CN116459743A - Electrocatalytic cracking device and electrocatalytic cracking method for petroleum hydrocarbon - Google Patents
Electrocatalytic cracking device and electrocatalytic cracking method for petroleum hydrocarbon Download PDFInfo
- Publication number
- CN116459743A CN116459743A CN202310313239.3A CN202310313239A CN116459743A CN 116459743 A CN116459743 A CN 116459743A CN 202310313239 A CN202310313239 A CN 202310313239A CN 116459743 A CN116459743 A CN 116459743A
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- pipe
- electric heater
- steam
- settler
- catalyst
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- 239000003209 petroleum derivative Substances 0.000 title claims description 23
- 238000005336 cracking Methods 0.000 title claims description 18
- 238000000034 method Methods 0.000 title claims description 13
- 239000003054 catalyst Substances 0.000 claims abstract description 77
- 239000007921 spray Substances 0.000 claims abstract description 35
- 238000004523 catalytic cracking Methods 0.000 claims abstract description 13
- 239000002994 raw material Substances 0.000 claims abstract description 13
- 239000003208 petroleum Substances 0.000 claims abstract description 3
- 238000006243 chemical reaction Methods 0.000 claims description 22
- 238000005485 electric heating Methods 0.000 claims description 13
- 239000007789 gas Substances 0.000 claims description 13
- 238000000197 pyrolysis Methods 0.000 claims description 11
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 7
- 239000003546 flue gas Substances 0.000 claims description 7
- 238000006477 desulfuration reaction Methods 0.000 claims description 4
- 230000023556 desulfurization Effects 0.000 claims description 4
- 230000008929 regeneration Effects 0.000 claims description 4
- 238000011069 regeneration method Methods 0.000 claims description 4
- 238000000926 separation method Methods 0.000 claims description 3
- 229930195733 hydrocarbon Natural products 0.000 claims 1
- 150000002430 hydrocarbons Chemical class 0.000 claims 1
- 230000035484 reaction time Effects 0.000 claims 1
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 abstract description 8
- 239000001569 carbon dioxide Substances 0.000 abstract description 4
- 229910002092 carbon dioxide Inorganic materials 0.000 abstract description 4
- 239000000047 product Substances 0.000 description 17
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 5
- 229910052799 carbon Inorganic materials 0.000 description 5
- 239000002803 fossil fuel Substances 0.000 description 5
- 239000000446 fuel Substances 0.000 description 5
- 239000000571 coke Substances 0.000 description 4
- 238000009826 distribution Methods 0.000 description 3
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 2
- 238000002485 combustion reaction Methods 0.000 description 2
- 239000002283 diesel fuel Substances 0.000 description 2
- 230000007613 environmental effect Effects 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 239000001993 wax Substances 0.000 description 2
- VXNZUUAINFGPBY-UHFFFAOYSA-N 1-Butene Chemical compound CCC=C VXNZUUAINFGPBY-UHFFFAOYSA-N 0.000 description 1
- 239000005662 Paraffin oil Substances 0.000 description 1
- IAQRGUVFOMOMEM-UHFFFAOYSA-N butene Natural products CC=CC IAQRGUVFOMOMEM-UHFFFAOYSA-N 0.000 description 1
- 239000007795 chemical reaction product Substances 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000005611 electricity Effects 0.000 description 1
- 238000004134 energy conservation Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- -1 ethylene, propylene Chemical group 0.000 description 1
- 239000003502 gasoline Substances 0.000 description 1
- 238000012432 intermediate storage Methods 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 239000003921 oil Substances 0.000 description 1
- 239000012188 paraffin wax Substances 0.000 description 1
- 239000001294 propane Substances 0.000 description 1
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 description 1
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 description 1
- 238000002407 reforming Methods 0.000 description 1
- 239000002893 slag Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 239000002699 waste material Substances 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
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/005—Separating solid material from the gas/liquid stream
- B01J8/0075—Separating solid material from the gas/liquid stream by electrostatic precipitation
-
- 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
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/08—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with moving particles
- B01J8/082—Controlling processes
-
- 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
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/08—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with moving particles
- B01J8/085—Feeding reactive fluids
-
- 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
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/08—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with moving particles
- B01J8/12—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with moving particles moved by gravity in a downward flow
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G11/00—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
- C10G11/02—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils characterised by the catalyst used
Abstract
The invention relates to the technical field of petroleum processing, in particular to an electric catalytic cracking device, which comprises a regenerator and a settler, wherein the regenerator is provided with a regenerated catalyst outlet and a spent catalyst inlet, the bottom of the regenerator is provided with a main air pipe, the main air pipe is connected with a main fan, and a first electric heater is arranged in the main air pipe; the bottom of the settler is connected with a spent catalyst inlet, a second electric heater is arranged in the settler, a steam spray pipe is wrapped outside the second electric heater, the steam spray pipe is communicated with a steam air supply pipe, a plurality of steam spray holes are arranged on the steam spray pipe, steam flows in a space formed by the second electric heater and the inner wall of the steam spray pipe, and is sprayed out by the steam spray holes; the regenerated catalyst outlet is connected with a lifting pipe, the lifting pipe is provided with a raw material inlet, the lifting pipe extends into the settler from the bottom of the settler, the lifting pipe is provided with an outlet, and the outlet is arranged above the second electric heater. The invention has less equipment investment and simultaneously reduces the carbon dioxide emission.
Description
Technical Field
The invention relates to the technical field of petroleum processing, in particular to an electrocatalytic cracking device and an electrocatalytic cracking method for petroleum hydrocarbon.
Background
In the traditional catalytic cracking and cracking device reaction system in petrochemical industry, a regenerator provides required heat for catalytic cracking or cracking reaction through the scorching heat release of fossil raw materials, so that a large amount of carbon dioxide emission and fuel consumption are caused. With the increasing demand of chemical raw materials such as propane, propylene, butene and the like in society, catalytic cracking devices for producing more oil products are required to convert to catalytic cracking, so that higher reaction temperature and lighter raw materials are required, the lighter raw materials mean insufficient burning heat of the catalytic cracking devices, and the higher reaction temperature also means more heat. By adopting the existing catalytic cracking technology, more wax oil, diesel oil and other heavy fuels are required to be injected for burning, so that additional heat is provided for catalytic cracking, and the problems of fuel waste and fossil fuel carbon emission are caused. Because of the large amount of fuel burn-out reaction, a high-power main fan is required to provide air for the burn-out reaction of the regenerator, so that the regenerator is large in design size. The high-power main fan and the large-size regenerator cause the increase of equipment investment, and a large amount of subsequently generated flue gas also needs to be matched with a flue gas desulfurization and denitrification system with large treatment capacity, so that the requirements of low carbon and environmental protection are not met, the equipment investment is increased, and the production cost is increased.
Disclosure of Invention
The invention aims to solve the technical problems of providing an electric catalytic cracking device which has the advantages of simple structure, energy conservation and less equipment investment. Meanwhile, the method for electrically catalyzing and cracking the petroleum hydrocarbon is low in carbon and environment-friendly, and the carbon dioxide emission is effectively reduced.
The invention relates to an electric catalytic cracking device, which comprises a regenerator and a settler, wherein the regenerator is provided with a regenerated catalyst outlet and a spent catalyst inlet, the bottom of the regenerator is provided with a main air pipe, the main air pipe is connected with a main fan, and a first electric heater is arranged in the main air pipe; the bottom of the settler is connected with a spent catalyst inlet, a second electric heater is arranged in the settler, a steam spray pipe is wrapped outside the second electric heater, the steam spray pipe is communicated with a steam air supply pipe, a plurality of steam spray holes are arranged on the steam spray pipe, steam flows in a space formed by the second electric heater and the inner wall of the steam spray pipe, and is sprayed out by the steam spray holes; the regenerated catalyst outlet is connected with a lifting pipe, the lifting pipe is provided with a raw material inlet, the lifting pipe extends into the settler from the bottom of the settler, the lifting pipe is provided with an outlet, and the outlet is arranged above the second electric heater.
The first electric heater comprises a plurality of groups of electric heating tube bundles connected in series.
The top of the regenerator is provided with a flue gas outlet which is connected with a desulfurization and denitrification system.
The second electric heater is a fin-tube electric heater and comprises a plurality of groups of electric heating tube bundles, and steam spray pipes are wrapped outside each group of electric heating tube bundles.
The top of the settler is provided with a product gas outlet which is connected with a product gas separation unit.
The pipeline can be provided with a valve according to the control requirement, and the on-off of materials in the corresponding pipeline and the flow of the materials are conveniently controlled through the opening and closing of the valve.
The invention also provides an electrocatalytic pyrolysis method for petroleum hydrocarbon by using the electrocatalytic pyrolysis device, which comprises the following steps of:
(1) Petroleum hydrocarbon with the feeding temperature of 120-220 ℃ enters a lifting pipe through a raw material inlet, contacts with a regenerated catalyst with the temperature of 750-800 ℃ to carry out cracking reaction for 1-3 s, so as to obtain a gas-phase product and a catalyst to be regenerated, wherein the mass ratio of the regenerated catalyst to the petroleum hydrocarbon is 8-10;
(2) The gas-phase product and the spent catalyst are lifted to the outlet of the lifting pipe and then are separated, the spent catalyst falls down in the settler at the moment, and the temperature of the spent catalyst is 550-600 ℃;
(3) When the spent catalyst falls into the steam spray pipe, heat exchange is carried out between the spent catalyst and high-temperature steam sprayed out of the steam spray hole, the temperature is raised to 600-650 ℃, the spent catalyst is sent out from the settler and enters the regenerator through a spent catalyst inlet, and the high-temperature steam is obtained by heat exchange between the steam provided by the steam air supply pipe and the second electric heater after entering the steam spray pipe;
(4) The main fan blows air through a main air pipe, the air is heated to 400 ℃ through a first electric heater and then enters the regenerator to contact with a catalyst to be regenerated in the regenerator to start reaction, meanwhile, the regenerated catalyst is heated by heat release and finally reaches the scorching temperature to realize catalyst regeneration, and then the catalyst is sent out to a riser through a regenerated catalyst outlet to catalyze the cracking reaction of petroleum hydrocarbon, wherein the scorching temperature is 750-800 ℃, and the scorching time is 1-3 min.
The petroleum hydrocarbon is one of light paraffin oil, naphtha, carbon five and paraffin-based common slag.
The coke burning temperature of the regenerator is generally 660-730 ℃, and the regenerator is a place for coke burning and regeneration of the catalyst, and provides heat for the catalyst through coke burning; the reaction temperature of the outlet of the lifting pipe is 550-600 ℃, so that the temperature of the catalyst to be regenerated sent out from the outlet is 550-600 ℃, the lifting pipe is a place where the high-temperature regenerated catalyst contacts with raw oil for reaction, and petroleum hydrocarbon reacts with the regenerated catalyst to generate products such as ethylene, propylene, liquefied gas, gasoline, diesel oil and the like; the settler is a place for separating gas phase products and catalysts after petroleum hydrocarbon reaction, and is an intermediate storage place for circulating the catalysts in the regenerator and the riser, and the temperature of the catalyst to be regenerated entering the settler is 550-600 ℃. The catalyst is continuously and circularly reacted and regenerated among the regenerator, the riser and the settler to provide the heat required by the reaction.
The regenerator is burnt and needs the main fan to blow a large amount of air into the main fan through a main air pipe as main air, the main air temperature of an outlet of the main fan is 200 ℃, the main air temperature is increased to 400 ℃ by adding a first electric heater, the first electric heater comprises 3-5 groups of electric heating tube bundles connected in series, the series electric heating tube bundles sequentially heat the main air, and the electric heater in the main air pipe adopts a common industrial electric heating tube bundle.
And a second electric heater is arranged in the settler according to the need, the second electric heater comprises 4-8 groups of electric heating tube bundles, the spent catalyst at 550-600 ℃ separated from the reaction product falls from the outlet of the lifting tube, and when the spent catalyst passes through the second electric heater, the spent catalyst is heated to 600-650 ℃ after heat exchange with the second electric heater. The spent catalyst at 600-650 ℃ enters a regenerator and is heated to 400 ℃ with main air to carry out a small amount of burning heat release, so that the temperature of 750-800 ℃ can be reached, and the reaction temperature of the riser can be flexibly controlled to reach the catalytic cracking reaction temperature above 600 ℃.
Compared with the prior art, the invention has the beneficial effects that:
1. the electric power is used for replacing fossil fuels such as wax oil, gas, coke and the like as energy sources for chemical reaction, so that the energy sources are saved, and simultaneously, the carbon dioxide emission caused by the fossil fuels is reduced, thereby being beneficial to low carbon and environmental protection;
2. the device has a simple structure, can be realized by reforming the existing fuel burning device, and does not need a high-power main fan and a large-size regenerator because fossil fuel combustion is not adopted to provide burning heat, thereby reducing equipment investment and meeting the requirement of raw material lightening.
Drawings
FIG. 1 is a schematic diagram of the structure of the present invention;
in the figure: 1. a regenerator; 2. a settler; 3. a regenerated catalyst outlet; 4. a spent catalyst inlet; 5. a main air pipe; 6. a first electric heater; 7. a second electric heater; 8. a riser; 9. a raw material inlet; 10. a flue gas outlet; 11. a product gas outlet; 12. a steam nozzle; 13. a steam supply pipe.
Detailed Description
The present invention will now be described more fully hereinafter with reference to the accompanying drawings.
It should be noted that relational terms such as first and second are used solely to distinguish one entity or action from another entity or action to facilitate expression and not to represent a sequential relationship.
As shown in fig. 1, the electrocatalytic pyrolysis device comprises a regenerator 1 and a settler 2, wherein the regenerator 1 is provided with a regenerated catalyst outlet 3 and a spent catalyst inlet 4, the bottom of the regenerator 1 is provided with a main air pipe 5, the main air pipe 5 is connected with a main fan, and a first electric heater 6 is arranged in the main air pipe 5; the bottom of the settler 2 is connected with a spent catalyst inlet 4, a second electric heater 7 is arranged in the settler 2, a steam spray pipe 12 is wrapped outside the second electric heater 7, the steam spray pipe 12 is communicated with a steam supply pipe 13, a plurality of steam spray holes are arranged on the steam spray pipe 12, steam flows in a space formed by the second electric heater 7 and the inner wall of the steam spray pipe 12, and is sprayed out by the steam spray holes; the regenerated catalyst outlet 3 is connected with a riser pipe 8, the riser pipe 8 is provided with a raw material inlet 9, the riser pipe 8 extends into the settler 2 from the bottom of the settler 2, the riser pipe 8 is provided with an outlet, and the outlet is arranged above the second electric heater 7.
The first electric heater 6 comprises 3 groups of electric heating tube bundles connected in series.
The top of the regenerator 1 is provided with a flue gas outlet 10, and the flue gas outlet 10 is connected with a desulfurization and denitrification system.
The second electric heater 7 is a fin-tube electric heater and comprises 6 groups of electric heating tube bundles, and steam spray pipes 12 are wrapped outside each group of electric heating tube bundles.
The top of the settler 2 is provided with a product gas outlet 11, and the product gas outlet 11 is connected with a product gas separation unit.
The invention relates to an electrocatalytic cracking method of petroleum hydrocarbon, which comprises the following steps:
(1) Petroleum hydrocarbon enters a riser through a raw material inlet and contacts with a regenerated catalyst at 750-800 ℃ to carry out cracking reaction for 1-3 s to obtain a gas-phase product and a spent catalyst, wherein the mass ratio of the regenerated catalyst to the petroleum hydrocarbon is 8-10;
(2) The gas-phase product and the spent catalyst are lifted to the outlet of the lifting pipe and then are separated, the spent catalyst falls down in the settler at the moment, and the temperature of the spent catalyst is 550-600 ℃;
(3) When the spent catalyst falls into the steam spray pipe, heat exchange is carried out between the spent catalyst and high-temperature steam sprayed out of the steam spray hole, the temperature is raised to 600-650 ℃, the spent catalyst is sent out from the settler and enters the regenerator through a spent catalyst inlet, and the high-temperature steam is obtained by heat exchange between the steam provided by the steam air supply pipe and the second electric heater after entering the steam spray pipe;
(4) The main fan blows air through a main air pipe, the air is heated to 400 ℃ through a first electric heater and then enters the regenerator to contact with a catalyst to be regenerated in the regenerator to start reaction, meanwhile, the regenerated catalyst is heated by heat release and finally reaches the scorching temperature to realize catalyst regeneration, and then the catalyst is sent out to a riser through a regenerated catalyst outlet to catalyze the cracking reaction of petroleum hydrocarbon, wherein the scorching temperature is 750-800 ℃, and the scorching time is 1-3 min.
The process parameters of examples 1-2 are shown in Table 1, and the distribution of the obtained products is shown in tables 2-3.
Table 1 examples 1-2 process parameters
Table 2 example 1 product distribution
TABLE 3 example 2 product distribution
As can be seen from the data in tables 2 and 3, the invention uses electricity to replace fossil fuel combustion to provide cracking and burning heat, can realize catalytic cracking of petroleum hydrocarbon, and has small burning ratio and high product rate.
Claims (10)
1. The electric catalytic cracking device is characterized by comprising a regenerator and a settler, wherein the regenerator is provided with a regenerated catalyst outlet and a spent catalyst inlet, the bottom of the regenerator is provided with a main air pipe, the main air pipe is connected with a main fan, and a first electric heater is arranged in the main air pipe; the bottom of the settler is connected with a spent catalyst inlet, a second electric heater is arranged in the settler, a steam spray pipe is wrapped outside the second electric heater, the steam spray pipe is communicated with a steam air supply pipe, a plurality of steam spray holes are arranged on the steam spray pipe, steam flows in a space formed by the second electric heater and the inner wall of the steam spray pipe, and is sprayed out by the steam spray holes; the regenerated catalyst outlet is connected with a lifting pipe, the lifting pipe is provided with a raw material inlet, the lifting pipe extends into the settler from the bottom of the settler, the lifting pipe is provided with an outlet, and the outlet is arranged above the second electric heater.
2. The electrocatalytic pyrolysis apparatus of claim 1, wherein the first electric heater comprises a plurality of series-connected groups of electric heating tube bundles.
3. The electrocatalytic pyrolysis device according to claim 1, wherein a flue gas outlet is formed in the top of the regenerator and is connected with a desulfurization and denitrification system.
4. The electrocatalytic pyrolysis device of claim 1, wherein the second electric heater is a fin-tube electric heater, the second electric heater comprising a plurality of groups of electric heating tube bundles, each group of electric heating tube bundles having a steam nozzle wrapped around the exterior thereof.
5. The electrocatalytic pyrolysis device of claim 1, wherein a product gas outlet is provided at the top of the settler, the product gas outlet being connected to a product gas separation unit.
6. A method for electrocatalytic cracking of petroleum hydrocarbons using the apparatus of any one of claims 1-5, comprising the steps of:
(1) Petroleum hydrocarbon with the feeding temperature of 120-220 ℃ enters a lifting pipe through a raw material inlet, contacts with a regenerated catalyst to carry out a cracking reaction, and a gas-phase product and a spent catalyst are obtained;
(2) The gas phase product and the spent catalyst are lifted to a lifting pipe outlet for delivery and then separated, and the spent catalyst falls in a settler;
(3) When the spent catalyst falls into the steam spray pipe, heat exchange with high-temperature steam sprayed from the steam spray hole is carried out, the temperature is raised, the spent catalyst is sent out from the settler and enters the regenerator through the inlet of the spent catalyst, wherein the high-temperature steam is obtained by heat exchange with a second electric heater after the steam provided by the steam supply pipe enters the steam spray pipe;
(4) The main fan blows air through the main air pipe, the air is heated to 400 ℃ through the first electric heater and then enters the regenerator to contact with the catalyst to be regenerated in the regenerator to start reaction, meanwhile, the regenerated catalyst is heated by heat release, the burning temperature is finally reached, catalyst regeneration is realized, and then the catalyst is sent out to the riser through the regenerated catalyst outlet to catalyze the cracking reaction of petroleum hydrocarbon.
7. The method for electrocatalytic pyrolysis of petroleum hydrocarbon according to claim 6, wherein the temperature of the regenerated catalyst in the step (1) is 750-800 ℃, the mass ratio of the regenerated catalyst to the petroleum hydrocarbon is 8-10, and the reaction time is 1-3 s.
8. The method for electrocatalytic pyrolysis of petroleum hydrocarbon according to claim 6, wherein the temperature of the spent catalyst in the step (2) is 550-600 ℃.
9. The method for electrocatalytic pyrolysis of petroleum hydrocarbon according to claim 6, wherein the temperature of the spent catalyst in step (3) is raised to 600-650 ℃.
10. The electrocatalytic pyrolysis method of petroleum hydrocarbon according to claim 6, wherein the scorching temperature in the step (4) is 750-800 ℃ and the scorching time is 1-3 min.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202310313239.3A CN116459743A (en) | 2023-03-28 | 2023-03-28 | Electrocatalytic cracking device and electrocatalytic cracking method for petroleum hydrocarbon |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202310313239.3A CN116459743A (en) | 2023-03-28 | 2023-03-28 | Electrocatalytic cracking device and electrocatalytic cracking method for petroleum hydrocarbon |
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| Publication Number | Publication Date |
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| CN116459743A true CN116459743A (en) | 2023-07-21 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202310313239.3A Pending CN116459743A (en) | 2023-03-28 | 2023-03-28 | Electrocatalytic cracking device and electrocatalytic cracking method for petroleum hydrocarbon |
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| Country | Link |
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| CN (1) | CN116459743A (en) |
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- 2023-03-28 CN CN202310313239.3A patent/CN116459743A/en active Pending
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