CN114516795A - Method for producing methyl acrylate by using methanol and methyl acetate as raw materials - Google Patents
Method for producing methyl acrylate by using methanol and methyl acetate as raw materials Download PDFInfo
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- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 title claims abstract description 87
- BAPJBEWLBFYGME-UHFFFAOYSA-N Methyl acrylate Chemical compound COC(=O)C=C BAPJBEWLBFYGME-UHFFFAOYSA-N 0.000 title claims abstract description 50
- KXKVLQRXCPHEJC-UHFFFAOYSA-N acetic acid trimethyl ester Natural products COC(C)=O KXKVLQRXCPHEJC-UHFFFAOYSA-N 0.000 title claims abstract description 40
- XBDQKXXYIPTUBI-UHFFFAOYSA-M Propionate Chemical compound CCC([O-])=O XBDQKXXYIPTUBI-UHFFFAOYSA-M 0.000 title claims abstract description 38
- 239000002994 raw material Substances 0.000 title claims abstract description 13
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 10
- 238000006243 chemical reaction Methods 0.000 claims abstract description 20
- 239000003054 catalyst Substances 0.000 claims description 104
- 230000008929 regeneration Effects 0.000 claims description 40
- 238000011069 regeneration method Methods 0.000 claims description 40
- 238000000034 method Methods 0.000 claims description 33
- 239000007789 gas Substances 0.000 claims description 22
- 239000000463 material Substances 0.000 claims description 14
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 12
- 239000007795 chemical reaction product Substances 0.000 claims description 11
- 238000010438 heat treatment Methods 0.000 claims description 11
- 229910052757 nitrogen Inorganic materials 0.000 claims description 6
- 239000011148 porous material Substances 0.000 claims description 6
- 239000006200 vaporizer Substances 0.000 claims description 4
- 230000005484 gravity Effects 0.000 claims description 3
- 230000000630 rising effect Effects 0.000 claims description 3
- 125000004122 cyclic group Chemical group 0.000 claims description 2
- 239000000779 smoke Substances 0.000 claims description 2
- WSFSSNUMVMOOMR-UHFFFAOYSA-N Formaldehyde Chemical compound O=C WSFSSNUMVMOOMR-UHFFFAOYSA-N 0.000 description 12
- 239000000203 mixture Substances 0.000 description 3
- VQTUBCCKSQIDNK-UHFFFAOYSA-N Isobutene Chemical compound CC(C)=C VQTUBCCKSQIDNK-UHFFFAOYSA-N 0.000 description 2
- 208000012839 conversion disease Diseases 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000010926 purge Methods 0.000 description 2
- 238000011144 upstream manufacturing Methods 0.000 description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 2
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 1
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 description 1
- 239000005977 Ethylene Substances 0.000 description 1
- VVQNEPGJFQJSBK-UHFFFAOYSA-N Methyl methacrylate Chemical compound COC(=O)C(C)=C VVQNEPGJFQJSBK-UHFFFAOYSA-N 0.000 description 1
- RJUFJBKOKNCXHH-UHFFFAOYSA-N Methyl propionate Chemical compound CCC(=O)OC RJUFJBKOKNCXHH-UHFFFAOYSA-N 0.000 description 1
- 208000005374 Poisoning Diseases 0.000 description 1
- 238000007664 blowing Methods 0.000 description 1
- 238000004364 calculation method Methods 0.000 description 1
- 238000004891 communication Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 239000003546 flue gas Substances 0.000 description 1
- 229940017219 methyl propionate Drugs 0.000 description 1
- 231100000572 poisoning Toxicity 0.000 description 1
- 230000000607 poisoning effect Effects 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 239000002351 wastewater Substances 0.000 description 1
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C67/00—Preparation of carboxylic acid esters
- C07C67/30—Preparation of carboxylic acid esters by modifying the acid moiety of the ester, such modification not being an introduction of an ester group
- C07C67/333—Preparation of carboxylic acid esters by modifying the acid moiety of the ester, such modification not being an introduction of an ester group by isomerisation; by change of size of the carbon skeleton
- C07C67/343—Preparation of carboxylic acid esters by modifying the acid moiety of the ester, such modification not being an introduction of an ester group by isomerisation; by change of size of the carbon skeleton by increase in the number of carbon atoms
-
- 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
- B01J38/00—Regeneration or reactivation of catalysts, in general
- B01J38/02—Heat treatment
-
- 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
- B01J38/00—Regeneration or reactivation of catalysts, in general
- B01J38/04—Gas or vapour treating; Treating by using liquids vaporisable upon contacting spent catalyst
- B01J38/12—Treating with free oxygen-containing gas
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/584—Recycling of catalysts
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- Engineering & Computer Science (AREA)
- Materials Engineering (AREA)
- Chemical Kinetics & Catalysis (AREA)
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- Thermal Sciences (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention discloses a method for producing methyl acrylate by using methanol and methyl acetate as raw materials. The invention adopts methanol as raw material, and directly reacts with methyl acetate to produce methyl acrylate, the conversion rate of the methyl acetate reaches more than 30%, and the selectivity of the methyl acrylate reaches more than 95%.
Description
Technical Field
The invention relates to the field of chemical industry, in particular to a method for producing methyl acrylate by using methanol and methyl acetate as raw materials.
Background
Methyl acrylate is the main material for producing methyl propionate and methyl methacrylate, and the methyl acrylate producing technology has been that isobutene process and ethylene process are adopted mostly, and formaldehyde and methyl acetate are reacted to produce methyl acrylate.
Disclosure of Invention
The invention aims to provide a method for producing methyl acrylate by using methanol and methyl acetate as raw materials. The invention adopts methanol as raw material, and directly reacts with methyl acetate to produce methyl acrylate, the conversion rate of the methyl acetate reaches more than 30%, and the selectivity of the methyl acrylate reaches more than 95%.
In order to achieve the purpose, the invention adopts the following technical scheme:
A method for producing methyl acrylate by using methanol and methyl acetate as raw materials comprises the following steps:
after being vaporized into a gas phase by a vaporizer, the mixed material of the methanol and the methyl acetate sequentially enters a preheater and a heating furnace to be heated to 300-310 ℃, and then enters a reaction unit to react;
the reaction unit comprises a stripping tube reactor, a first settling chamber, a first cyclone separator and a second cyclone separator; the upper part of the gas-lift tube reactor is sleeved in the first settling chamber, the top of the gas-lift tube reactor is connected with a first cyclone separator, a second cyclone separator is arranged at an outlet at the top of the first settling chamber, and a gas outlet of the second cyclone separator is connected with an outlet at the top of the first settling chamber; the bottom of the first settling chamber is provided with a catalyst outlet which is connected with an inlet of a catalyst regeneration unit, and an outlet of the catalyst regeneration unit is connected with a catalyst inlet positioned at the lower part of the gas stripping reactor;
the mixed material heated to 300-310 ℃ enters from the bottom of the gas-lift tube reactor, the catalyst in the gas-lift tube reactor is pneumatically conveyed to the top of the gas-lift tube reactor, the catalyst catalyzes methyl acetate and methanol in the pneumatic conveying process, and a reaction product is obtained after reaction;
The reaction product enters a first cyclone separator from the top of the stripping tube reactor, is collected at the top of a first settling chamber after being output from the top of the first cyclone separator, and is separated by a second cyclone separator to enter and be output; the output reaction product is preheated by the preheater to the mixed material of the methanol and the methyl acetate which is vaporized into gas phase, and the heat is recovered;
the catalyst separated by the first cyclone separator and the second cyclone separator is settled to the bottom of the first settling chamber and enters the catalyst regeneration unit through the catalyst outlet for catalyst regeneration, and the regenerated catalyst enters the gas stripping tube reactor through the catalyst inlet for cyclic utilization.
According to the method of the invention, the molar ratio of the methyl acetate to the methanol is preferably 1 (9-10).
According to the method, preferably, the upper part of the stripper reactor, which is positioned in the first settling chamber, is provided with a pore canal on the side wall, a part of the catalyst and the reaction products in the stripper reactor enter the bottom of the first settling chamber through the pore canal, and gas enters the first cyclone separator from the top of the stripper reactor; the catalyst carried out from the pore canal sinks to the bottom of the first settling chamber.
According to the method of the invention, preferably, the first settling chamber is provided with a turning plate at the bottom of the inner cavity, and the catalyst outlet is positioned below the turning plate; the catalyst settled to the bottom of the first settling chamber passes through the turning plate, enters the bottommost part of the first settling chamber, and enters the catalyst regeneration unit through the catalyst outlet to be regenerated.
According to the method of the present invention, preferably, the catalyst regeneration unit is regenerated using hot air.
According to the process of the present invention, preferably, the catalyst regeneration unit comprises a riser regenerator, a second settling chamber and a side sub-tank;
the upper part of the riser regenerator is sleeved in the second settling chamber, the top of the riser regenerator is open, and the bottom of the riser regenerator is provided with a regenerated gas inlet;
the bottom of the side auxiliary tank is connected with a catalyst inlet of the gas stripping reactor, and the top of the side auxiliary tank is connected with the second settling chamber;
the catalyst outlet at the bottom of the first settling chamber is connected with the bottom of the riser regenerator;
preheating air by an air preheater, and then heating the air in the heating furnace to a regeneration temperature; the hot air drives the catalyst from the first settling chamber to enter the riser regenerator, the catalyst spirally rises, the regeneration of the catalyst by the hot air is completed in the period, the catalyst is separated from the hot air through the gravity action in the rising process, the catalyst is settled to the bottom of the second settling chamber and flows into the side-by-side tank, and then the catalyst is controlled to enter the riser reactor;
And the hot air at the top of the second settling chamber is output from the top, and is sent out in a smoke mode after the heat is recovered by the air preheater.
According to the method, the regeneration temperature of the catalyst is preferably 200-300 ℃.
According to the method of the present invention, preferably, the catalyst from the first settling chamber enters the riser regenerator after being subjected to nitrogen reverse purging, and the reaction materials are controlled not to enter the catalyst regeneration unit.
According to the method, preferably, during the process that the regenerated catalyst enters the stripper reactor from the side auxiliary tank, the nitrogen is blown reversely, so that entrained gas is blown to the top of the side auxiliary tank and enters the second settling chamber, and air is prevented from entering the stripper reactor along with the catalyst.
According to the method of the present invention, preferably, the catalyst regeneration unit further comprises a third cyclone; the third cyclone separator is positioned outside the second settling chamber, and an inlet, a top outlet and a bottom outlet of the third cyclone separator are communicated with the second settling chamber;
during the process that the hot air rises to the top in the second settling chamber, the entrained catalyst is separated by the third cyclone separator and then returns to the second settling chamber.
The invention provides a method for producing methyl acrylate by taking methanol and methyl acetate as raw materials, wherein the prior similar technology adopts formaldehyde as the raw material, so that the formaldehyde wastewater is difficult to treat, and meanwhile, the formaldehyde has poisoning risk to production operators.
Drawings
FIG. 1 is a schematic diagram of a process for producing methyl acrylate from methanol and methyl acetate according to a preferred embodiment of the present invention.
Description of reference numerals:
1. a vaporizer;
2. a preheater;
3. heating furnace;
4. a gas-lift tube reactor;
5. a first settling chamber;
6. a first cyclone separator;
7. a second cyclone separator;
8. a top outlet of the first settling chamber;
9. turning plate
10. An air preheater;
11. a riser regenerator;
12. a second settling chamber;
13. a side auxiliary tank;
14. a third cyclone separator.
Detailed Description
In order to more clearly illustrate the invention, the invention is further described below in connection with preferred embodiments. It is to be understood by persons skilled in the art that the following detailed description is illustrative and not restrictive, and is not to be taken as limiting the scope of the invention.
The invention provides a preferable scheme, as shown in figure 1, a method for producing methyl acrylate by using methanol and methyl acetate as raw materials comprises the following processes:
methyl acetate and methanol are mixed according to the molar ratio of 1 (9-10), the mixed material is vaporized into gas phase by a vaporizer 1, and then enters a preheater 2 and a heating furnace 3 in sequence to be heated to 310 ℃ of 300-.
The reaction unit comprises a stripper tube reactor 4, a first settling chamber 5, a first cyclone separator 6 and a second cyclone separator 7; the upper part of the gas-lift tube reactor 4 is sleeved in the first settling chamber 5, the top of the gas-lift tube reactor 4 is connected with a first cyclone separator 6, a second cyclone separator 7 is arranged at the top outlet of the interior of the first settling chamber 5, and the gas outlet of the second cyclone separator 7 is connected with the top outlet 8 of the first settling chamber 5; the bottom of the first settling chamber 5 is provided with a catalyst outlet which is connected with an inlet of a catalyst regeneration unit, and an outlet of the catalyst regeneration unit is connected with a catalyst inlet positioned at the lower part of the stripper reactor 4.
The mixed material heated to 300-310 ℃ enters from the bottom of the stripping tube reactor 4, the catalyst in the stripping tube reactor 4 is pneumatically conveyed to the top of the stripping tube reactor 4, the catalyst catalyzes methyl acetate and methanol in the pneumatic conveying process, and methyl acetate is completely reacted to obtain methyl acrylate and excessive methanol.
The reaction product enters a first cyclone separator 6 from the top of the stripping tube reactor 4, is collected at the top of a first settling chamber 5 after being output from the top of the first cyclone separator 6, and is separated by a second cyclone separator 7 to enter and be output; the output reaction product is preheated by the preheater 2 to recover heat from the mixture of methanol and methyl acetate vaporized to a gas phase, and then sent to a subsequent separation unit.
The catalyst separated by the first cyclone separator 6 and the second cyclone separator 7 is settled to the bottom of the first settling chamber 5, and enters the catalyst regeneration unit through the catalyst outlet for catalyst regeneration, and the regenerated catalyst enters the stripper reactor 4 through the catalyst inlet for recycling.
Further, the upper part of the stripper reactor 4 located in the first settling chamber 5 is provided with a pore channel on the side wall, a part of the catalyst and the reaction product in the stripper reactor 4 enter the bottom of the first settling chamber 5 through the pore channel, and the gas enters the first cyclone separator 6 from the top of the stripper reactor 4; the catalyst entrained from the portholes settles to the bottom of the first settling chamber 5.
Further, a turning plate 9 is arranged at the bottom of the inner cavity of the first settling chamber 5, and the catalyst outlet is positioned below the turning plate 9; the catalyst settled to the bottom of the first settling chamber 5 passes through the turning plate 9 and then enters the bottommost part of the first settling chamber 5, and enters the catalyst regeneration unit through the catalyst outlet for catalyst regeneration.
The catalyst regeneration unit adopts hot air for regeneration. The catalyst regeneration unit comprises a riser regenerator 11, a second settling chamber 12, a side auxiliary tank 13 and a third cyclone separator 14; the upper part of the riser regenerator 11 is sleeved in the second settling chamber 12, the top of the riser regenerator is open, and the bottom of the riser regenerator is provided with a regeneration gas inlet; the bottom of the side auxiliary tank 13 is connected with the catalyst inlet of the stripper reactor 11, and the top of the side auxiliary tank is connected with the second settling chamber 12; the catalyst regeneration unit further comprises the third cyclone 14 located outside the second settling chamber 12 and having its inlet, top outlet and bottom outlet all in communication with the second settling chamber 12. The catalyst outlet at the bottom of the first settling chamber 5 is connected with the bottom of the riser regenerator 11.
Air enters the heating furnace 3 after being preheated by the air preheater 10 and is heated to the regeneration temperature of 200-300 ℃, the higher the temperature is, the higher the regeneration speed is, and the smaller the regenerator size is. The hot air drives the catalyst from the first settling chamber 5 to enter the riser regenerator 11, the catalyst spirally rises, the catalyst is regenerated by the hot air in the period, the catalyst is separated from the hot air by the action of gravity in the rising process, the catalyst settles to the bottom of the second settling chamber 12 and flows into the side-by-side tank 13, and then the catalyst is controlled to enter the stripper reactor 4. The hot air in the top of the second settling chamber 12 is output from the top and sent out in the form of flue gas after heat recovery by the air preheater 10. During the upward movement of the heated air to the top in the second settling chamber 12, entrained catalyst is separated by the third cyclone 14 and returned to the second settling chamber 12.
Wherein, the pipeline of the first settling chamber 4 connected with the riser regenerator 11 controls the flow through a slide valve, and controls the reaction materials not to enter the catalyst regeneration unit through the reverse purging of nitrogen at the upstream of the slide valve. The line connecting the side sub tank 13 to the stripper reactor 4 is also flow-controlled by a slide valve, upstream of which is blown in reverse by nitrogen, blowing entrained gas to the top of the side sub tank 13 and into the second settling chamber 12, preventing air from entering the stripper reactor 4 with the catalyst.
Application example
The application example adopts the flow of the method in figure 1, and uses methanol and methyl acetate as raw materials to produce methyl acrylate.
The purity of the methyl acetate is 95 wt%, and the feeding flow is 1 t/h; the purity of the methanol is 99.9 wt%, the feeding flow is 3.2t/h, the two materials are mixed and pressurized to 0.3MPaG by a pump, heated to 103 ℃ by a gasifier and then enter a preheater, heated to 220 ℃ and then enter a heating furnace, and heated to 270 ℃ in the heating furnace and then enter a reaction unit.
The reaction discharge is methyl acrylate, methanol, methyl acetate, water and others. The specific composition is shown in table 1 below:
TABLE 1 reaction discharge composition
| Name of material | Outlet flow (t/h) | Mass ratio (%) |
| Acrylic acid methyl ester | 0.342 | 8.14 |
| Methanol | 3.04 | 72.48 |
| Acetic acid methyl ester | 0.64 | 15.24 |
| Water (W) | 0.09 | 2.08 |
| Others | 0.09 | 2.05 |
The content of methyl acetate in the feed is 1t/h, the purity is 95 percent, wherein the content of pure methyl acetate is 0.95t/h, the content of methyl acetate in the discharge is 0.64t/h, the reaction conversion is 0.31t/h, and the conversion rate is 0.31/0.95-32.63 percent.
The content of methyl acetate in the feed is 1t/h, the purity is 95 percent, wherein the content of pure methyl acetate is 0.95t/h, the content of methyl acetate in the discharge is 0.64t/h, and the reaction conversion is 0.31 t/h.
The mass balance for the reaction of methanol with methyl acetate to produce methyl acrylate is as follows:
according to the calculation, 0.31t/h of pure methyl acetate can be converted into 0.36t/h of methyl acrylate through the reaction, but the content of the methyl acrylate in the reaction discharge material is 0.342t/h, and the selectivity of the reaction on the methyl acrylate is 0.342/0.36-95%.
It should be understood that the above-mentioned embodiments of the present invention are only examples for clearly illustrating the present invention, and are not intended to limit the embodiments of the present invention, and it will be obvious to those skilled in the art that other variations or modifications may be made on the basis of the above description, and all embodiments may not be exhaustive, and all obvious variations or modifications may be included within the scope of the present invention.
Claims (10)
1. A method for producing methyl acrylate by using methanol and methyl acetate as raw materials is characterized by comprising the following steps:
after being vaporized into a gas phase by a vaporizer, the mixed material of the methanol and the methyl acetate sequentially enters a preheater and a heating furnace to be heated to 300-310 ℃, and then enters a reaction unit to react;
the reaction unit comprises a stripping tube reactor, a first settling chamber, a first cyclone separator and a second cyclone separator; the upper part of the gas-stripping tube reactor is sleeved in the first settling chamber, the top of the gas-stripping tube reactor is connected with a first cyclone separator, a second cyclone separator is arranged at an outlet at the top of the first settling chamber, and a gas outlet of the second cyclone separator is connected with an outlet at the top of the first settling chamber; the bottom of the first settling chamber is provided with a catalyst outlet which is connected with an inlet of a catalyst regeneration unit, and an outlet of the catalyst regeneration unit is connected with a catalyst inlet positioned at the lower part of the stripping tube reactor;
the mixed material heated to 300-310 ℃ enters from the bottom of the gas-lift tube reactor, the catalyst in the gas-lift tube reactor is pneumatically conveyed to the top of the gas-lift tube reactor, the catalyst catalyzes methyl acetate and methanol in the pneumatic conveying process, and a reaction product is obtained after reaction;
The reaction product enters a first cyclone separator from the top of the stripping tube reactor, is collected at the top of a first settling chamber after being output from the top of the first cyclone separator, and is separated by a second cyclone separator to enter and be output; the output reaction product is preheated by the preheater to the mixed material of the methanol and the methyl acetate which is vaporized into gas phase, and the heat is recovered;
the catalyst separated by the first cyclone separator and the second cyclone separator is settled to the bottom of the first settling chamber and enters the catalyst regeneration unit through the catalyst outlet for catalyst regeneration, and the regenerated catalyst enters the gas stripping tube reactor through the catalyst inlet for cyclic utilization.
2. The method according to claim 1, wherein the molar ratio of methyl acetate to methanol is 1 (9-10).
3. The method according to claim 1, characterized in that the upper part of the stripper reactor, which is positioned in the first settling chamber, is provided with holes on the side wall, a part of the catalyst and the reaction products in the stripper reactor enter the bottom of the first settling chamber through the holes, and gas enters the first cyclone separator from the top of the stripper reactor; the catalyst carried out from the pore canal sinks to the bottom of the first settling chamber.
4. The method according to claim 2, wherein the first settling chamber is provided with a flap at the bottom of the inner chamber, and the catalyst outlet is located below the flap; the catalyst settled to the bottom of the first settling chamber passes through the turning plate, enters the bottommost part of the first settling chamber, and enters the catalyst regeneration unit through the catalyst outlet to perform catalyst regeneration.
5. The method of claim 1, wherein the catalyst regeneration unit employs hot air regeneration.
6. The process of claim 5, wherein the catalyst regeneration unit comprises a riser regenerator, a second settling chamber, and a side sub-tank;
the upper part of the riser regenerator is sleeved in the second settling chamber, the top of the riser regenerator is open, and the bottom of the riser regenerator is provided with a regenerated gas inlet;
the bottom of the side auxiliary tank is connected with a catalyst inlet of the stripping tube reactor, and the top of the side auxiliary tank is connected with the second settling chamber;
the catalyst outlet at the bottom of the first settling chamber is connected with the bottom of the riser regenerator;
preheating air by an air preheater, and then heating the air in the heating furnace to a regeneration temperature; the hot air drives the catalyst from the first settling chamber to enter the riser regenerator, the catalyst spirally rises, the regeneration of the catalyst by the hot air is completed in the period, the catalyst is separated from the hot air through the gravity action in the rising process, the catalyst is settled to the bottom of the second settling chamber and flows into the side-by-side tank, and then the catalyst is controlled to enter the riser reactor;
And the hot air at the top of the second settling chamber is output from the top, and is sent out in a smoke mode after the heat is recovered by the air preheater.
7. The method according to claim 6, wherein the regeneration temperature of the catalyst is 200 to 300 ℃.
8. The process of claim 6 wherein the catalyst from said first settling chamber is purged countercurrently with nitrogen and passed to said riser regenerator, with the reaction mass being controlled not to pass to said catalyst regeneration unit.
9. The method of claim 6, wherein during the process of entering the stripper reactor from the side sub-tank, the regenerated catalyst is blown by nitrogen in a reverse direction to blow entrained gas to the top of the side sub-tank and into the second settling chamber, thereby preventing air from entering the stripper reactor with the catalyst.
10. The method of claim 6, wherein the catalyst regeneration unit further comprises a third cyclone; the third cyclone separator is positioned outside the second settling chamber, and an inlet, a top outlet and a bottom outlet of the third cyclone separator are communicated with the second settling chamber;
during the process that the hot air rises to the top in the second settling chamber, the entrained catalyst is separated by the third cyclone separator and then returns to the second settling chamber.
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