochemical intermediate, is widely used in the production of chemical products such as polypropylene, acrylonitrile, and ethylene oxide. In recent years, China's consumption of propylene and its downstream derivatives has continued to grow. Traditional routes for producing propylene from naphtha cracking and catalytic cracking as a byproduct cannot meet the demand for propylene feedstock in chemical production. Propane dehydrogenation to propylene, however, has seen rapid development due to its shorter process flow, lower equipment investment, and better economics. Propane catalytic dehydrogenation is an endothermic reaction involving an increase in the number of molecules, resulting in high energy consumption, chemical equilibrium limitations, and low single-pass conversion rates. While oxidative dehydrogenation, which converts hydrogen from activated propane to water, is exothermic and its conversion rate is not limited by equilibrium conversion rates, it completely converts high-value-added hydrogen to water, and due to excessive oxidation, propylene has low selectivity (CN114849770A).
[0003] There are numerous propane dehydrogenation processes globally, including the Catofin process developed by ABB Lummus, the Oleflex process developed by UOP, the STAR process developed by ThyssenKrupp, and the PDH process developed by Linde, BASF, and Statoil, among others. According to Chinese patent CN109651047B, UOP's Oleflex process and Lummus's Catofin process are currently widely used in industrial propane dehydrogenation to propylene. The Oleflex process uses a Pt / Al2O3 catalyst, achieving a propane single-pass conversion of 35%-40% and a propylene selectivity of 84%-89% under operating conditions of 600℃-700℃ and greater than 0.1MPa (CN96117222.3, US4438288). The Catofin process uses a Cr2O3 / Al2O3 catalyst, achieving a propane single-pass conversion of 45%-50% and a selectivity greater than 88% under conditions of 540-640℃ and greater than 0.05MPa (CN200910012450.1, CN200610126812.6).
[0004] While the Oleflex and Catofin processes have been industrialized, some problems still exist. Taking the Catofin process as an example, it includes reduction, dehydrogenation, purging, and coke regeneration. Propane undergoes dehydrogenation in an adiabatic bed (590-600℃). As the bed temperature decreases (560-580℃), coke burning is necessary to raise the bed temperature and burn off a small amount of coke deposited on the catalyst. A single dehydrogenation cycle takes only about 9 minutes (CN115073156A), significantly impacting the reactor's effective production time. Furthermore, propane and propylene in the dehydrogenation products are separated using cryogenic distillation, resulting in high energy consumption. The single-pass conversion rate of propane significantly affects the energy consumption of the dehydrogenation process (CN113372189A).
[0005] Propane dehydrogenation coupled with hydrogen combustion can remove some of the hydrogen from the products through catalytic combustion, breaking the thermodynamic equilibrium of the reaction, and can also use the heat generated by hydrogen combustion for the propane dehydrogenation reaction, saving energy. Through multiple reactors connected in series, the reactants first pass through the first dehydrogenation reactor, and the gaseous mixture after the reaction (including propane, propylene, hydrogen, ethane, ethylene, etc.) enters the hydrogen selective oxidation reactor for hydrogen combustion. After the reaction, it enters the next stage dehydrogenation reactor. Although the hydrogen combustion process in this method has a relatively mild environment, the overall process flow is complex (Hu Rui. Simulation and Optimization of Propane Dehydrogenation and Hydrogen Selective Oxidation Coupled Process).
[0006] Based on the current status of propane dehydrogenation processes, a new propane dehydrogenation process that couples the dehydrogenation and hydrogen combustion processes in a single reactor, achieving self-heating reaction, by-product hydrogen production, high single-pass conversion rate, and long single-pass dehydrogenation cycle, plays an important role in reducing energy consumption and improving economic efficiency. Summary of the Invention
[0007] To address the technical problems of existing technologies, such as short single-pass dehydrogenation cycle, high reaction energy consumption, and low single-pass conversion, this invention provides an integrated propane dehydrogenation process that couples catalytic dehydrogenation and hydrogen combustion.
[0008] The propane dehydrogenation integrated process of the present invention, which combines coupled catalytic dehydrogenation and hydrogen combustion, introduces a propane dehydrogenation-hydrogenation catalyst into the propane dehydrogenation reaction.
[0009] Furthermore, the propane dehydrogenation-hydrogenation catalyst is composed of a propane dehydrogenation component, a hydrogenation active component, and a hydrophobic component; the dehydrogenation component is an oxygen-rich metal oxide or a metal composite oxide, which does not require hydrogen reduction before the reaction; the hydrogenation component is a metal oxide that catalyzes hydrogen combustion; the hydrophobicity can be achieved by hydrophobic modification or by adding a hydrophobic component.
[0010] Furthermore, the propane dehydrogenation component is one of Ga2O3 / Al2O3 or Cr2O3 / Al2O3.
[0011] Furthermore, the active components for propane dehydrogenation (such as Ga2O3 / Al2O3 and Cr2O3 / Al2O3) are Ga2O3 and CrO3, respectively. x The mass of the catalyst is 0.001-60 wt% of the total mass of the propane dehydrogenation-hydrogenation catalyst; preferably 10-50 wt%.
[0012] Furthermore, the hydrogen-burning active component is one or more of the metal oxides corresponding to group IIIB-VIIB elements or group IIIA-VA elements.
[0013] Furthermore, the metal oxides corresponding to the group IIIB-VIIB elements are selected from La2O3, CeO2, WO3, and Ce. 0.75 Cr 0.25 O2, WO3 / SiO2 or LaMnO3.
[0014] Furthermore, the metal oxides corresponding to the group IIIA-VA elements are selected from In2O3, Bi2O3, In2O3 / SiO2, Bi2O3 / SiO2, and Bi2Mo3O. 12 Or In2O2Mo3O 12 .
[0015] Furthermore, the mass of the hydrogen-burning active component accounts for 0.001-50 wt% of the total mass of the propane dehydrogenation-hydrogenation catalyst.
[0016] Furthermore, the hydrophobic component is one of hydrophobic graphite, graphene, or SiO2.
[0017] Furthermore, the propane dehydrogenation reaction is carried out according to a conventional propane dehydrogenation process, for example, it can be carried out according to the following steps:
[0018] (1) The propane dehydrogenation reaction is carried out in a fixed bed, which serves as the dehydrogenation reactor;
[0019] (2) The dehydrogenation reaction temperature is 570-630℃ (preferably 580-620℃, more preferably 590-610℃). If the dehydrogenation reaction temperature is too high, the catalyst will sinter. If the temperature is too low, the dehydrogenation activity will be low. Both too high and too low temperatures will result in low dehydrogenation efficiency.
[0020] (3) The dehydrogenation reaction pressure is 0.8-1.2 MPa (preferably 0.4-0.8 MPa, more preferably 0-0.4 MPa). Propane dehydrogenation is a reversible reaction with an increase in the number of molecules, and low pressure is conducive to the forward reaction.
[0021] The catalyst of this invention has the functions of both propane catalytic dehydrogenation and selective hydrogen combustion. If only the hydrogen combustion catalyst and the propane dehydrogenation catalyst are mixed, the effect is not ideal. During the experiment, the inventors accidentally discovered that by adding hydrophobic components or making hydrophobic modifications, and then mixing the two catalysts, the single-pass conversion rate of propane dehydrogenation can be significantly improved, and very good results can be obtained.
[0022] The beneficial effects of this invention are as follows:
[0023] (1) Reduce the partial pressure of hydrogen at the end of the reactor, improve the single-pass conversion rate of propane dehydrogenation, and reduce the energy consumption of product separation;
[0024] (2) By introducing heat through hydrogen burning, the temperature drop of the catalyst bed is slowed down, and the single dehydrogenation cycle of propane dehydrogenation is extended.
[0025] (3) Adjust the depth of hydrogen combustion and control the heat release of the hydrogen combustion reaction, transforming the integrated process into a self-heating process while producing hydrogen as a byproduct.
[0026] (4) The catalyst can react without hydrogen reduction, simplifying the process. Attached Figure Description
[0027] Figure 1 This is a simplified diagram of the integrated propane dehydrogenation process of the present invention, which couples catalytic dehydrogenation and hydrogen combustion. Detailed Implementation
[0028] The present invention will be further described in detail through the following embodiments, but the present invention is not limited to these embodiments.
[0029] The propane dehydrogenation reaction examples and comparative examples of the present invention adopted a fixed-bed continuous reaction process, with a catalyst loading of 3g, and the product was subjected to chromatographic analysis every 1 hour.
[0030] The specific implementation scheme of the present invention is summarized as follows:
[0031] Example 1
[0032] Preparation of hydrogen combustion catalyst (i.e., hydrogen combustion catalyst): First, 0.005 mol of sodium molybdate was added to 60 ml of deionized water and magnetically stirred until a clear solution A was obtained. Then, 0.01 mol of indium nitrate hydrate was added to 20 ml of deionized water and magnetically stirred until a clear solution B was obtained. Solution B was added to solution A and stirred for 60 min. Then, 0.001 mol of hexadecyltrimethylammonium bromide was added and stirred for 30 min. The resulting precursor suspension was transferred to a 100 ml polytetrafluoroethylene-lined stainless steel autoclave, heated to 180°C, maintained for 24 hours, and then naturally cooled to room temperature. The obtained sample was centrifuged, washed alternately with deionized water and ethanol, dried in an 80°C oven, and finally calcined in a muffle furnace at 600°C for 6 h to obtain In₂Mo₃O. 12 .
[0033] Preparation of propane dehydrogenation catalyst: 1.00 g alumina support was added to 30 ml deionized water, 0.3 g hydrated gallium nitrate was added and dissolved by ultrasonication, then stirred and impregnated for 8 h. After impregnation, it was dried in an 80 °C oven and finally calcined in a muffle furnace at 600 °C for 6 h to obtain 10% Ga2O3 / Al2O3.
[0034] The hydrophobic component of the catalyst is hydrophobic graphite.
[0035] Propane dehydrogenation component, hydrogen oxidizing component and hydrophobic graphite are coupled and shaped in a physical mixing manner for use.
[0036] The reaction process is as follows: using the above catalyst, propane (35 mL / min) and argon (25 mL / min) are introduced, the reaction temperature is 600℃, and the reaction pressure is 0.1 MPa.
[0037] Comparative Example 1
[0038] Preparation of hydrogen combustion catalyst: First, 0.005 mol sodium molybdate was added to 60 ml of deionized water and magnetically stirred until a clear solution A was obtained. Then, 0.01 mol indium nitrate hydrate was added to 20 ml of deionized water and magnetically stirred until a clear solution B was obtained. Solution B was added to solution A and stirred for 60 min. Then, 0.001 mol hexadecyltrimethylammonium bromide was added and stirred for 30 min. The resulting precursor suspension was transferred to a 100 ml polytetrafluoroethylene-lined stainless steel autoclave, heated to 180°C, maintained for 24 hours, and then naturally cooled to room temperature. The obtained sample was centrifuged, washed alternately with deionized water and ethanol, dried in an 80°C oven, and finally calcined in a muffle furnace at 600°C for 6 h to obtain In₂Mo₃O. 12 .
[0039] Preparation of propane dehydrogenation catalyst: 1.00 g alumina support was added to 30 ml deionized water, 0.3 g hydrated gallium nitrate was added and dissolved by ultrasonication, then stirred and impregnated for 8 h. After impregnation, it was dried in an 80 °C oven and finally calcined in a muffle furnace at 600 °C for 6 h to obtain 10% Ga2O3 / Al2O3.
[0040] The propane dehydrogenation component and the hydrogen calcination component are coupled and shaped in a physical mixing manner for use. That is, unlike Example 1, it does not contain hydrophobic components.
[0041] The reaction process is as follows: using the above catalyst, propane (35 mL / min) and argon (25 mL / min) are introduced, the reaction temperature is 600℃, and the reaction pressure is 0.1 MPa.
[0042] Example 2
[0043] Preparation of hydrogen combustion catalyst: First, 0.005 mol of sodium molybdate was added to 60 ml of deionized water and magnetically stirred until a clear solution A was obtained. Then, 0.01 mol of bismuth nitrate hydrate was added to 20 ml of deionized water and magnetically stirred until a clear solution B was obtained. Solution B was added to solution A and stirred for 60 min. Then, 0.001 mol of hexadecyltrimethylammonium bromide was added and stirred for 30 min. The resulting precursor suspension was transferred to a 100 ml PTFE-lined stainless steel autoclave, heated to 180°C, maintained for 24 hours, and then naturally cooled to room temperature. The obtained sample was centrifuged, washed alternately with deionized water and ethanol, dried in an 80°C oven, and finally calcined in a muffle furnace at 600°C for 6 h to obtain Bi₂Mo₃O. 12 .
[0044] Preparation of propane dehydrogenation catalyst: 1.00 g alumina support was added to 30 ml deionized water, 0.3 g hydrated gallium nitrate was added and dissolved by ultrasonication, then stirred and impregnated for 8 h. After impregnation, it was dried in an 80 °C oven and finally calcined in a muffle furnace at 600 °C for 6 h to obtain 10% Ga2O3 / Al2O3.
[0045] The hydrophobic component of the catalyst is hydrophobic graphite.
[0046] Propane dehydrogenation component, hydrogen oxidizing component and hydrophobic graphite are coupled and shaped in a physical mixing manner for use.
[0047] The reaction process is as follows: using the above catalyst, propane (35 mL / min) and argon (25 mL / min) are introduced, the reaction temperature is 600℃, and the reaction pressure is 0.1 MPa.
[0048] Comparative Example 2
[0049] Preparation of hydrogen combustion catalyst: First, 0.005 mol of sodium molybdate was added to 60 ml of deionized water and magnetically stirred until a clear solution A was obtained. Then, 0.01 mol of bismuth nitrate hydrate was added to 20 ml of deionized water and magnetically stirred until a clear solution B was obtained. Solution B was added to solution A and stirred for 60 min. Then, 0.001 mol of hexadecyltrimethylammonium bromide was added and stirred for 30 min. The resulting precursor suspension was transferred to a 100 ml PTFE-lined stainless steel autoclave, heated to 180°C, maintained for 24 hours, and then naturally cooled to room temperature. The obtained sample was centrifuged, washed alternately with deionized water and ethanol, dried in an 80°C oven, and finally calcined in a muffle furnace at 600°C for 6 h to obtain Bi₂Mo₃O. 12 .
[0050] Preparation of propane dehydrogenation catalyst: 1.00 g of alumina support was added to 30 ml of deionized water, 0.3 g of hydrated gallium nitrate was added and dissolved by ultrasonication, then stirred and impregnated for 8 h. After impregnation, it was dried in an 80 °C oven and finally calcined in a muffle furnace at 600 °C for 6 h to obtain 10% Ga2O3 / Al2O3. The mass percentage of the active component was 0.001-60 wt%, preferably 10-50%.
[0051] The propane dehydrogenation component and the hydrogen calcination component are coupled and shaped in a physical mixing manner for use. That is, unlike Example 2, it does not contain hydrophobic components.
[0052] The reaction process is as follows: using the above catalyst, propane (35 mL / min) and argon (25 mL / min) are introduced, the reaction temperature is 600℃, and the reaction pressure is 0.1 MPa.
[0053] Example 3
[0054] The hydrogen combustion catalyst is In2O3.
[0055] Preparation of propane dehydrogenation catalyst: 1.00 g alumina support was added to 30 ml deionized water, 0.3 g hydrated gallium nitrate was added and dissolved by ultrasonication, then stirred and impregnated for 8 h. After impregnation, it was dried in an 80 °C oven and finally calcined in a muffle furnace at 600 °C for 6 h to obtain 10% Ga2O3 / Al2O3.
[0056] The hydrophobic component of the catalyst is hydrophobic graphite.
[0057] Propane dehydrogenation component, hydrogen oxidizing component and hydrophobic graphite are coupled and shaped in a physical mixing manner for use.
[0058] The reaction process is as follows: using the above catalyst, propane (35 mL / min) and argon (25 mL / min) are introduced, the reaction temperature is 600℃, and the reaction pressure is 0.1 MPa.
[0059] Comparative Example 3
[0060] The hydrogen combustion catalyst is In2O3.
[0061] Preparation of propane dehydrogenation catalyst: 1.00 g of alumina support was added to 30 ml of deionized water, 0.3 g of hydrated gallium nitrate was added and dissolved by ultrasonication, then stirred and impregnated for 8 h. After impregnation, it was dried in an 80 °C oven and finally calcined in a muffle furnace at 600 °C for 6 h to obtain 10% Ga2O3 / Al2O3. The mass percentage of the active component was 0.001-60 wt%, preferably 10-50%.
[0062] The propane dehydrogenation component and the hydrogen calcination component are coupled and shaped in a physical mixing manner for use. That is, unlike Example 3, it does not contain hydrophobic components.
[0063] The reaction process is as follows: using the above catalyst, propane (35 mL / min) and argon (25 mL / min) are introduced, the reaction temperature is 600℃, and the reaction pressure is 0.1 MPa.
[0064] Example 4
[0065] The hydrogen combustion catalyst is Bi2O3.
[0066] Preparation of propane dehydrogenation catalyst: 1.00 g alumina support was added to 30 ml deionized water, 0.3 g hydrated gallium nitrate was added and dissolved by ultrasonication, then stirred and impregnated for 8 h. After impregnation, it was dried in an 80 °C oven and finally calcined in a muffle furnace at 600 °C for 6 h to obtain 10% Ga2O3 / Al2O3.
[0067] The hydrophobic component of the catalyst is hydrophobic graphite.
[0068] Propane dehydrogenation component, hydrogen oxidizing component and hydrophobic graphite are coupled and shaped in a physical mixing manner for use.
[0069] The reaction process is as follows: using the above catalyst, propane (35 mL / min) and argon (25 mL / min) are introduced, the reaction temperature is 600℃, and the reaction pressure is 0.1 MPa.
[0070] Comparative Example 4
[0071] The hydrogen combustion catalyst is Bi2O3.
[0072] Preparation of propane dehydrogenation catalyst: 1.00 g alumina support was added to 30 ml deionized water, 0.3 g hydrated gallium nitrate was added and dissolved by ultrasonication, then stirred and impregnated for 8 h. After impregnation, it was dried in an 80 °C oven and finally calcined in a muffle furnace at 600 °C for 6 h to obtain 10% Ga2O3 / Al2O3.
[0073] The propane dehydrogenation component and the hydrogen calcination component are coupled and shaped in a physical mixing manner for use. That is, unlike Example 4, it does not contain hydrophobic components.
[0074] The reaction process is as follows: using the above catalyst, propane (35 mL / min) and argon (25 mL / min) are introduced, the reaction temperature is 600℃, and the reaction pressure is 0.1 MPa.
[0075] Example 5
[0076] The hydrogen combustion catalyst is In2O3.
[0077] Preparation of propane dehydrogenation catalyst (with hydrophobic treatment): 1.00 g of alumina support was added to 30 ml of deionized water, along with 0.3 g of hydrated gallium nitrate, and dissolved by ultrasonication. The mixture was then stirred and impregnated for 8 h. After impregnation, it was dried in an 80 °C oven and finally calcined in a muffle furnace at 600 °C for 6 h to obtain 10% Ga2O3 / Al2O3. 0.3 g of 10% Ga2O3 / Al2O3 was accurately weighed into a beaker, and 40 mL of ethanol and 2 mL of concentrated ammonia were added. After mixing thoroughly, 20 mL of LTEOS was added and the mixture was stirred vigorously for 12 h. After stirring, the solid was centrifuged and washed repeatedly with alternating water and ethanol. It was then dried in an 80 °C oven and finally calcined in a muffle furnace at 600 °C for 6 h to obtain 5% SiO2@10% Ga2O3 / Al2O3.
[0078] The propane dehydrogenation component and the hydrogen calcination component are coupled and shaped by physical mixing for use.
[0079] The reaction process is as follows: using the above catalyst, propane (35 mL / min) and argon (25 mL / min) are introduced, the reaction temperature is 600℃, and the reaction pressure is 0.1 MPa.
[0080] Comparative Example 5
[0081] The hydrogen combustion catalyst is In2O3.
[0082] Preparation of propane dehydrogenation catalyst: 1.00 g alumina support was added to 30 ml deionized water, 0.3 g hydrated gallium nitrate was added and dissolved by ultrasonication, then stirred and impregnated for 8 h. After impregnation, it was dried in an 80 °C oven and finally calcined in a muffle furnace at 600 °C for 6 h to obtain 10% Ga2O3 / Al2O3.
[0083] The propane dehydrogenation component and the hydrogen calcination component are coupled and shaped by physical mixing for use.
[0084] The reaction process is as follows: using the above catalyst, propane (35 mL / min) and argon (25 mL / min) are introduced, the reaction temperature is 600℃, and the reaction pressure is 0.1 MPa.
[0085] Example 6
[0086] The hydrogen combustion catalyst is Bi2O3.
[0087] Preparation of propane dehydrogenation catalyst (with hydrophobic treatment): 1.00 g of alumina support was added to 30 ml of deionized water, along with 0.3 g of hydrated gallium nitrate, and dissolved by ultrasonication. The mixture was then stirred and impregnated for 8 h. After impregnation, it was dried in an 80 °C oven and finally calcined in a muffle furnace at 600 °C for 6 h to obtain 10% Ga2O3 / Al2O3. 0.3 g of 10% Ga2O3 / Al2O3 was accurately weighed into a beaker, and 40 mL of ethanol and 2 mL of concentrated ammonia were added. After mixing thoroughly, 20 mL of LTEOS was added and the mixture was stirred vigorously for 12 h. After stirring, the solid was centrifuged and washed repeatedly with alternating water and ethanol. It was then dried in an 80 °C oven and finally calcined in a muffle furnace at 600 °C for 6 h to obtain 5% SiO2@10% Ga2O3 / Al2O3.
[0088] The propane dehydrogenation component and the hydrogen calcination component are coupled and shaped by physical mixing for use.
[0089] The reaction process is as follows: using the above catalyst, propane (35 mL / min) and argon (25 mL / min) are introduced, the reaction temperature is 600℃, and the reaction pressure is 0.1 MPa.
[0090] Comparative Example 6
[0091] The hydrogen combustion catalyst is Bi2O3.
[0092] Preparation of propane dehydrogenation catalyst: 1.00 g alumina support was added to 30 ml deionized water, 0.3 g hydrated gallium nitrate was added and dissolved by ultrasonication, then stirred and impregnated for 8 h. After impregnation, it was dried in an 80 °C oven and finally calcined in a muffle furnace at 600 °C for 6 h to obtain 10% Ga2O3 / Al2O3.
[0093] The propane dehydrogenation component and the hydrogen calcination component are coupled and shaped by physical mixing for use.
[0094] The reaction process is as follows: using the above catalyst, propane (35 mL / min) and argon (25 mL / min) are introduced, the reaction temperature is 600℃, and the reaction pressure is 0.1 MPa.
[0095] Comparative Example 7
[0096] Preparation of propane dehydrogenation catalyst: 1.00 g alumina support was added to 30 ml deionized water, 0.3 g hydrated gallium nitrate was added and dissolved by ultrasonication, then stirred and impregnated for 8 h. After impregnation, it was dried in an 80 °C oven and finally calcined in a muffle furnace at 600 °C for 6 h to obtain 10% Ga2O3 / Al2O3.
[0097] The reaction process is as follows: using the above catalyst, propane (35 mL / min) and argon (25 mL / min) are introduced, the reaction temperature is 600℃, and the reaction pressure is 0.1 MPa.
[0098] The reaction results of the above embodiments and comparative examples are shown in Table 1.
[0099]
[0100] Table 1 shows that the present invention significantly improves the conversion rate of propane and the selectivity of propylene by introducing a hydrophobic propane dehydrogenation-hydrogenation catalyst into the propane dehydrogenation reaction. However, the reaction results of Comparative Examples 6 and 7 indicate that if only the propane dehydrogenation component and the hydrogenation component are coupled without introducing a hydrophobic component or undergoing hydrophobic treatment, the introduction of the hydrogenation component actually severely hinders the propane dehydrogenation effect. Therefore, the effect of direct coupling between the propane dehydrogenation component and the hydrogenation component is significantly weaker than the case where only the propane dehydrogenation component is present.
Claims
1. An integrated propane dehydrogenation process coupling catalytic dehydrogenation and hydrogen combustion, characterized in that, A propane dehydrogenation-hydrogenation catalyst is introduced into the propane dehydrogenation reaction; the propane dehydrogenation-hydrogenation catalyst is composed of a propane dehydrogenation component, a hydrogenation active component, and a hydrophobic component; the propane dehydrogenation component is one of Ga2O3 / Al2O3 and Cr2O3 / Al2O3; the mass of the propane dehydrogenation active component accounts for 0.001-60 wt% of the total mass of the propane dehydrogenation-hydrogenation catalyst; the hydrophobic component is graphite or graphene.
2. The propane dehydrogenation integrated process of coupled catalytic dehydrogenation and hydrogen combustion according to claim 1, characterized in that, The active component for hydrogen calcination is one or more of the metal oxides corresponding to elements in groups IIIB-VIIB or group IIIA-VA.
3. The propane dehydrogenation integrated process of coupled catalytic dehydrogenation and hydrogen combustion according to claim 1, characterized in that, The active component for hydrogenation is selected from WO3.
4. The integrated propane dehydrogenation process of coupled catalytic dehydrogenation and hydrogen combustion according to claim 1, characterized in that, The hydrogen-burning active component is selected from In2O3, Bi2O3, and Bi2Mo3O. 12 or In2Mo3O 12 .
5. The integrated propane dehydrogenation process of coupled catalytic dehydrogenation and hydrogen combustion according to claim 1, characterized in that, The mass of the hydrogen-burning active component accounts for 0.001-50 wt% of the total mass of the propane dehydrogenation-hydrogenation catalyst.