CN101314126B - Steam cracking catalyst, preparation and application thereof - Google Patents
Steam cracking catalyst, preparation and application thereof Download PDFInfo
- Publication number
- CN101314126B CN101314126B CN2007100998446A CN200710099844A CN101314126B CN 101314126 B CN101314126 B CN 101314126B CN 2007100998446 A CN2007100998446 A CN 2007100998446A CN 200710099844 A CN200710099844 A CN 200710099844A CN 101314126 B CN101314126 B CN 101314126B
- Authority
- CN
- China
- Prior art keywords
- catalyst
- calcium aluminate
- oxide
- carrier
- rare earth
- 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.)
- Active
Links
Classifications
-
- 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
- Y02P20/52—Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts
Landscapes
- Catalysts (AREA)
Abstract
The present invention provides a catalyst for preparing low carbon olefin by steam cracking, a preparation method and an application thereof. The catalyst by weight percent contains 1 to 10 percent of calcium aluminate, and 90 to 99 percent of other aluminiferous compound carriers except the calcium aluminate with the specific surface area between 80 and 300m<2>/g. The catalyst has the advantages of suitable pore structure, high catalytic activity, low reaction temperature, high mechanical strength and so on. The method for preparing the low carbon olefin by using the catalyst has the advantages of high air speed, high percent conversion and high yield of the low carbon olefin.
Description
Technical field
The invention relates to cracking petroleum hydrocarbon vapor and produce the catalyst and the application thereof of low-carbon alkene, in particular, the present invention is to be catalyst and the application thereof that raw material is produced ethene and propylene with the petroleum hydrocarbon.
Background technology
The tube furnace steam cracking technology dominates in petroleum hydrocarbon cracking ethylene preparation and production of propylene all the time, its technology is gradually improved, but the problem that exists mainly contains at present: the energy consumption height, and the steam cracking process consumed energy accounts for 40% of whole petrochemical enterprise at present; Ethene, propene yield are difficult to improve again, in recent years, because reaction condition harsh more (is that 900 ℃, the time of staying are 0.1 second as the millisecond furnace cracking temperature) is subjected to the restriction of furnace tube material, is difficult to improve ethene, propene yield by the severity that improves cracking reaction again; Harsh reaction condition makes the easier coking of boiler tube and has shortened the cycle of burning, and damages easily owing to carburizing makes boiler tube.Various countries researcher research thinks that the method for catalytic pyrolysis can effectively address the above problem.Catalytic pyrolysis is meant the hydrocarbon cracking reaction of carrying out in the presence of catalyst, can reduce reaction temperature, improves selectivity and product yield.
CN1317545A discloses a kind of catalyst for steam cracking reaction, by CaO/Al
2O
3Crystallization calcium aluminate and the oxide of molybdenum and/or vanadium of mol ratio in 1/6 to 3 scope form, described two kinds of oxide content sums are 0.5～10 weight %, its preparation method is at first to prepare the calcium aluminate presoma with the homogeneous phase preparation method, the calcium aluminate presoma makes the crystallization calcium aluminate 1300～1400 ℃ of roastings then, with the granular crystal calcium aluminate in the salting liquid that contains molybdenum and vanadium, flood, dry, roasting forms, this catalyst shows higher activity in steam cracking.
US2003070963A1 discloses a kind of hydrocarbon vapours cleavage method and consersion unit, and inside reactor has the coating that the coating of catalytic activity is calcium aluminate and alkali metal vanadate or pyrovanadic acid potassium in this method.
Calcium aluminate is because of the difference of CaO content, and CaO.6Al is arranged
2O
3, CaO.2Al
2O
3, 3CaO.5Al
2O
3, CaO.Al
2O
3, 5CaO.3Al
2O
3, 12CaO.7Al
2O
3, 2CaO.Al
2O
3And 3CaO.Al
2O
3Multiple thing phase, research think catalytic activity best be 12CaO.7Al
2O
3The calcium aluminate catalyst.But seldom about the report of calcium aluminate Preparation of Catalyst, generally all adopt corresponding calcium salt and aluminium salt mechanical mixture, through the method preparation of high-temperature roasting, owing to mix the influence of degree, can cause to have several calcium aluminate thing phases in the catalyst, influence its catalytic activity.
US20030109376A1 discloses a kind of preparation 12CaO.7Al
2O
3Method, the salting liquid of calcic and aluminium is mixed with multicomponent organic acid, be prepared into 12CaO.7Al through spray-drying and high-temperature roasting
2O
3Catalyst, but in preparation catalyst process, need 1300～1400 ℃ high-temperature roasting in this way, its energy consumption is very high, and the specific area of catalyst is very little simultaneously, makes activity of such catalysts center decreased number, and activity of such catalysts and conversion ratio are low.
Summary of the invention
One of purpose of the present invention provides a kind of moulding, mechanical strength height, steam cracking catalyst that catalytic activity is high of being easy to.
Two of purpose of the present invention provides a kind of preparation method of steam cracking catalyst.
Three of purpose of the present invention provides the method that a kind of steam cracking is produced low-carbon alkene.
Steam cracking catalyst provided by the invention, this catalyst contains the calcium aluminate of 1～10 weight %, other aluminum contained compound carriers except that calcium aluminate of 90～99 weight %, the specific area of this catalyst is 80～300m
2/ g.
Preferred this catalyst also contains and is not more than 3 weight %, preferredly consist of the calcium aluminate that this catalyst contains 1～9.9 weight %, other aluminum contained compound carriers except that calcium aluminate of 90～98.9 weight %, the rare earth oxide of 0.1～3 weight % and/or transition metal oxide.
In the catalyst provided by the invention, described catalyst is by the method for flooding calcium aluminate to be loaded on the aluminum contained compound carrier to obtain, or the method by step impregnation is calcium aluminate, and rare earth oxide and/or transition metal oxide load on and obtain on the aluminum contained compound carrier.
In the catalyst provided by the invention, CaO/Al in the described calcium aluminate
2O
3Mol ratio be 1/6～3, preferred CaO/Al
2O
3Mol ratio is 12/7 calcium aluminate.Described aluminum contained compound carrier is aluminium oxide or magnesium aluminate spinel compound, wherein preferred α-Al
2O
3
In the catalyst provided by the invention, described rare earth oxide and/or transition metal oxide are selected from cerium oxide, iron oxide, perovskite oxide and the manganese oxide one or more mixture, wherein preferred cerium oxide.
The calcium aluminate preparation method who reports in patent and the document generally has three kinds: (1) aluminium salt and calcium salt are through fully mixed, and roasting makes calcium aluminate under high temperature (more than 1300 ℃) then; (2) adopt the homogeneous phase preparation method that aluminium salt and calcium salt soln mixing back is spray-dried, ((more than 1300 ℃) roasting down make calcium aluminate at high temperature then; (3) on reactor, adopt the method for coating to make the calcium aluminate Catalytic Layer.All there is a problem in all these methods, and the specific area of the calcium aluminate catalyst that makes exactly is very little, so its active sites quantity is few.The method of employing step impregnation provided by the invention with the catalyst of active constituent loading on porous carrier have with prior art in the different microstructure of catalyst for preparing, active component is distributed in the top layer, duct of catalyst surface and porous carrier, improve specific surface area of catalyst, increased the active sites quantity that contacts with reactant.
Simultaneously, the inventor discovers that formed smooth surface became coarse when high temperature sintering originally after enclosing skim calcium aluminate active component on the carrier surface, so the specific area of carrier has increased about 20% after the load.
In calcium aluminate compound, add a small amount of rare earth oxide and/or transition metal oxide, can improve its activity in the steam cracking reaction process, obviously reduce reaction temperature.
The specific area of catalyst provided by the invention improves greatly than conventional calcium aluminate catalyst, by 0.25m
2/ g brings up to 86～185m
2/ g, average pore size is reduced to 86.4～175 dusts by 775 dusts, and pore structure is preferably; Pure calcium aluminate (12CaO.7Al with routine
2O
3) compare, the catalytic activity of catalyst provided by the invention (calcium aluminate content is 2.91%～8.97%) is higher, and conversion ratio improves 7.99～16.95 percentage points, and the productive rate of ethene+propylene+butadiene improves about 3.49～10.36 percentage points; Have also that reaction temperature is low, the mechanical strength advantages of higher.
The preparation method of steam cracking catalyst provided by the invention is respectively according to the contained component difference of catalyst:
The concrete steps that preparation only contains the catalyst of calcium aluminate, the aluminum contained compound carrier except that calcium aluminate are:
(1) salting liquid that will contain aluminium and calcium floods carrier;
(2) soaked carrier being placed temperature is to carry out drying in 100～150 ℃ the environment;
(3) the above-mentioned soaked carrier of roasting obtained catalyst at least in 2 hours in 800～1200 ℃ temperature range.
The concrete steps that preparation contains the catalyst of calcium aluminate, aluminum contained compound carrier, rare earth oxide and/or transition metal oxide except that calcium aluminate are:
(1) salting liquid that will contain aluminium and calcium floods carrier;
(2) soaked carrier being placed temperature is to carry out drying in 100～150 ℃ the environment;
(3) the above-mentioned soaked carrier of roasting at least 2 hours in 800～1200 ℃ temperature range;
(4) solution that will contain rare earth metal salt and/or transition metal salt floods the carrier of above-mentioned load crystalline phase calcium aluminate;
(5) soaked carrier being placed temperature is to carry out drying in 100～150 ℃ the environment;
(6) in 500～650 ℃ of temperature ranges, above-mentioned dried carrier roasting was obtained catalyst at least in 4 hours.
In the Preparation of catalysts method provided by the invention, the salt of described calcic is calcium acetate and/or calcium nitrate, and the described salt that contains aluminium is aluminum nitrate, describedly contains rare earth metal salt and/or transition metal salt is a nitrate.
The preparation method of steam cracking catalyst provided by the invention, sintering temperature is low, the saving energy consumption, and the requirement of active component is still less.
Steam cracking provided by the invention is produced the method for low-carbon alkene, is hydrocarbon oil crude material and steam are introduced in the reactor, and be that 720～800 ℃, water-oil factor are 0.5～2.0, air speed is 1～100h in temperature
-1Condition under, contact with catalyst arbitrary in the claim 1～9 and to react, the separating reaction afterproduct obtains low-carbon alkene.
In the method provided by the invention, described hydrocarbon oil crude material is selected from one or more the mixture in C1～C8 lighter hydrocarbons, naphtha, kerosene, light diesel fuel and the heavy oil.
In the method provided by the invention, described reactor can be fixed bed reactors, also can be fluidized-bed reactor, moving-burden bed reactor or riser reactor.
The method that steam cracking provided by the invention is produced low-carbon alkene has the air speed height, conversion ratio height, the advantage that productivity of low carbon olefin hydrocarbon is high.As in embodiment and Comparative Examples as seen, method conversion ratio provided by the invention improves 7.99～16.95 percentage points, the productive rate of ethene+propylene+butadiene improves about 3.49～10.36 percentage points.
The specific embodiment
The following examples will give further instruction to method provided by the invention, but not thereby limiting the invention.
Among Comparative Examples and the embodiment, the specific area of catalyst and average pore size adopt RIPP145-90 standard method (seeing volumes such as " petrochemical industry analytical method " (RIPP test method) Yang Cuiding, Science Press, nineteen ninety publication) to measure by nitrogen adsorption capacity method;
Reagent among Comparative Examples and the embodiment is chemical pure.
Comparative Examples 1
The 12CaO.7Al of pure phase in the Comparative Examples 1 explanation prior art
2O
3The preparation method.
With 151 gram calcium nitrate (CaC
2H
6O
4H
2O) and 375.13 gram aluminum nitrate (Al (NO
3)
39H
2O) be dissolved in and make solution in the distilled water, add 393.1 gram citric acids.The spray-dried machine spray thing of the homogeneous phase solution of gained is also dry, 1350 ℃ of roastings 4 hours, makes crystalline phase calcium aluminate catalyst D, and structure is 12CaO.7Al
2O
3Measure the specific area and the average pore size of catalyst, and the crushing strength of catalyst, the results are shown in Table 1.
Embodiment 1～4 explanation Preparation of catalysts method provided by the invention.
Embodiment 1
With 500 gram α-Al
2O
3In the solution that contains 18.98 gram calcium acetates and 323.39 gram aluminum nitrates, carry out saturated dipping, then in 120 ℃ of dryings 4 hours, 850 ℃ of roastings 4 hours; Catalyst after the roasting is being contained 18.92 gram cerous nitrate (Ce (NO
3)
36H
2O) saturated dipping in the solution, 110 ℃ of dryings 4 hours, 550 ℃ of roastings 5 hours, the catalyst A 1 that makes contains α-Al of 89.68%
2O
3Carrier, 8.97% calcium aluminate, CaO/Al
2O
3Mol ratio be 1/4, contain 1.35% cerium oxide.Measure the specific area and the average pore size of catalyst, and the crushing strength of catalyst, the results are shown in Table 1.
Embodiment 2
With 500 gram α-Al
2O
3In the solution that contains 27.87 gram calcium acetates and 118.71 gram aluminum nitrates, carry out saturated dipping, then in 120 ℃ of dryings 4 hours, 900 ℃ of roastings 4 hours; With the saturated dipping in the solution that contains 31.53 gram cerous nitrates of the catalyst after the roasting, flooded back 110 ℃ of dryings 4 hours, 500 ℃ of roastings 5 hours, the catalyst A 2 that makes contains α-Al of 93.02%
2O
3Carrier, 4.65% calcium aluminate, CaO/Al
2O
3Mol ratio be 1/1, contain 2.33% cerium oxide.Measure the specific area and the average pore size of catalyst, and the crushing strength of catalyst, the results are shown in Table 1.
Embodiment 3
With 500 gram α-Al
2O
3Containing 71.56 gram calcium nitrate (Ca (NO
3)
24H
2O) and in the solution of 132.62 gram aluminum nitrates carry out saturated dipping, then in 120 ℃ of dryings 4 hours, 1000 ℃ of roastings 4 hours; Catalyst after the roasting is being contained 20.2 gram ferric nitrate (Fe (NO
3)
39H
2O) saturated dipping in the solution, 110 ℃ of dryings 4 hours, 600 ℃ of roastings 4 hours, the catalyst A 3 that makes contains α-Al of 92.76%
2O
3Carrier, 6.49% calcium aluminate, CaO/Al
2O
3Mol ratio be 12/7, contain 0.75% iron oxide.Measure the specific area and the average pore size of catalyst, and the crushing strength of catalyst, the results are shown in Table 1.
Embodiment 4
500 gram magnesium aluminate spinels are carried out saturated dipping in the solution that contains 27.3 gram calcium acetates and 46.5 gram aluminum nitrates, then in 120 ℃ of dryings 4 hours, 1100 ℃ of roastings 4 hours, the catalyst A 4 that makes contains 97.09% magnesium aluminate spinel, 2.91% calcium aluminate, CaO/Al
2O
3Mol ratio be 5/2.Measure the specific area and the average pore size of catalyst, and the crushing strength of catalyst, the results are shown in Table 1.
Comparative Examples 2
The effect that the catalytic pyrolysis hydrocarbon ils of the pure crystalline phase calcium aluminate catalyst of this Comparative Examples explanation Comparative Examples 1 preparation is produced low-carbon alkene.
On the small fixed catalyst test apparatus, reactor capacity is 10ml, the catalyst D that Comparative Examples is made packs in the reactor, in reactor, feed normal octane and water vapour, carry out steam cracking reaction, separating obtained gaseous products is analyzed with gas-chromatography, and feedstock property sees Table 2, reaction condition and the results are shown in Table 3.
The effect that embodiment 5～8 explanations catalyst cracking hydrocarbon ils provided by the invention is produced low-carbon alkene.
Embodiment 5
The catalyst A 1 that embodiment 1 is made is packed in the fixed bed reactors, in reactor, feed normal octane and water vapour, carry out steam cracking reaction, separating obtained gaseous products is analyzed with gas-chromatography, feedstock property sees Table 2, reaction condition and the results are shown in Table 3.
Embodiment 6
The catalyst A 2 that embodiment 2 is made is packed in the fixed bed reactors, in reactor, feed naphtha and water vapour, carry out steam cracking reaction, separating obtained gaseous products is analyzed with gas-chromatography, feedstock property sees Table 2, reaction condition and the results are shown in Table 3.
Embodiment 7
The catalyst A 3 that embodiment 3 is made is packed in the fixed bed reactors, in reactor, feed light diesel fuel and water vapour, carry out steam cracking reaction, separating obtained gaseous products is analyzed with gas-chromatography, feedstock property sees Table 2, reaction condition and the results are shown in Table 3.
Embodiment 8
The catalyst A 4 that embodiment 3 is made is packed in the fixed bed reactors, feeds heavy oil and water vapour in reactor, carries out steam cracking reaction, and separating obtained gaseous products is analyzed with gas-chromatography, and feedstock property sees Table 2, reaction condition and the results are shown in Table 3.
Table 1
| Comparative Examples 1 | Embodiment 1 | Embodiment 2 | Embodiment 3 | Embodiment 4 | |
| Catalyst | D | A1 | A2 | A3 | A4 |
| Form | Calcium aluminate 100% | α-Al 2O 389.68% calcium aluminate, 8.97% cerium oxide 1.35% | α-Al 2O 393.02% calcium aluminate, 4.65% cerium oxide 2.33% | α-Al 2O 392.76% calcium aluminate, 6.49% iron oxide 0.75% | Magnesium aluminate spinel 97.09% calcium aluminate 2.91% |
| CaO/Al 2O 3 | 12/7 | 1/4 | 1/1 | 12/7 | 5/2 |
| Specific area, m 2/g | 0.25 | 136 | 185 | 154 | 86 |
| Average pore size, dust | 775 | 175 | 86.4 | 126 | 157 |
| Crushing strength, kg/cm 2 | 2.3 | 19.7 | 19.7 | 19.7 | 19.7 |
By data in the table 1 as seen, compare with conventional calcium aluminate catalyst, specific surface area of catalyst provided by the invention improves, by 0.25m
2/ g brings up to 86～185m
2/ g, average pore size is reduced to 86.4～175 dusts by 775 dusts, and pore size distribution is more reasonable.Because crushing strength has directly reflected the mechanical strength of catalyst, the mechanical strength of visible catalyst has improved 7.5 times.
Table 2
| Normal octane | Naphtha | Light diesel fuel | Heavy oil | |
| Density (20 ℃), g/cm 3 | 0.703 | 0.7374 | 0.8090 | 0.8425 |
| The BMCI value | -0.03 | 19.48 | 17.58 | 22.54 |
| Refractive power, n d 20 | 1.3976 | 1.4163 | 1.4528 | |
| Elementary analysis Cm%Hm%SppmNppm | 84.2115.7900 | 85.2014.731101.1 | 85.9314.0046754.47 | 86.1113.771234292 |
| Boiling range, ℃ IBP10%～30%50%～70%90%～95%FBP | 125.7125.7125.7125.7125.7 | 4277～103119～135152～159169 | 167205～242276～304339～356>360 | 227298～332355～376396～405420 |
Table 3
By table 3 data as seen, with the pure calcium aluminate (12CaO.7Al of routine
2O
3) compare, the activity of catalyst provided by the invention (calcium aluminate content is 2.91%～8.97%) is higher, and conversion ratio improves 7.99～16.95 percentage points, and the productive rate of ethene+propylene+butadiene improves about 3.49～10.36 percentage points.
Claims (11)
1. steam cracking producing light olefins catalyst, it is characterized in that this catalyst contains the calcium aluminate of 1～10 weight %, other aluminum contained compound carriers except that calcium aluminate of 90～99 weight %, also contain the rare earth oxide and/or the transition metal oxide that are not more than 3 weight %, the specific area of this catalyst is 80～300m
2/ g; Described rare earth oxide and/or transition metal oxide are selected from cerium oxide, iron oxide, perovskite oxide and the manganese oxide one or more mixture.
2. according to the catalyst of claim 1, it is characterized in that described catalyst contains the calcium aluminate of 1～9.9 weight %, other aluminum contained compound carriers except that calcium aluminate of 90～98.9 weight %, the rare earth oxide of 0.1～3 weight % and/or transition metal oxide.
3. according to the catalyst of claim 1 or 2, it is characterized in that this catalyst is by the method for flooding calcium aluminate to be loaded on the aluminum contained compound carrier to obtain, or the method by step impregnation is calcium aluminate, and rare earth oxide and/or transition metal oxide load on and obtain on the aluminum contained compound carrier.
4. according to the catalyst of claim 1 or 2, it is characterized in that described aluminum contained compound carrier is aluminium oxide or magnesium aluminate spinel compound.
5. according to the catalyst of claim 4, it is characterized in that described aluminum contained compound carrier is α-Al
2O
3
6. according to the catalyst of claim 1, it is characterized in that CaO/Al in the described calcium aluminate
2O
3Mol ratio is 1/6～3.
7. according to the catalyst of claim 1, described rare earth oxide is a cerium oxide.
8. claim 1 or 2 Preparation of catalysts method is characterized in that the concrete steps of this method are:
(1) salting liquid that will contain aluminium and calcium floods carrier;
(2) soaked carrier being placed temperature is to carry out drying in 100～150 ℃ the environment;
(3) the above-mentioned soaked carrier of roasting at least 2 hours in 800～1200 ℃ temperature range;
(4) solution that will contain rare earth metal salt and/or transition metal salt floods the carrier of above-mentioned load crystalline phase calcium aluminate;
(5) soaked carrier being placed temperature is to carry out drying in 100～150 ℃ the environment;
(6) in 500～650 ℃ of temperature ranges, above-mentioned dried carrier roasting was obtained catalyst at least in 4 hours.
9. according to the preparation method of claim 8, the salt that it is characterized in that described calcic is calcium acetate and/or calcium nitrate, and the described salt that contains aluminium is aluminum nitrate, and described rare earth metal salt and/or transition metal salt are nitrate.
10. a steam cracking is produced the method for low-carbon alkene, it is characterized in that hydrocarbon oil crude material and steam are introduced in the reactor, and be that 720～800 ℃, water-oil factor are 0.5～2.0, air speed is 1～100h in temperature
-1Condition under, contact with catalyst arbitrary in the claim 1～7 and to react, the separating reaction afterproduct obtains low-carbon alkene.
11., it is characterized in that described hydrocarbon oil crude material is selected from one or more the mixture in C1～C8 lighter hydrocarbons, naphtha, kerosene, light diesel fuel and the heavy oil according to the method for claim 10.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2007100998446A CN101314126B (en) | 2007-05-31 | 2007-05-31 | Steam cracking catalyst, preparation and application thereof |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2007100998446A CN101314126B (en) | 2007-05-31 | 2007-05-31 | Steam cracking catalyst, preparation and application thereof |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN101314126A CN101314126A (en) | 2008-12-03 |
| CN101314126B true CN101314126B (en) | 2011-07-20 |
Family
ID=40105364
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2007100998446A Active CN101314126B (en) | 2007-05-31 | 2007-05-31 | Steam cracking catalyst, preparation and application thereof |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN101314126B (en) |
Families Citing this family (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101858901B (en) * | 2010-07-07 | 2011-12-21 | 中国汽车技术研究中心 | System and method for testing activity of vehicle exhaust purification catalytic material |
| US9643163B2 (en) * | 2014-10-10 | 2017-05-09 | Crystaphase Products, Inc. | Heterogeneous catalyst for transesterification and method of preparing same |
| WO2016168697A1 (en) | 2015-04-17 | 2016-10-20 | Crystaphase Products, Inc. | Heterogeneous catalyst for transesterification and method of preparing same |
| CN107812542B (en) * | 2016-09-14 | 2020-10-23 | 中国石油化工股份有限公司 | Alpha-alumina carrier and preparation method and application thereof |
| CN109705913B (en) * | 2017-10-26 | 2021-05-14 | 中国石油化工股份有限公司 | Method and system for producing high-octane gasoline and low-carbon olefins in high yield |
| CN111760571A (en) * | 2020-07-14 | 2020-10-13 | 西安石油大学 | Preparation method and application of calcium aluminate catalyst capable of regulating olefin selectivity |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1317545A (en) * | 1999-12-17 | 2001-10-17 | 恩尼彻姆公司 | Catalyst for steam cracking reaction |
| CN1317546A (en) * | 1999-12-17 | 2001-10-17 | 恩尼彻姆公司 | Catalyst for steam cracking reaction and related preparing method |
| CN1612782A (en) * | 2000-12-06 | 2005-05-04 | 波利玛利欧洲股份公司 | Process for the regeneration of catalysts for steam cracking |
-
2007
- 2007-05-31 CN CN2007100998446A patent/CN101314126B/en active Active
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1317545A (en) * | 1999-12-17 | 2001-10-17 | 恩尼彻姆公司 | Catalyst for steam cracking reaction |
| CN1317546A (en) * | 1999-12-17 | 2001-10-17 | 恩尼彻姆公司 | Catalyst for steam cracking reaction and related preparing method |
| CN1612782A (en) * | 2000-12-06 | 2005-05-04 | 波利玛利欧洲股份公司 | Process for the regeneration of catalysts for steam cracking |
Also Published As
| Publication number | Publication date |
|---|---|
| CN101314126A (en) | 2008-12-03 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101314126B (en) | Steam cracking catalyst, preparation and application thereof | |
| CN101341230B (en) | Novel cracking catalytic compositions | |
| CN101024196A (en) | Catalyst for catalytic cracking of heavy oil and process for producing olefin and fuel oil | |
| KR20150133742A (en) | Method for manufacturing catalytic cracking catalyst for hydrocarbon oil | |
| CN1298425C (en) | Aromatization catalyst, its preparation method and application | |
| CN104437511B (en) | Catalyst for producing light olefins by fixed bed and preparation method for catalyst for producing light olefins by fixed bed | |
| WO1996034685A1 (en) | Catalyst and process for preparing same | |
| CN107913729B (en) | Composite catalyst and preparation method thereof | |
| CN101905168A (en) | Catalytic cracking assistant capable of increasing propylene yield with sulfur transfer agent function | |
| US11529612B2 (en) | Composition capable of reducing CO and NOx emissions, preparation method therefor and use thereof, and fluid catalytic cracking method | |
| CN102019198B (en) | Preparation and application of heavy metal pollution-resisting dual functional solid cocatalyst | |
| CN100395314C (en) | Aromatization catalyst, preparation method, and application | |
| CN107267190B (en) | A kind of method of high olefin content gasoline upgrading | |
| CN102228839B (en) | Silicon-aluminum dual binding agent vanadium-resisting additive and preparation method thereof | |
| CN110947417B (en) | Catalyst for producing propane and gasoline from alkane, preparation method and application | |
| CN1480255A (en) | Catalyzer for preparing olefine in low carbon number through catalytic cracking and its preparing method and application | |
| CN109569703B (en) | Catalyst for producing gasoline component from naphtha and methanol, preparation method and application | |
| US10413884B2 (en) | Catalytic cracking catalyst for RFCC process with maximized diesel yields and a method for the preparation thereof | |
| CN112742456A (en) | Dehydrogenation cracking catalyst, preparation method thereof and method for producing ethylene and propylene by using hydrocarbon four | |
| CN1031335A (en) | The material that is used to C3 hydrocarbon and C4 hydrocarbon are transformed is formed and method for transformation | |
| CN1301794C (en) | Molecular sieve type catalyst of low carbon olefine by catalizing thermo cracking process | |
| CN102453522B (en) | Catalytic conversion method of high-yield high-octane-number gasoline | |
| CN113355126A (en) | Crude oil catalytic cracking method | |
| CN1915920A (en) | Method for producing ethene, propylene through catalytic cracking | |
| US20040004024A1 (en) | Method for increasing yields of light oil and total liquid products, promoting the combustion of CO and reducing NOx emission in flue gas in the petroleum refining FCC process and the improved FCC catalyst |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant |