CN1160437C - Catalytic cracking catalyst with function of reducing sulfur content of gasoline - Google Patents
Catalytic cracking catalyst with function of reducing sulfur content of gasoline Download PDFInfo
- Publication number
- CN1160437C CN1160437C CNB01136971XA CN01136971A CN1160437C CN 1160437 C CN1160437 C CN 1160437C CN B01136971X A CNB01136971X A CN B01136971XA CN 01136971 A CN01136971 A CN 01136971A CN 1160437 C CN1160437 C CN 1160437C
- Authority
- CN
- China
- Prior art keywords
- catalyzer
- zeolite
- gasoline
- rare earth
- metal
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired - Fee Related
Links
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 title claims abstract description 37
- 239000003054 catalyst Substances 0.000 title claims abstract description 37
- 229910052717 sulfur Inorganic materials 0.000 title claims abstract description 14
- 239000011593 sulfur Substances 0.000 title claims abstract description 14
- 238000004523 catalytic cracking Methods 0.000 title abstract description 27
- 229910021536 Zeolite Inorganic materials 0.000 claims abstract description 18
- HNPSIPDUKPIQMN-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical compound O=[Si]=O.O=[Al]O[Al]=O HNPSIPDUKPIQMN-UHFFFAOYSA-N 0.000 claims abstract description 18
- 239000010457 zeolite Substances 0.000 claims abstract description 18
- 239000000463 material Substances 0.000 claims abstract description 14
- 229910052761 rare earth metal Inorganic materials 0.000 claims abstract description 14
- 150000002910 rare earth metals Chemical class 0.000 claims abstract description 14
- 238000005336 cracking Methods 0.000 claims abstract description 12
- 229910044991 metal oxide Inorganic materials 0.000 claims abstract description 11
- 150000004706 metal oxides Chemical class 0.000 claims abstract description 11
- 229910052739 hydrogen Inorganic materials 0.000 claims abstract description 7
- 239000001257 hydrogen Substances 0.000 claims abstract description 7
- 125000004435 hydrogen atom Chemical class [H]* 0.000 claims abstract description 6
- 239000002131 composite material Substances 0.000 claims abstract description 3
- 238000000034 method Methods 0.000 claims description 20
- 230000000694 effects Effects 0.000 claims description 10
- 150000001875 compounds Chemical class 0.000 claims description 9
- 239000002253 acid Substances 0.000 claims description 8
- 239000012153 distilled water Substances 0.000 claims description 8
- 239000000843 powder Substances 0.000 claims description 8
- 150000003839 salts Chemical class 0.000 claims description 8
- 239000000243 solution Substances 0.000 claims description 8
- 238000003756 stirring Methods 0.000 claims description 8
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 8
- 238000002360 preparation method Methods 0.000 claims description 7
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims description 6
- UCKMPCXJQFINFW-UHFFFAOYSA-N Sulphide Chemical compound [S-2] UCKMPCXJQFINFW-UHFFFAOYSA-N 0.000 claims description 6
- 238000001556 precipitation Methods 0.000 claims description 6
- 238000001035 drying Methods 0.000 claims description 4
- 239000012065 filter cake Substances 0.000 claims description 4
- 229910052746 lanthanum Inorganic materials 0.000 claims description 4
- 229910052751 metal Inorganic materials 0.000 claims description 4
- 239000002184 metal Substances 0.000 claims description 4
- 238000000967 suction filtration Methods 0.000 claims description 4
- 206010013786 Dry skin Diseases 0.000 claims description 3
- 229910052684 Cerium Inorganic materials 0.000 claims description 2
- 238000006424 Flood reaction Methods 0.000 claims description 2
- 229910052779 Neodymium Inorganic materials 0.000 claims description 2
- 229910052777 Praseodymium Inorganic materials 0.000 claims description 2
- 229910052772 Samarium Inorganic materials 0.000 claims description 2
- 229910052782 aluminium Inorganic materials 0.000 claims description 2
- 239000007864 aqueous solution Substances 0.000 claims description 2
- 229910052785 arsenic Inorganic materials 0.000 claims description 2
- 238000000975 co-precipitation Methods 0.000 claims description 2
- 229910052802 copper Inorganic materials 0.000 claims description 2
- 238000007598 dipping method Methods 0.000 claims description 2
- 229910052733 gallium Inorganic materials 0.000 claims description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-M hydroxide Chemical compound [OH-] XLYOFNOQVPJJNP-UHFFFAOYSA-M 0.000 claims description 2
- 230000003993 interaction Effects 0.000 claims description 2
- 229910052742 iron Inorganic materials 0.000 claims description 2
- 238000005304 joining Methods 0.000 claims description 2
- 229910000000 metal hydroxide Inorganic materials 0.000 claims description 2
- 150000004692 metal hydroxides Chemical class 0.000 claims description 2
- 229910021645 metal ion Inorganic materials 0.000 claims description 2
- 238000005554 pickling Methods 0.000 claims description 2
- 239000002244 precipitate Substances 0.000 claims description 2
- 239000012266 salt solution Substances 0.000 claims description 2
- 229910052718 tin Inorganic materials 0.000 claims description 2
- 229910052719 titanium Inorganic materials 0.000 claims description 2
- 229910052725 zinc Inorganic materials 0.000 claims description 2
- 229910052726 zirconium Inorganic materials 0.000 claims description 2
- 230000009286 beneficial effect Effects 0.000 abstract description 2
- 230000007613 environmental effect Effects 0.000 abstract description 2
- 239000003546 flue gas Substances 0.000 abstract description 2
- 230000001737 promoting effect Effects 0.000 abstract description 2
- 238000004064 recycling Methods 0.000 abstract description 2
- 239000005864 Sulphur Substances 0.000 description 23
- 238000006243 chemical reaction Methods 0.000 description 7
- 238000006477 desulfuration reaction Methods 0.000 description 7
- 230000023556 desulfurization Effects 0.000 description 7
- 238000004519 manufacturing process Methods 0.000 description 7
- 239000003921 oil Substances 0.000 description 5
- 239000000047 product Substances 0.000 description 5
- YTPLMLYBLZKORZ-UHFFFAOYSA-N Thiophene Chemical compound C=1C=CSC=1 YTPLMLYBLZKORZ-UHFFFAOYSA-N 0.000 description 4
- 230000003009 desulfurizing effect Effects 0.000 description 4
- 238000005984 hydrogenation reaction Methods 0.000 description 4
- 238000005303 weighing Methods 0.000 description 4
- 239000007795 chemical reaction product Substances 0.000 description 3
- 238000013461 design Methods 0.000 description 3
- 239000007789 gas Substances 0.000 description 3
- 229930195733 hydrocarbon Natural products 0.000 description 3
- 150000002430 hydrocarbons Chemical class 0.000 description 3
- 229930192474 thiophene Natural products 0.000 description 3
- 239000004215 Carbon black (E152) Substances 0.000 description 2
- LSDPWZHWYPCBBB-UHFFFAOYSA-N Methanethiol Chemical compound SC LSDPWZHWYPCBBB-UHFFFAOYSA-N 0.000 description 2
- 230000002378 acidificating effect Effects 0.000 description 2
- 239000000654 additive Substances 0.000 description 2
- 230000000996 additive effect Effects 0.000 description 2
- HRKQOINLCJTGBK-UHFFFAOYSA-N dihydroxidosulfur Chemical compound OSO HRKQOINLCJTGBK-UHFFFAOYSA-N 0.000 description 2
- 238000009826 distribution Methods 0.000 description 2
- 238000011156 evaluation Methods 0.000 description 2
- 239000004744 fabric Substances 0.000 description 2
- 238000010438 heat treatment Methods 0.000 description 2
- 238000009775 high-speed stirring Methods 0.000 description 2
- MRELNEQAGSRDBK-UHFFFAOYSA-N lanthanum(3+);oxygen(2-) Chemical compound [O-2].[O-2].[O-2].[La+3].[La+3] MRELNEQAGSRDBK-UHFFFAOYSA-N 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- TVMXDCGIABBOFY-UHFFFAOYSA-N octane Chemical compound CCCCCCCC TVMXDCGIABBOFY-UHFFFAOYSA-N 0.000 description 2
- 239000002245 particle Substances 0.000 description 2
- 238000005504 petroleum refining Methods 0.000 description 2
- 238000012545 processing Methods 0.000 description 2
- 238000007670 refining Methods 0.000 description 2
- 239000007787 solid Substances 0.000 description 2
- 150000003568 thioethers Chemical class 0.000 description 2
- -1 this Chemical compound 0.000 description 2
- 238000006276 transfer reaction Methods 0.000 description 2
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 1
- 150000001336 alkenes Chemical class 0.000 description 1
- 239000010779 crude oil Substances 0.000 description 1
- 239000013078 crystal Substances 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 239000003208 petroleum Substances 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 229920006395 saturated elastomer Polymers 0.000 description 1
- 238000001179 sorption measurement Methods 0.000 description 1
- 150000003577 thiophenes Chemical class 0.000 description 1
Landscapes
- Catalysts (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
A catalytic cracking catalyst with the function of reducing sulfur content in gasoline is prepared from zeolite as cracking active component, rare-earth material as hydrogen transfer promoting center, and the composite oxide of metal oxide with large specific surface area and multiple metal oxides as carrier of catalyst2S, thus facilitating the recycling of sulfur and reducing SO in the flue gasxDischarge and is beneficial to environmental protection.
Description
The present invention relates to a kind of catalytic cracking catalyst that reduces the content of sulfur in gasoline function that has, it is the innovation that belongs in the petroleum refining industry the light-end products process for refining.It mainly is to have developed a kind of novel catalytic cracking catalyst that can reduce the FCC content of sulfur in gasoline, and this catalyzer both can mix use with certain proportion with common FCC catalyzer, also can be used as catalytic cracking catalyst and used separately; Existing catalytic cracking function has the content of sulfur in gasoline of reduction function again.
Gasoline is one of main products in the petroleum refining process.People have often taked the complete processing of many raising light-end products yields in order to obtain more light-end products from crude oil in the process in refining of petroleum, catalytic cracking is exactly one of main processing means, and catalytically cracked gasoline also is its main product.And the sulphur in the gasoline more than 90% from the catalytically cracked gasoline component, thereby the sulphur content that reduces catalytically cracked gasoline is to reduce the key of content of sulfur in gasoline.In order to reduce the sulphur content of catalytically cracked gasoline, all be the method for gasoline being carried out hydrogenation that adopts usually, this method cost height, gasoline octane rating reduces; Though it is a kind of very effective sulfur method that catalytically cracked gasoline is carried out hydrogenation, the cost height of hydrogenation, the octane value of gasoline also can decrease because of alkene is saturated.Though Wormsbecher and Kim (U.S.Pat.No.5,525,210 and U.S.Pat.No.5,376,608) the catalytically cracked gasoline sweetening additive of invention can add in the catalytic cracking reaction process at any time, also the sweetening additive component can be prepared in the catalytic cracking catalyst, can play certain desulfidation, but absolute desulfurization amount is lower, has only about 100 μ g/g, and addition can not arbitrarily increase, otherwise can influence the products distribution of catalytic cracking process.The hydrogenation ability of China refinery is lower, and most catalytically cracked materials are without hydrotreatment.Divide angle to consider from production cost, if can be in catalytic cracking process the sulphur content of gasoline component be reduced to below the national standard, not only can reduce the investment of refinery equipment, and can reduce production link, product purification loss and process cost, thereby reduce production cost.
Purpose of the present invention provides a kind of catalytic cracking catalyst that reduces the content of sulfur in gasoline function that has with regard to being to avoid above-mentioned the deficiencies in the prior art part, this catalyzer not only has the function of common catalytic cracking catalyst, but also have the effect that reduces content of sulfur in gasoline simultaneously, make the sulphur content ratio of the gasoline of production use the sulphur content of the gasoline of common catalytic cracking catalyst production that remarkable reduction is arranged.This catalyzer both can use as catalytic cracking catalyst separately, also can mix use with common catalytic cracking catalyst as one sees fit according to the actual sulphur content situation of the gasoline of producing.Use this catalytic cracking catalyst with gasoline desulfur function, the sulfide overwhelming majority who removes changes into hydro carbons and H
2S is convenient to the recycling of sulphur and the SOx discharging in the minimizing flue gas like this, is beneficial to environmental protection.Because the sulfide in the catalytically cracked material is of a great variety, complex structure behind catalytic cracking reaction, can generate mercaptan, thioether and thiophenes etc., and in the majority with the thiophene-based material.Mercaptan, thioether can be on an acidic catalyst remove wherein sulphur through hydrogen transference, cracking reaction; The thiophene-based material is first cracking open loop on the B acid site of an acidic catalyst earlier then, generates the middle species of thio-alcohol, and species pass through hydrogen transference, cracking reaction again in the middle of the thio-alcohol, and sulphur wherein changes into H
2S removes.Therefore, when this catalytic cracking catalyst with desulfurizing function of design, the inventor considers that catalyzer at first will have suitable hydrocarbon cracking activity and higher sulfide cracking activity, catalyzer also must have the ability of the sulfide in the selective adsorption product gasoline in addition, makes it change into hydrocarbon and H in the heart in cracking activity
2S.So, be to be as catalyzer cracking activity component on catalyst design with zeolitic material, rare earth material promotes the center as the hydrogen transference of catalyzer, the composite oxides that the metal oxide of large specific surface and multiple metal oxide are formed are then as the carrier of catalyzer, be to select the MCM series zeolite on Preparation of catalysts, ZSM-5, the β zeolite, HY and USY etc. have more highly acid material as the cracking activity component, select Cu, Zn, Fe, Al, As, Hg, Ni, Zr, Sn, Ga and Ti etc. have the compound or complex oxide formed than the oxide compound of large specific surface and appropriate acid or by these metal oxides as carrier, consider that sulfide hydrogen transfer reactions in the cracking sweetening process plays a very important role, for promoting hydrogen transfer reactions, in catalyzer, add proper amount of rare-earth, as La, Ce, Pr, the oxide compound of Nd and Sm etc.This Preparation of catalysts is comprehensively to have adopted pickling process and coprecipitation method, promptly can make catalyzer of the present invention by following steps:
(1) floods 0.1～50% rare earth on the acid zeolite, after 5～10 hours,, rare earth is dispersed on the zeolite with the form of oxide compound again 200～700 ℃ of roastings 0.5～10 hour 60～200 ℃ of dryings;
(2) one or more are had the soluble salt of metal of strong affinity interaction and the soluble salt of rare earth to sulfide and be dissolved in the distilled water, be mixed with concentration at 0.5～30% solution.The zeolite of dipping rare earth is ground into fine powder, by 1～80% joining in the metal salt solution of being prepared into finished catalyst.The salts solution that will add zeolite powder with agitator fully stirs, and drips 0.1～25% KOH, NaOH or NH in the process that stirs
3H
2The aqueous solution of O allows the precipitate metal hydroxides that forms equably zeolite be contained;
(3) after metal ion changes into precipitation of hydroxide fully, the throw out that obtains is left standstill 5～10h;
(4) throw out is carried out suction filtration, and with an amount of distilled water wash 3～5 times.The gained filter cake is at 50～200 ℃ of drying 10～24h hours, and roasting 1～24 hour in 300～900 ℃ retort furnace is then pulverized and sieved, and can obtain desired catalyzer.
Below in conjunction with embodiment in detail technical characterstic of the present invention is described in detail.
When actual design and preparation catalyzer of the present invention, the inventor adopts above-mentioned preparation section, adopts different metal oxides to make following two kinds of catalyzer as carrier:
1. embodiment 1. takes by weighing USY zeolite 150g, and wet method was flooded several times and contained the solution that lanthanum trioxide is 0.01g/mL at the beginning of employing was dipped into, and had flooded all dry 1h in 100 ℃ baking oven, then at 500 ℃ of roasting 2h at every turn.Obtain containing 10%La
2O
3La-USY.Grind to form behind the fine powder La-USY standby.2. take by weighing ZrOCl
28H
2O and Al (NO
3)
39H
2Each 200g of O and 2000g join in the beaker of a 2000mL.Add distilled water 500g, under heating condition, constantly stir, make two kinds of salt dissolvings.3. the La-USY powder is joined in this beaker, after fully stirring, under the condition of high-speed stirring, slowly drip NH
3H
2O all becomes solid precipitation to the solution in the beaker.Leave standstill 6h.4. throw out is moved in the cloth formula funnel and carry out suction filtration, and repeatedly wash, remove the NH in the precipitation as far as possible with distilled water
4 +And NO
3 -Filter cake is dry 20h in 150 ℃ baking oven, again roasting 6h in 600 ℃ retort furnace.The break-up of catalyst that obtains, sieve out O.078～particle of 0.18mm.Like this, just, prepared La-USY/ZrO
2/ Al
2O
3Has the catalytic cracking catalyst that reduces the content of sulfur in gasoline function.
Fluidized-bed evaluation result to this catalyzer shows, under suitable reaction conditions and sufficiently high addition condition, compares with using pure FCC catalyzer, and the sulphur content of the gasoline of generation is low more than 35%, and the yield of gasoline and liquefied gas also has obvious the raising.
1. embodiment 2. takes by weighing USY zeolite 150g, and wet method was flooded several times and contained the solution that lanthanum trioxide is 0.01g/mL at the beginning of employing was dipped into, and had flooded all dry 1h in 100 ℃ baking oven, then at 500 ℃ of roasting 2h at every turn.Obtain containing 10%La
2O
3La-USY.Grind to form behind the fine powder La-USY standby.2. take by weighing Zn (NO
3)
26H
2O and Al (NO
3)
39H
2Each 650g of O and 1300g join in the beaker of a 2000mL.Add distilled water 500g, under heating condition, constantly stir, make two kinds of salt dissolvings.3. the La-USY powder is joined in this beaker, after fully stirring, under the condition of high-speed stirring, slowly drip NH
3H
2O all becomes solid precipitation to the solution in the beaker.Leave standstill 6h.4. throw out is moved in the cloth formula funnel and carry out suction filtration, and repeatedly wash, remove the NH in the precipitation as far as possible with distilled water
4 +And NO
3 -Filter cake is dry 20h in 150 ℃ baking oven, again roasting 6h in 600 ℃ retort furnace.The break-up of catalyst that obtains, sieve out the particle of 0.078～0.18mm.Like this, just, prepared La-USY/ZnO
2/ Al
2O
3Has the catalytic cracking catalyst that reduces the content of sulfur in gasoline function.
Undertaken under the blended condition by 3/7 at this catalyzer and common FCC catalyzer, be to react under 5 the condition at 500 ℃, agent-oil ratio, the sulphur content of the gasoline that generates is about 630 μ g/g, with the sulphur content with the gasoline that uses pure FCC catalyzer to generate under the condition be 1116 μ g/g ratios, sulphur content has reduced by 43.5%.As seen, sulphur effect highly significant falls.
Through the fluidized-bed evaluation, prove guaranteeing catalytic cracking production not to be distributed to produce under the situation of bad influence to have tangible sweetening effectiveness by prescription of the present invention and the prepared catalytic cracking catalyst of preparation method with desulfurizing function.With the decompressed wax oil is raw material, experimental result on fluid catalystic cracking reaction evaluating device shows, be respectively in agent-oil ratio, temperature of reaction under 5 and 500 ℃ the condition, the common catalytic cracking catalyst of simple use, sulphur content in the gasoline that generates is 1100 μ g/g (Ignition Lamp Method, down together), after adding the catalyzer with desulfurizing function of preparation, the sulphur content of gasoline reduces with the increase of addition, when use pure developed have the catalyzer of desulfurizing function the time, sulphur content has dropped to 700 μ g/g.Compare with using pure common catalytic cracking catalyst, use pure desulfurization catalyst, sulphur content can reduce more than 35%, and absolute desulfurization amount is about 400 μ g/g.Under 500 ℃, different agent-oil ratio condition, to using the pure FCC catalyzer and the sulphur content comparing result of the gasoline that uses FCC and 30% desulfurization catalyst (DS) blended mixed catalyst to generate to show, increase along with agent-oil ratio, the sulphur content of the gasoline of two kinds of catalyzer generations all descends, and the sulphur content of the gasoline of spent mixed catalyst generation is all hanged down about 250 μ g/g than the sulphur content of the gasoline that uses pure FCC catalyzer to generate.In addition, behind the interpolation desulfurization catalyst, the yield of gasoline and liquefied gas increases along with the increase of desulfurization catalyst addition in the FCC catalyzer, and the yield of dry gas only slightly increases.As seen, this desulfurization catalyst does not have disadvantageous effect to the distribution of catalytic cracking production.This catalyzer is regenerated through repeated multiple times, and activity of such catalysts, stability, specific surface area and crystal phase structure do not have considerable change, illustrates that this catalyzer has good stability.
Claims (2)
1. have the purposes of the catalyzer of reduction content of sulfur in gasoline function as the FCC catalyzer, this catalyzer mainly is by zeolitic material, rare earth material is formed with the metal oxide that has than large specific surface, it is characterized in that this catalyzer is to have more highly acid zeolitic material as catalyzer cracking activity component, rare earth material promotes the center as the hydrogen transference of catalyzer, to have the compound or complex oxide formed than the metal oxide of large specific surface and appropriate acid or by these metal oxides as carrier, wherein said zeolitic material is the MCM series zeolite, ZSM-5, the β zeolite, HY or USY zeolite, the described metal oxide that has than large specific surface and appropriate acid is Cu, Zn, Fe, Al, As, Hg, Ni, Zr, Sn, a kind of oxide compound of Ga or Ti or by several formed composite oxides or complex oxide in these metal oxides, the method for its preparation is comprehensively to adopt pickling process and coprecipitation method:
(1) on acid zeolite, floods 0.1～50% rare earth, after 5～10 hours,, rare earth is dispersed on the zeolite with the form of oxide compound again 200～700 ℃ of roastings 0.5～10 hour 60～200 ℃ of dryings;
(2) one or more are had than the soluble salt of the metal of affinity interaction and the soluble salt of rare earth are dissolved in the distilled water by force sulfide, be mixed with concentration at 0.5～30% solution, the zeolite of dipping rare earth is ground into fine powder, by 1～80% joining in the metal salt solution of being prepared into finished catalyst, the salts solution that will add zeolite powder with agitator fully stirs, and drips 0.1～25% KOH, NaOH or NH in the process that stirs
3H
2The aqueous solution of O allows the precipitate metal hydroxides that forms equably zeolite be contained;
(3) after metal ion changes into precipitation of hydroxide fully, the throw out that obtains was left standstill 5～10 hours;
(4) throw out is carried out suction filtration, and with an amount of distilled water wash 3～5 times, the gained filter cake is 50～200 ℃ of dryings 10～24 hours, and roasting 1～24 hour in 300～900 ℃ retort furnace is then pulverized and sieved, and can obtain desired catalyzer.
2. purposes according to claim 1 is characterized in that described rare earth material is a kind of oxide compound or several oxide compound of La, Ce, Pr, Nd or Sm.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB01136971XA CN1160437C (en) | 2001-12-27 | 2001-12-27 | Catalytic cracking catalyst with function of reducing sulfur content of gasoline |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB01136971XA CN1160437C (en) | 2001-12-27 | 2001-12-27 | Catalytic cracking catalyst with function of reducing sulfur content of gasoline |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1356374A CN1356374A (en) | 2002-07-03 |
| CN1160437C true CN1160437C (en) | 2004-08-04 |
Family
ID=4674046
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNB01136971XA Expired - Fee Related CN1160437C (en) | 2001-12-27 | 2001-12-27 | Catalytic cracking catalyst with function of reducing sulfur content of gasoline |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN1160437C (en) |
Families Citing this family (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103861436B (en) * | 2014-03-20 | 2016-03-30 | 中国石油大学(华东) | Catalytic cracking fuel gas sulfur transfer additive of multiphase and preparation method thereof and application |
| CN109364985A (en) * | 2018-11-13 | 2019-02-22 | 陈开龙 | A kind of catalytic gasoline absorbing desulfurization catalyst and preparation method thereof |
-
2001
- 2001-12-27 CN CNB01136971XA patent/CN1160437C/en not_active Expired - Fee Related
Also Published As
| Publication number | Publication date |
|---|---|
| CN1356374A (en) | 2002-07-03 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101940908B (en) | Ultra-deep absorption desulfurizer for light oil and application thereof | |
| CN101481627B (en) | Hydrocarbon oil desulphurization adsorbing agent and use method thereof | |
| CN102430412B (en) | Method for preparing desulfurizer capable of absorbing catalytic cracking gas at high selection | |
| CN104209142A (en) | Hydrocarbon oil desulfurization catalyst and application method thereof | |
| CN104722311B (en) | Sulfur-transferring additive for regenerative flue gas in catalytic cracking and preparation method thereof | |
| CN111195520B (en) | High-dispersion adsorption desulfurization catalyst and preparation and application thereof | |
| CN104549131A (en) | Adsorption desulfurization additive, as well as preparation method and desulfurization system thereof | |
| CN1978593B (en) | Cracking catalyst | |
| CN104069795A (en) | Gas desulfurization and adsorption composition, preparation method thereof and method for desulfurizing sulfurous gases | |
| CN101327419B (en) | Method for preparing catalytic cracking gasoline adsorbing and desulfurizing agent | |
| CN106238091A (en) | A kind of mercaptan-eliminating catalyst and preparation method and application | |
| CN101619231A (en) | Fuel oil adsorption desulfurization adsorbent and method for preparing same | |
| CN103240117A (en) | Gasoline desulfurization catalyst and preparation method thereof and gasoline desulfurization method | |
| CN101766984A (en) | Desulfuration adsorbent containing phosphorus and preparation method and application thereof | |
| CN103657711A (en) | Catalytic cracking catalyst and preparation method thereof | |
| CN1160437C (en) | Catalytic cracking catalyst with function of reducing sulfur content of gasoline | |
| JPH01500571A (en) | Improved vanadium, rare earth metal-containing spinel compositions and methods of using the same | |
| CN114345329A (en) | Application of normal-pressure ultra-deep desulfurization catalyst | |
| CN1173011C (en) | Desulfurization additive capable of simultaneously reducing sulfur content in gasoline and coke on catalyst | |
| CN106955735B (en) | A kind of method of desulfurization of hydrocarbon oil catalyst and preparation method thereof and desulfurization of hydrocarbon oil | |
| CN100404128C (en) | Catalytic cracking auxiliary agent for reducing sulfur content of gasoline, preparation method and application | |
| CN101433821A (en) | Sorbent for reducing sulfur content in hydrocarbon oils | |
| CN1102640C (en) | Catalytic cracking and desulfurizing catalyst for refining light oil products | |
| CN104107694A (en) | Selective hydrogenation catalyst, preparation method and application thereof | |
| CN102895943A (en) | Hydrocarbon oil desulphurization adsorbent, and preparation method and application thereof |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C06 | Publication | ||
| PB01 | Publication | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CF01 | Termination of patent right due to non-payment of annual fee | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20040804 Termination date: 20201227 |