CN115055212A - Regeneration method for preparing olefin from methanol with zero emission of carbon dioxide - Google Patents
Regeneration method for preparing olefin from methanol with zero emission of carbon dioxide Download PDFInfo
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- CN115055212A CN115055212A CN202210654904.0A CN202210654904A CN115055212A CN 115055212 A CN115055212 A CN 115055212A CN 202210654904 A CN202210654904 A CN 202210654904A CN 115055212 A CN115055212 A CN 115055212A
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- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 title claims abstract description 68
- 229910002092 carbon dioxide Inorganic materials 0.000 title claims abstract description 34
- 239000001569 carbon dioxide Substances 0.000 title claims abstract description 34
- 238000011069 regeneration method Methods 0.000 title claims description 30
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 title claims description 21
- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 title claims description 8
- 150000001336 alkenes Chemical class 0.000 title claims description 7
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 105
- 239000003546 flue gas Substances 0.000 claims abstract description 82
- 238000000034 method Methods 0.000 claims abstract description 25
- 229910002091 carbon monoxide Inorganic materials 0.000 claims abstract description 23
- 239000002918 waste heat Substances 0.000 claims abstract description 20
- 239000007789 gas Substances 0.000 claims abstract description 19
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 claims abstract description 17
- 238000010521 absorption reaction Methods 0.000 claims abstract description 16
- 230000008569 process Effects 0.000 claims abstract description 16
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 16
- 239000003054 catalyst Substances 0.000 claims abstract description 15
- -1 alcohol amine Chemical class 0.000 claims abstract description 12
- 238000000926 separation method Methods 0.000 claims abstract description 11
- 238000006243 chemical reaction Methods 0.000 claims abstract description 8
- 239000007788 liquid Substances 0.000 claims abstract description 8
- 238000003795 desorption Methods 0.000 claims abstract description 7
- 230000001172 regenerating effect Effects 0.000 claims abstract description 5
- 238000002156 mixing Methods 0.000 claims abstract description 4
- 238000004939 coking Methods 0.000 claims abstract description 3
- 239000000843 powder Substances 0.000 claims abstract description 3
- 230000008929 regeneration Effects 0.000 claims description 17
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 12
- 229910052760 oxygen Inorganic materials 0.000 claims description 12
- 239000001301 oxygen Substances 0.000 claims description 12
- 239000002737 fuel gas Substances 0.000 claims description 3
- 229910001882 dioxygen Inorganic materials 0.000 claims description 2
- 239000007787 solid Substances 0.000 claims description 2
- 238000001179 sorption measurement Methods 0.000 claims description 2
- 229910052799 carbon Inorganic materials 0.000 abstract description 11
- 238000005265 energy consumption Methods 0.000 abstract description 11
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 abstract description 10
- 238000002485 combustion reaction Methods 0.000 abstract description 2
- 239000000203 mixture Substances 0.000 description 4
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 description 3
- 239000005977 Ethylene Substances 0.000 description 3
- 230000000052 comparative effect Effects 0.000 description 3
- 238000006073 displacement reaction Methods 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 239000007800 oxidant agent Substances 0.000 description 3
- 230000001590 oxidative effect Effects 0.000 description 3
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 description 3
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 description 3
- 230000009919 sequestration Effects 0.000 description 3
- 230000008901 benefit Effects 0.000 description 2
- 239000006227 byproduct Substances 0.000 description 2
- 239000003795 chemical substances by application Substances 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 239000000047 product Substances 0.000 description 2
- 238000011084 recovery Methods 0.000 description 2
- 230000009467 reduction Effects 0.000 description 2
- 239000010865 sewage Substances 0.000 description 2
- 230000009471 action Effects 0.000 description 1
- 238000004364 calculation method Methods 0.000 description 1
- 238000006555 catalytic reaction Methods 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 239000003153 chemical reaction reagent Substances 0.000 description 1
- 230000006835 compression Effects 0.000 description 1
- 238000007906 compression Methods 0.000 description 1
- 230000018109 developmental process Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- 239000005431 greenhouse gas Substances 0.000 description 1
- 239000003915 liquefied petroleum gas Substances 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 239000003208 petroleum Substances 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 239000012492 regenerant Substances 0.000 description 1
- 238000004088 simulation Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
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- 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
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1425—Regeneration of liquid absorbents
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1456—Removing acid components
- B01D53/1475—Removing carbon dioxide
-
- 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
- Y02P30/00—Technologies relating to oil refining and petrochemical industry
- Y02P30/40—Ethylene production
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- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Analytical Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Materials Engineering (AREA)
- Organic Chemistry (AREA)
- Carbon And Carbon Compounds (AREA)
- Gas Separation By Absorption (AREA)
Abstract
The invention discloses a method for regenerating methanol-to-olefin with zero emission of carbon dioxide. The method comprises the following steps: mixing a part of pure oxygen with the circulating flue gas to obtain mixed gas, and feeding the mixed gas and a catalyst to be generated into a regenerator to perform a coking reaction to obtain regenerated flue gas; the other part of the pure oxygen enters a carbon monoxide waste heat boiler; the regenerated flue gas is subjected to cyclone separation to obtain regenerated flue gas without catalyst fine powder, and the regenerated flue gas enters a carbon monoxide waste heat boiler for combustion; part of flue gas of outlet flue gas of the carbon monoxide waste heat boiler is taken as circulating flue gas, the rest flue gas is subjected to low-temperature heat exchange to obtain low-temperature regenerated flue gas, and water is separated by a water separator to obtain dry flue gas; the dry flue gas enters an absorption tower to be in countercurrent contact with the mixed alcohol amine solution, and rich solution is obtained at the bottom of the tower; the rich liquid enters a desorption tower after heat exchange and is rectified and separated to obtain CO with the concentration of more than 99 percent 2 And circulating the alcohol amine solution. The invention adopts pure oxygen and circulating flue gas as main air of the regenerator, thereby greatly improving the efficiency of the regeneratorThe concentration of carbon dioxide in the regenerated flue gas is reduced, and the energy consumption of the subsequent carbon capture process is greatly reduced.
Description
Technical Field
The invention relates to a regeneration method for preparing olefin from methanol with zero emission of carbon dioxide, belonging to the technical field of petroleum processing.
Background
The low-carbon olefin is an important chemical basic raw material, the annual growth rate of propylene exceeds that of ethylene in recent years, the main source of the propylene is the separation of byproducts of ethylene production and FCC liquefied petroleum gas, and the productivity is relatively low. With the change of market conditions and the combination of the characteristics of Chinese energy structures, the MTO process with larger propylene/ethylene product ratio has good development prospect. In the methanol-to-olefin regenerator, the activity of the catalyst is recovered through a scorching reaction, and a great amount of carbon dioxide greenhouse gas is released in the scorching process of the regenerator, so that the reduction of carbon dioxide emission in the regeneration process of the methanol-to-olefin has important significance.
Since the carbon dioxide concentration in the regeneration flue gas is low, usually below 10%, if the carbon capture is performed directly, higher energy consumption will result, and higher carbon dioxide generation concentration usually means lower carbon dioxide capture and compression cost, so increasing the carbon dioxide concentration is an effective way to reduce the carbon capture operation cost.
Chinese patent application (CN 103721742a) discloses a method for regenerating a catalyst for reducing carbon dioxide emission, which uses pure oxygen as an oxidant for coke-burning regeneration. The flue gas at the outlet of the first regenerator is divided into two parts, one part is supplemented to the second regenerator to be used as fluidizing gas, and the other part enters a flue gas energy recovery system. Because the oxygen concentration in the oxidant is higher, the carbon dioxide concentration in the regenerated flue gas can reach more than 50%, the higher carbon dioxide concentration greatly reduces the energy consumption of a subsequent carbon capture device, but the pure oxygen is used as the oxidant, so that the oxygen utilization rate is low, meanwhile, the energy consumption of an air separation device is higher, and the carbon emission reduction effect is limited.
Disclosure of Invention
The invention aims to provide a methanol-to-olefin regeneration method with zero emission of carbon dioxide on the basis of the existing methanol-to-olefin regeneration process so as to reduce carbon emission from the source.
The invention provides a method for regenerating olefin from methanol with zero emission of carbon dioxide, which comprises the following steps:
s1, mixing a part of pure oxygen with the circulating flue gas to obtain a mixed gas, and feeding the mixed gas and a spent catalyst into a regenerator to perform a coking reaction to obtain regenerated flue gas; the other part of the pure oxygen enters a carbon monoxide waste heat boiler;
s2, performing cyclone separation on the regenerated flue gas to obtain regenerated flue gas without catalyst fine powder, feeding the regenerated flue gas into the carbon monoxide waste heat boiler, and combusting the regenerated flue gas with the introduced pure oxygen gas and the introduced fuel gas;
s3, taking part of flue gas of the outlet flue gas of the carbon monoxide waste heat boiler as the circulating flue gas, and performing low-temperature heat exchange on the rest flue gas to obtain low-temperature regenerated flue gas;
s4, separating moisture from the low-temperature regenerated flue gas through a water separator to obtain dry flue gas;
s5, enabling the dry flue gas to enter an absorption tower and to be in countercurrent contact with a mixed alcohol amine solution so as to absorb and enrich carbon dioxide in the dry flue gas, wherein lean gas is obtained at the top of the absorption tower, and rich liquid is obtained at the bottom of the absorption tower;
and S6, the rich solution enters a desorption tower after heat exchange, carbon dioxide with the concentration of more than 99% and a circulating alcohol amine solution are obtained through rectification and separation, the circulating alcohol amine solution and the rich solution enter the absorption tower after heat exchange, and the obtained high-concentration carbon dioxide can be directly used for sequestration or oil displacement treatment.
In the regeneration method, in step S1, the volume fraction of oxygen in the mixed gas is 15 to 25%; if the combustion rate is too slow when the oxygen content is lower than 15%, the oxygen is difficult to be completely consumed, and if the oxygen content is higher than 25%, an excessively high reaction rate is caused near the inlet area, so that the carbon content difference between a local high-temperature area and a local low-temperature area is too large, and the process requirement is not met.
In the regeneration method, in step S1, the temperature of the scorch reaction is 600-690 ℃, and the pressure is 100-200 kPa.
In the regeneration method, in step S1, the regeneration flue gas mainly includes carbon dioxide, carbon monoxide, water vapor and a small amount of oxygen, wherein the volume fraction of the carbon monoxide is 10-20%, and the volume fraction of the oxygen is less than 0.5%.
In the regeneration method, in step S3, the temperature of the flue gas at the outlet of the carbon monoxide waste heat boiler is 160 to 200 ℃, and a heat recovery device is arranged in the carbon monoxide waste heat boiler.
In the regeneration method, in step S3, the circulating flue gas enters the regenerator after being pressurized to 120-220 kPa by a compressor;
the flue gas exchanges heat with the low-temperature heat exchanger to heat domestic hot water;
the temperature of the low-temperature regeneration flue gas is 20-50 ℃.
In the regeneration method, in step S4, the water separator is a low-temperature gas-liquid separation device, a solid adsorption water removal device, or a combination device of a low-temperature heat exchanger and a gas-liquid separation tank;
the temperature of the low-temperature flue gas is 5-40 ℃.
Compared with the existing regeneration method for preparing olefin from methanol, the method has the following main advantages:
1. the heat of the regenerated flue gas is fully utilized, so that the energy loss is reduced;
2. pure oxygen and circulating flue gas are used as main air of the regenerator, so that the concentration of carbon dioxide in the regenerated flue gas is greatly improved, and the energy consumption of a subsequent carbon capture process is greatly reduced;
3. after absorption and desorption processes, high-concentration carbon dioxide gas with the concentration of more than 99 percent is obtained and can be used for sequestration or oil displacement operation.
Drawings
FIG. 1 is a schematic flow diagram of the process of the present invention.
Detailed Description
The experimental procedures used in the following examples are all conventional procedures unless otherwise specified.
Materials, reagents and the like used in the following examples are commercially available unless otherwise specified.
FIG. 1 shows a flow chart of the method of the present invention.
Firstly, pure oxygen 1 is divided into two parts, one part of pure oxygen 2 is mixed with circulating flue gas 15 to obtain mixed gas 4, the other part of pure oxygen 3 directly enters a carbon monoxide waste heat boiler 11, the mixed gas 4 and spent catalyst 5 enter a regenerator 6 for a scorching reaction, and a regenerated catalyst 7 returns to the reactor for a catalytic reaction. The regeneration flue gas 8 is first passed through a three stage cyclone 9 to separate catalyst fines. Then the mixture enters a carbon monoxide waste heat boiler 11, simultaneously, the other part of pure oxygen 3 and a small amount of fuel gas 10 enter the carbon monoxide waste heat boiler 11 at the same time, a part of flue gas 13 discharged by the carbon monoxide waste heat boiler enters a flue gas circulating compressor 14 to be pressurized to obtain circulating flue gas 15, the circulating flue gas is mixed with a part of pure oxygen 2 to obtain mixed gas 4, the other part of flue gas 16 discharged by the carbon monoxide waste heat boiler enters a low-temperature heat exchanger 19 to heat domestic water 17 into high-temperature water 18, then low-temperature regenerated flue gas 20 enters a water separator 21, separated sewage 22 is sent to sewage treatment, dry flue gas 23 enters an absorption tower 24 to enrich carbon dioxide under the absorption action of a mixed alcohol amine solution 29, lean gas 26 discharged from the top of the absorption tower 24 is sent to a chimney, rich liquid 25 discharged from the bottom of the absorption tower 24 is heated by a feeding heat exchanger 28 and then enters a desorption tower 30, the circulating alcohol amine solution 27 discharged from the bottom of the desorption tower 30 is mixed with a fresh alcohol amine solution 31 after heat exchange by the feeding heat exchanger 28 Mixing to obtain mixed alcohol amine solution 29, returning to the absorption tower, and obtaining high-concentration carbon dioxide 32 at the top of the desorption tower 30 for sequestration or oil displacement treatment.
Examples 1,
In order to verify the effect of the invention, according to the process flow chart shown in fig. 1, the energy consumption and the product are subjected to simulation calculation by using flow simulation software.
The properties of the catalyst are shown in Table 1, the compositions of the mixed gas 4, the regenerated flue gas 8, the circulating flue gas 15 and the dry flue gas 23 are shown in Table 2, and the energy consumption of part of the equipment is shown in Table 3. The volume fraction of oxygen in the mixed gas is 22%, the regeneration temperature is 680 ℃, the regeneration pressure is 150kPa, the concentration of carbon monoxide in the regenerated flue gas is 13%, the temperature of the flue gas at the outlet of the carbon monoxide waste heat boiler is 180 ℃, the temperature of the flue gas at the outlet of the low-temperature heat exchanger is 40 ℃, and the final concentration of high-concentration carbon dioxide is 99.9%.
Comparative examples 1,
The same spent catalyst as in example 1 was regenerated using a conventional methanol-to-olefins regeneration process and a carbon dioxide absorption process, with the main air being air, the oxygen volume fraction of which was 21%, the carbon monoxide waste heat boiler outlet temperature being 180 ℃, and the high concentration carbon dioxide obtained at the top of the desorber being 99%. The catalyst properties are listed in table 1, the regenerator main air and regeneration flue gas compositions are listed in table 2, and part of the plant energy consumption is summarized in table 3.
As can be seen from tables 2 and 3, compared with comparative example 1, the method for regenerating olefin from methanol with zero emission of carbon dioxide provided by the invention can fully utilize the heat of the regenerated flue gas, increase the comprehensive steam production, produce hot water as a byproduct, and greatly improve the concentration of carbon dioxide in the regenerated flue gas, so that the energy consumption for capturing carbon dioxide is greatly reduced, and the economic benefit is obviously increased.
TABLE 1 Properties of the catalysts
| Average particle diameter of spent agent, mum | 80 |
| The carbon content of the agent to be generated is wt% | 6.6 |
| The carbon content of the regenerant is wt% | 1.6 |
TABLE 2 composition of the gases
TABLE 3 energy consumption of the respective treatment modes
| Item, unit | Example 1 | Comparative example 1 |
| Steam yield, t/h, of external heat collector of regenerator | 119 | 120 |
| Steam yield, t/h of waste heat boiler | 61 | 56 |
| High temperature water yield of low temperature heat exchanger, t/h | 60 | 0 |
| Power of the flue gas circulating compressor, GJ/h | 1.7 | 0 |
| Carbon dioxide Capture energy consumption, GJ/ |
12 | 48 |
Claims (7)
1. A method for regenerating olefin from methanol with zero emission of carbon dioxide comprises the following steps:
s1, mixing a part of pure oxygen with the circulating flue gas to obtain a mixed gas, and feeding the mixed gas and a spent catalyst into a regenerator to perform a coking reaction to obtain regenerated flue gas; the other part of the pure oxygen enters a carbon monoxide waste heat boiler;
s2, performing cyclone separation on the regenerated flue gas to obtain regenerated flue gas without catalyst fine powder, feeding the regenerated flue gas into the carbon monoxide waste heat boiler, and combusting the regenerated flue gas with the introduced pure oxygen gas and the introduced fuel gas;
s3, taking part of flue gas of the outlet flue gas of the carbon monoxide waste heat boiler as the circulating flue gas, and performing low-temperature heat exchange on the rest flue gas to obtain low-temperature regenerated flue gas;
s4, separating moisture from the low-temperature regenerated flue gas through a water separator to obtain dry flue gas;
s5, enabling the dry flue gas to enter an absorption tower and to be in countercurrent contact with a mixed alcohol amine solution so as to absorb and enrich carbon dioxide in the dry flue gas, wherein lean gas is obtained at the top of the absorption tower, and rich liquid is obtained at the bottom of the absorption tower;
and S6, the rich solution enters a desorption tower after heat exchange, carbon dioxide with the concentration of more than 99% and a circulating alcohol amine solution are obtained through rectification and separation, and the circulating alcohol amine solution enters the absorption tower after heat exchange with the rich solution.
2. The regeneration method according to claim 1, characterized in that: in step S1, the volume fraction of oxygen in the mixed gas is 15 to 25%.
3. Regeneration method according to claim 1 or 2, characterized in that: in step S1, the temperature of the scorch reaction is 600-690 ℃, and the pressure is 100-200 kPa.
4. Regeneration process according to any one of claims 1 to 3, characterized in that: in step S1, in the regeneration flue gas, the volume fraction of carbon monoxide is 10 to 20%, and the volume fraction of oxygen is less than 0.5%.
5. Regeneration process according to any one of claims 1 to 4, characterized in that: in the step S3, the temperature of the flue gas at the outlet of the carbon monoxide waste heat boiler is 160-200 ℃.
6. Regeneration process according to any one of claims 1 to 5, characterized in that: in the step S3, the circulating flue gas enters the regenerator after being pressurized to 120-220 kPa by a compressor;
the flue gas exchanges heat with the low-temperature heat exchanger to heat domestic hot water;
the temperature of the low-temperature regeneration flue gas is 20-50 ℃.
7. Regeneration process according to any one of claims 1 to 6, characterized in that: in step S4, the water separator is a low-temperature gas-liquid separation device, a solid adsorption water removal device, or a combination device of a low-temperature heat exchanger and a gas-liquid separation tank;
the temperature of the dry flue gas is 5-40 ℃.
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| CN202210654904.0A CN115055212A (en) | 2022-06-10 | 2022-06-10 | Regeneration method for preparing olefin from methanol with zero emission of carbon dioxide |
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| CN109200759A (en) * | 2018-09-05 | 2019-01-15 | 中石化上海工程有限公司 | The recovery method of methanol-to-olefins device pressure energy |
| CN110876958A (en) * | 2018-09-06 | 2020-03-13 | 中国科学院大连化学物理研究所 | Method for regenerating carbon deposition catalyst and co-producing carbon monoxide |
| CN113877371A (en) * | 2021-11-10 | 2022-01-04 | 中国石油大学(北京) | Catalytic cracking regeneration method with zero emission of carbon dioxide |
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