CN1332755C - Conversion catalyst for preparing small molecule olefin - Google Patents
Conversion catalyst for preparing small molecule olefin Download PDFInfo
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- CN1332755C CN1332755C CNB2004100689311A CN200410068931A CN1332755C CN 1332755 C CN1332755 C CN 1332755C CN B2004100689311 A CNB2004100689311 A CN B2004100689311A CN 200410068931 A CN200410068931 A CN 200410068931A CN 1332755 C CN1332755 C CN 1332755C
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Abstract
The present invention relates to a catalytic conversion catalyst for preparing small molecular alkene, which comprises 10 to 70 wt% of clay, 5 to 75 wt% of inorganic oxide and 10 to 65 wt% of zeolite base on catalyst weight. The zeolite is silicon-rich zeolite with a five-membered ring structure, containing phosphorus and rare earth and modified by one or more metal elements optionally selected from Fe, Zn, Mg and Ag. The clay contains 10 to 50 wt% of rectorite. The catalyst has the advantages of excellent hydrothermal stability, high mechanical strength and good propene selectivity, improves the carbon-carrying rate of the catalyst, and is beneficial to maintain the thermal balance of a reaction-regeneration system.
Description
Technical field
The present invention relates to a kind of catalytic converting catalyst of producing small-numerator olefin.
Background technology
The needed small-numerator olefin of chemical process as ethene, propylene etc., is mainly derived from steam cracking device at present, and remainder is from the accessory substance of oil refining process, as catalytic cracking process.In addition, can also by hydro carbons particularly alkene contact with zeolite containing catalyst the generation cracking reaction, produce small-numerator olefin.Disclosing a kind of silica alumina ratio of producing ethene and propylene by low value-added alkene as CN1414068A is the ZSM-5 type zeolite catalyst of 20-70.At least two kinds of materials that the contained zeolite utilization of catalyst is selected from IIA family metal, thulium and the phosphorus carry out modification.
CN1149185C discloses a kind of hydrocarbon feed that will contain C4-C12 alkene and has contacted with zeolite containing catalyst, produces the method for ethene and propylene.The silica alumina ratio of described zeolite is that 200-5000, aperture are 0.5-0.65nm, and this zeolite contains the metal of at least a IB of being selected from family, preferred silver, this zeolite contain every gram zeolite 0.02 mM or proton still less during by ionic liquid phase exchange/filtrate titration measuring.
CN1284109A discloses and a kind of olefin feedstock has been contacted with containing the zeolite catalyst of sial atom at least about 180, produces the method for propylene.
US6222087 disclose a kind of utilize silicon-aluminum containing than greater than 300 ZSM-5 type zeolite catalyst with C
4-C
7Alkene or alkane are converted into the method for small-numerator olefin, and zeolite utilizes phosphorus and gallium to carry out modification.
CN1037327C discloses a kind of catalyst for cracking that contains silica-rich zeolite, and this catalyst is made up of the modification silica-rich zeolite of the heavy % of 10-30 and the carrier of the heavy % of 70-90.Wherein, the modification silica-rich zeolite is to contain the heavy % phosphorus of 0.01-3.0, the heavy % iron of 0.01-1.0 or the heavy % aluminium of 0.01-10, its framework si-al ratio greater than 15 ZSM zeolite, β zeolite or modenite.Carrier is a kind of inorganic oxide or above-mentioned inorganic oxide and kaolinic mixture that comprises aluminium oxide, silica, silica-alumina, silica-magnesia, silica-zirconia.This catalyst has stronger acidity and comparatively desirable low-carbon alkene, gasoline, diesel yield.
Above-mentioned technology changes measures such as zeolite silica alumina ratio mainly by Zeolite modifying, improves the productive rate and the selectivity of propylene in the product.Because the raw material that is adopted is a lightweight material, the contained zeolite of catalyst is a silica-rich zeolite, and its sour density is low, thereby coking rate is low on the catalyst, causes above-mentioned technology to be difficult to keep the thermal balance of reaction system self in process of production.
Summary of the invention
The objective of the invention is to provide on the basis of existing technology a kind of novel catalytic converting catalyst, make the non-heavy crude hydrocarbon feed that is rich in alkene be converted into small-numerator olefins such as ethene, propylene as much as possible, alleviate catalytic convention design self heat balanced contradiction simultaneously to a certain extent.
Catalyst provided by the invention contains with the catalyst weight clay of the heavy % of 10-70 that is benchmark, the inorganic oxide of the heavy % of 5-75 and the zeolite of the heavy % of 10-65, described zeolite is the silica-rich zeolite with five-membered ring structure of any one or more than one the metal-modified phosphorous and rare earth in Fe, Zn, Mg and Ag, and the weight of rectorite accounts for the heavy % of 10-50 of clay weight in the described clay.
Compared with prior art, beneficial effect of the present invention is: catalyst provided by the invention, have good hydrothermal stability and mechanical strength, good small-numerator olefin, particularly propylene selectivity, therefore utilize production propylene and ethene that catalyst of the present invention can high selectivity.In addition, the present invention is by to the modification of zeolite and the design of catalyst formulation, small-numerator olefin productive rate and optionally simultaneously in guaranteeing product, and the carbon hanging rate of raising catalyst helps keeping reaction-regeneration system self thermal balance.
The specific embodiment
Inorganic oxide of the present invention is selected from Al
2O
3, SiO
2, SiO
2Al
2O
3Or MgOAl
2O
3In one or more mixture.
Clay of the present invention can be natural or artificial synthetic, through or without various chemistry and/or physical treatment, usually as the various clays of cracking catalyst carrier, as rectorite, kaolin, halloysite etc.The weight of rectorite accounts for the heavy % of 10-50 of clay weight, the heavy % of preferred 15-40 in the described clay.The present invention introduces the inorganic oxide that accounts for the heavy % of rectorite weight 10-20 in the rectorite expanding layer and supports, and the structure of rectorite is carried out modulation.Described inorganic oxide is selected from: a kind of in aluminium oxide, silica, the zirconia, preferred aluminium oxide.The modulating method of rectorite is as follows: with the precursor of rectorite, inorganic oxide, as aluminium colloidal sol, boehmite, mix by predetermined ratio, and it is mixed with the slurries of solid content at the heavy % of 25-50 with decationized Y sieve water, stirred at normal temperatures 3-5 hour, the gained slurries promptly can be used for catalyst preparation process.
In the five-membered ring structure high-silicon zeolite of phosphorous and rare earth of the present invention, with silica-rich zeolite weight is benchmark, the heavy % of iron content and/or magnesium and/or zinc and/or silver (in metal oxide) 0.5-5, the heavy % of preferred iron content and/or magnesium and/or zinc and/or silver-colored 0.75-4.5.
Phosphorous and five-membered ring structure high-silicon zeolite rare earth of the present invention carries out modification as follows: the silica-rich zeolite of the phosphorous and rare-earth five-membered ring structure that will make is with being selected from: the nitrate of any one or more than one the metal among Fe, Zn, Mg and the Ag or halide salt solution flood the five-membered ring structure high-silicon zeolite of phosphorous and rare earth, and the five-membered ring silica-rich zeolite behind the dipping was at 300-600 ℃ of roasting 0.5-6 hour.
Phosphorous and rare-earth five-membered ring silica-rich zeolite of the present invention be with aluminum phosphate handle obtain contain the rare-earth five-membered ring silica-rich zeolite, phosphorous in this zeolite (with P
2O
5Meter) the heavy % of 2-20, the preferably heavy % of 2-10.
The described five-membered ring silica-rich zeolite (trade names ZRP) that contains rare earth be the applicant at USP5, the zeolite disclosed in 232,675, it has the x-ray diffraction spectra of ZSM-5 zeolite family, its anhydrous chemical composition expression formula is: 0.01-0.30RE
2O
30.4-1.0Na
2OAl
2O
320-150SiO
2Rare earth in this composition used faujasite seeds that contains rare earth when synthetic.The duct of this zeolite is narrow than the ZSM-5 zeolite, it to the ratio of the adsorbance of n-hexane and cyclohexane be the ZSM-5 zeolite 2-4 doubly.This zeolite is to be raw material with waterglass, aluminum phosphate, inorganic acid, is crystal seed with REY or REHY, makes at 130-200 ℃ of following crystallization 12-60 hour.When the silica alumina ratio of zeolite at 20-150, preferably during 40-100, catalyst mesolite content is preferably in 20-50% at 10-65%, activity of such catalysts is mated preferably with selecting performance.
The method of handling the ZRP zeolite with aluminum phosphate is as follows: zeolite is exchanged processing in advance with ammonium ion, make its sodium content (with Na
2O meter) reduces to and be not more than 0.1 heavy %, will form Al
2O
3: P
2O
5=1: the aluminum phosphate colloid of 1-3 is according to P
2O
5: zeolite (butt)=1: the weight ratio of 5-99 and this zeolite mix, in the presence of 300-600 ℃, 10-100% steam roasting 0.5-6 hour.
Method for preparing catalyst provided by the invention is as follows: with the precursor of inorganic oxide, as aluminium colloidal sol, boehmite, Ludox or its mixture and silicon-aluminum sol or gel, mix by preset blending ratio with the rectorite slurries behind clay and the modulation, stir, use inorganic acid, example hydrochloric acid, nitric acid, phosphoric acid, sulfuric acid transfers to 2-4 with slurries PH, keep this pH value, the zeolite slurry that after leaving standstill 0-2 hour under 20-80 ℃, adds scheduled volume, and it is mixed with the slurries of the heavy % of solid content 15-25, homogeneous, spray-drying with decationized Y sieve water, the flush away free sodium ion, drying.
The following examples will give further instruction to method provided by the invention, but not thereby limiting the invention.
Used rectorite is that the distinguished personages of Zhongxiang City, Hubei rectorite Science and Technology Co., Ltd. produces in the example, and its composition sees Table 1, represents with percetage by weight.
Table 1
| F | Na 2O | MgO | Al 2O 3 | SiO 2 | P2O 5 | SO 3 | K 2O |
| 0.17 | 1.4 | 0.55 | 39.3 | 42.5 | 0.52 | 2.5 | 1.6 |
| CaO | TiO 2 | Cr 2O 3 | Fe 2O 3 | SrO | Y 2O 3 | ZrO 2 | |
| 4.7 | 3.5 | 0.12 | 2.9 | 0.19 | 0.065 | 0.093 |
The modulating method of used rectorite is as follows in the example: with rectorite (solid content 80%), aluminium colloidal sol (Zhou village, Shandong catalyst plant product, Al
2O
311.4%, pH:2-3), mix, and with decationized Y sieve water it to be mixed with solid content be 35% slurries that stirred at normal temperatures 3-5 hour, the gained slurries promptly can be used for follow-up Preparation of Catalyst in 85: 15 (butt) ratios.Part character before and after the rectorite modulation sees Table 2.
Table 2
| Sample | Specific surface/m 2/g | Pore volume/ml/g | |||
| S BET | S Z | S M | V micro | V pore | |
| Before the modulation | 13 | 0 | 13 | 0 | 0.03 |
| Behind the modulation | 125 | 22 | 103 | 0.01 | 0.14 |
Annotate: S
BETRepresent total specific area, S
ZRepresentative is corresponding to the specific surface of aperture less than 20 dusts,
S
MRepresentative is corresponding to the specific surface of aperture greater than 20 dusts, V
MicroRepresent the pore volume of aperture less than 20 dusts,
V
PoreRepresent total void volume.
Being prepared as follows of the five-membered ring silica-rich zeolite of used phosphorous and rare earth in the example: get 100 gram (butt) ZRP zeolite (Zhou village, Shandong catalyst plant product, SiO
2/ Al
2O
3=60, RE
2O
3=2.0%), according to zeolite (butt): ammonium sulfate: the weight ratio of decationized Y sieve water=100: 25: 2000 is 90 ℃ of following ion-exchanges 1 hour, and exchange is once again after the filtration.Atomic absorption spectrum records in this zeolite sodium content (with Na
2The O meter) be 0.04%.With 13.8 gram boehmite (Shandong Aluminum Plant's product, Al
2O
395%, solid content 30%), 9.0 gram industrial phosphoric acids (content 85%) and 200 gram decationized Y sieve water mix the back add above-mentioned ammonium exchange zeolite in, stir, 110 ℃ of dry backs promptly got phosphorus content (with P in aging 4 hours in 800 ℃, 100% water vapour atmosphere
2O
5Meter) is the five-membered ring silica-rich zeolite of 5% phosphorous and rare earth.
The five-membered ring silica-rich zeolite of the phosphorous and rare earth of used any one or multiple modification in Fe, Zn, Mg, Ag is according to the following steps modification in the example: prepared phosphorous and rare-earth five-membered ring silica-rich zeolite 100 grams are restrained Fe (NO with 50
3)
3(concentration is 4.5 heavy % to solution, Fe (NO
3)
3Purity is greater than 99%) flooded 3 hours, five-membered ring silica-rich zeolite behind the dipping was 120 ℃ of dryings 2 hours, 450 ℃ of roastings 2 hours, obtain containing the phosphorous and rare-earth five-membered ring silica-rich zeolite of Fe (in metal oxide) 1.5 heavy %, below brief note is Fe-ZRP (1).By changing the kind and the consumption thereof of metal nitrate, prepare the zeolite shown in the table 3 respectively.
Prepared phosphorous the gram with 50 with rare-earth five-membered ring silica-rich zeolite 100 restrained Fe (NO
3)
3And Mg (NO
3)
2Solution (Fe (NO
3)
3Concentration is 2.25 heavy %, Mg (NO
3)
2Concentration is 5.5 heavy %, Fe (NO
3)
3, Mg (NO
3)
2Purity greater than 99%) dipping 3 hours, five-membered ring silica-rich zeolite behind the dipping was 450 ℃ of roastings 2 hours, obtain containing Fe (in metal oxide) 0.75 heavy %, contain the phosphorous and rare-earth five-membered ring silica-rich zeolite that Mg (in metal oxide) 0.75 weighs %, below brief note is FeMg-ZRP.
Table 3
| Numbering | Modified metal | Modified metal content * |
| Fe-ZRP(1) | Fe | 1.5 |
| Fe-ZRP(2) | Fe | 0.75 |
| Fe-ZRP(3) | Fe | 4.5 |
| Ag-ZRP | Ag | 1.5 |
| Zn-ZRP | Zn | 1.5 |
| Mg-ZRP | Mg | 1.5 |
| FeMg-ZRP | Fe and Mg | 1.5 |
* in metal oxide, account for the heavy % of molecular sieve
Example 1-3
Example 1 explanation: the preparation of the catalytic converting catalyst of volume increase small-numerator olefin provided by the present invention.
At 175 kilograms of aluminium colloidal sols (Zhou village, Shandong catalyst plant product, Al
2O
311.4%, pH:2-3) add 50 kilograms of kaolin (Suzhou china clay company industrial products in, solid content 80%), 15 kilograms of rectorite slurries (solid content is 35%) stirred 90 minutes, added 117 kilograms of Fe-ZRP (1) zeolite slurry (solid content is 30%) and 143 kilograms of decationized Y sieve water again, homogeneous, spray-drying, the gained sample is washed till pH value near 6, drying, 500 ℃ of following roastings 3 hours, promptly get catalyst sample A1-5.
According to each constituent content shown in the table 4, adjust rectorite slurries and kaolinic amount ranges, and be numbered the catalyst of A1-10 and A1-20 according to method for preparing.
Example 4
This example explanation: the preparation of the catalytic converting catalyst of volume increase small-numerator olefin provided by the present invention.
At 160 kilograms of aluminium colloidal sols (Zhou village, Shandong catalyst plant product, Al
2O
311.4%, pH:2-3) add 44 kilograms of kaolin (Suzhou china clay company industrial products in, solid content 80%), 30 kilograms of rectorite slurries (solid content is 35%) stirred 90 minutes, added 117 kilograms of Fe-ZRP (2) zeolite slurry (solid content is 30%) and 149 kilograms of decationized Y sieve water again, homogeneous, spray-drying, the gained sample is washed till pH value near 6, drying, 500 ℃ of following roastings 3 hours, promptly get catalyst sample A2.
Example 5
This example explanation: the preparation of the catalytic converting catalyst of volume increase small-numerator olefin provided by the present invention.
At 160 kilograms of aluminium colloidal sols (Zhou village, Shandong catalyst plant product, Al
2O
311.4%, pH:2-3) add 44 kilograms of kaolin (Suzhou china clay company industrial products in, solid content 80%), 30 kilograms of rectorite slurries (solid content is 35%) stirred 90 minutes, added 117 kilograms of Fe-ZRP (3) zeolite slurry (solid content is 30%) and 149 kilograms of decationized Y sieve water again, homogeneous, spray-drying, the gained sample is washed till pH value near 6, drying, 500 ℃ of following roastings 3 hours, promptly get catalyst sample A3.
Example 6
This example explanation: the preparation of the catalytic converting catalyst of volume increase small-numerator olefin provided by the present invention.
At 160 kilograms of aluminium colloidal sols (Zhou village, Shandong catalyst plant product, Al
2O
311.4%, pH:2-3) add 44 kilograms of kaolin (Suzhou china clay company industrial products in, solid content 80%), 30 kilograms of rectorite slurries (solid content is 35%) stirred 90 minutes, added 117 kilograms of Ag-ZRP zeolite slurries (solid content is 30%) and 149 kilograms of decationized Y sieve water again, homogeneous, spray-drying, the gained sample is washed till pH value near 6, drying, 500 ℃ of following roastings 3 hours, promptly get catalyst sample B.
Example 7
This example explanation: the preparation of the catalytic converting catalyst of volume increase small-numerator olefin provided by the present invention.
At 160 kilograms of aluminium colloidal sols (Zhou village, Shandong catalyst plant product, Al
2O
311.4%, pH:2-3) add 44 kilograms of kaolin (Suzhou china clay company industrial products in, solid content 80%), 30 kilograms of rectorite slurries (solid content is 35%) stirred 90 minutes, added 117 kilograms of Zn-ZRP zeolite slurries (solid content is 30%) and 149 kilograms of decationized Y sieve water again, homogeneous, spray-drying, the gained sample is washed till pH value near 6, drying, 500 ℃ of following roastings 3 hours, promptly get catalyst sample C.
Example 8
This example explanation: the preparation of the catalytic converting catalyst of volume increase small-numerator olefin provided by the present invention.
At 160 kilograms of aluminium colloidal sols (Zhou village, Shandong catalyst plant product, Al
2O
311.4%, pH:2-3) add 44 kilograms of kaolin (Suzhou china clay company industrial products in, solid content 80%), 30 kilograms of rectorite slurries (solid content is 35%) stirred 90 minutes, added 117 kilograms of Mg-ZRP zeolite slurries (solid content is 30%) and 149 kilograms of decationized Y sieve water again, homogeneous, spray-drying, the gained sample is washed till pH value near 6, drying, 500 ℃ of following roastings 3 hours, promptly get catalyst sample D.
Example 9
This example explanation: the preparation of the catalytic converting catalyst of volume increase small-numerator olefin provided by the present invention.
At 160 kilograms of aluminium colloidal sols (Zhou village, Shandong catalyst plant product, Al
2O
311.4%, pH:2-3) add 44 kilograms of kaolin (Suzhou china clay company industrial products in, solid content 80%), 30 kilograms of rectorite slurries (solid content is 35%) stirred 90 minutes, added 117 kilograms of FeMg-ZRP zeolite slurries (solid content is 30%) and 149 kilograms of decationized Y sieve water again, homogeneous, spray-drying, the gained sample is washed till pH value near 6, drying, 500 ℃ of following roastings 3 hours, promptly get catalyst sample E.
Comparative Examples 1
At 175 kilograms of aluminium colloidal sols (Zhou village, Shandong catalyst plant product, Al
2O
311.4%, pH:2-3) the middle 56 kilograms of kaolin (Suzhou china clay company industrial products, solid content 80%) that add stirred 90 minutes, added 117 kilograms of ZRP zeolites (Zhou village, Shandong catalyst plant product, SiO again
2/ Al
2O
3=60, RE
2O
3=2.0%) slurries (solid content is 30%) and 152 kilograms of decationized Y sieve water, homogeneous, spray-drying promptly gets contrast medium 1.
Embodiment 10-18
Embodiment 10-18 explanation: the catalytic perfomance of catalyst of the present invention.
Adopt the small fixed flowing bed device that above-mentioned catalyst sample A1-5, A1-10, A1-20, A2, A3, B, C, D, E are carried out test evaluation respectively.Before the test, above-mentioned catalyst sample is aging 14h in 790 ℃, 100% steam respectively.The key reaction condition is as follows: 620 ℃ of reaction temperatures, oil ratio 15, weight space velocity 6 hours-1, water injection rate 20%.Catalyst system therefor sees Table 4, and the composition of raw material sees Table 5.Result of the test is listed in table 6.Test procedure is as follows: raw material shown in the table 5 injects the small fixed flowing bed reactor, in the presence of steam, contacts with the catalyst sample of heat and reacts; Reaction product isolated obtains various products.Coke burning regeneration behind the reclaimable catalyst stripping, the catalyst circulation after the regeneration is used.Result of the test is listed in table 6-8 respectively.
By the result of the test among the table 6-8 as can be seen, catalyst of the present invention not only has comparatively desirable small-numerator olefin selectivity, and its coke yield increases to some extent than contrast medium.This characteristics help alleviating the unbalanced problem of cat-cracker self heat, and the heat of 10-50% can be provided for reactive moieties more.In addition, the result of the test among the table 6-8 shows that also compare with other several modified metals, iron has better modified effect, and the catalyst that contains the iron modified zeolite has higher small-numerator olefin productive rate and better choice.
Table 4
| The catalyst code name | The ZRP molecular sieve | Modified metal | Clay | Rectorite | Inorganic oxide |
| A1-5 | 35 | Fe | 40 | 5 | 20 |
| A1-10 | 35 | Fe | 35 | 10 | 20 |
| A1-20 | 35 | Fe | 25 | 20 | 20 |
| A2 | 35 | Fe | 35 | 10 | 20 |
| A3 | 35 | Fe | 35 | 10 | 20 |
| B | 35 | Ag | 35 | 10 | 20 |
| C | 35 | Zn | 35 | 10 | 20 |
| D | 35 | Mg | 35 | 10 | 20 |
| E | 35 | Fe and Mg | 35 | 10 | 20 |
| Contrast medium 1 | 35 | / | 45 | 0 | 20 |
Table 5
| Title | Form heavy % |
| The steam cracking carbon-4 | |
| Butane | 3.67 |
| Butylene | 96.33 |
Table 6
| Example | 10 | 11 | 12 | Comparative Examples |
| Feedstock oil | The swallowization steam cracking is taken out surplus C 4 | |||
| Catalyst | A1-5 | A1-10 | A1-20 | Contrast medium 1 |
| Material balance, heavy % | ||||
| Cracking gas | 82.75 | 83.94 | 84.07 | 83.21 |
| Fluid product+loss | 15.08 | 13.65 | 13.27 | 15.41 |
| Coke | 2.17 | 2.41 | 2.67 | 1.38 |
| The major product one-pass yield, heavy % | ||||
| Propylene | 28.24 | 27.58 | 28.19 | 27.67 |
| Ethene | 6.76 | 5.82 | 6.58 | 6.94 |
| Propylene, m/m | 12 | 11 | 12 | 11 |
| The major product selectivity | ||||
| Propylene | 45.5 | 46.9 | 46.5 | 46.2 |
| Ethene | 10.9 | 9.9 | 10.9 | 11.6 |
| Propylene+ethene | 56.4 | 56.8 | 57.4 | 57.8 |
Table 7
| Embodiment | 13 | 14 | 15 | Comparative Examples |
| Feedstock oil | The swallowization steam cracking is taken out surplus C 4 | |||
| Catalyst | A2 | A3 | B | Contrast medium |
| Material balance, heavy % | ||||
| Cracking gas | 82.39 | 84.56 | 84.74 | 83.21 |
| Fluid product+loss | 15.4 | 12.82 | 10.64 | 15.41 |
| Coke | 2.21 | 2.62 | 4.62 | 1.38 |
| The major product one-pass yield, heavy % | ||||
| Propylene | 23.5 | 26.4 | 20.8 | 27.67 |
| Ethene | 4.90 | 7.52 | 7.38 | 6.94 |
| Propylene, m/m | 11 | 10 | 8 | 11 |
| The major product selectivity | ||||
| Propylene | 42.6 | 43.5 | 41.6 | 46.2 |
| Ethene | 8.9 | 12.4 | 14.8 | 11.6 |
| Propylene+ethene | 51.5 | 55.9 | 56.4 | 57.8 |
Table 8
| Embodiment | 16 | 17 | 18 | Comparative Examples |
| Feedstock oil | The swallowization steam cracking is taken out surplus C 4 | |||
| Catalyst | C | D | E | Contrast medium |
| Material balance, heavy % | ||||
| Cracking gas | 83.83 | 83.54 | 84.67 | 83.21 |
| Fluid product+loss | 13.08 | 13.85 | 12.83 | 15.41 |
| Coke | 3.09 | 2.61 | 2.50 | 1.38 |
| The major product one-pass yield, heavy % | ||||
| Propylene | 22.1 | 22.9 | 23.1 | 27.67 |
| Ethene | 6.06 | 5.48 | 5.40 | 6.94 |
| Propylene, m/m | 12 | 13 | 13 | 11 |
| The major product selectivity | ||||
| Propylene | 41.6 | 44.3 | 45.8 | 46.2 |
| Ethene | 11.4 | 10.6 | 10.7 | 11.6 |
| Propylene+ethene | 55.7 | 56.4 | 56.4 | 57.8 |
Claims (14)
1, a kind of catalytic converting catalyst of producing small-numerator olefin, this catalyst contains with the catalyst weight clay of the heavy % of 10-70 that is benchmark, the inorganic oxide of the heavy % of 5-75 and the zeolite of the heavy % of 10-65, it is characterized in that the silica-rich zeolite with five-membered ring structure of described zeolite, and contain the rectorite of the heavy % of 10-50 in the described clay for any one or more than one the metal-modified phosphorous and rare earth in Fe, Zn, Mg and Ag.
2,, it is characterized in that containing in the described clay rectorite of the heavy % of 15-40 according to the catalyst of claim 1.
3, according to the catalyst of claim 1 or 2, it is characterized in that described rectorite is the rectorite through the structure modulation, that is, introduce the inorganic oxide that accounts for the heavy % of rectorite weight 10-20 in the expanding layer of rectorite expanding layer is supported.
4, according to the catalyst of claim 3, the modulating method that it is characterized in that described rectorite is as follows: the precursor of rectorite, inorganic oxide is mixed by predetermined ratio, and it is mixed with the slurries of solid content at the heavy % of 25-50 with decationized Y sieve water, stirred at normal temperatures 3-5 hour.
5, according to the catalyst of claim 1, it is characterized in that the silica-rich zeolite with five-membered ring structure of described phosphorous and rare earth, be benchmark with silica-rich zeolite weight, in metal oxide, the heavy % of iron content and/or magnesium and/or zinc and/or silver-colored 0.5-5.
6, according to the catalyst of claim 5, it is characterized in that the silica-rich zeolite with five-membered ring structure of described phosphorous and rare earth, be benchmark with silica-rich zeolite weight, in metal oxide, the heavy % of iron content and/or magnesium and/or zinc and/or silver-colored 0.75-4.5.
7, according to the catalyst of claim 5 or 6, the silica-rich zeolite with five-membered ring structure that it is characterized in that described phosphorous and rare earth any one in Fe, Zn, Mg and Ag is metal-modified.
8, according to the catalyst of claim 7, the silica-rich zeolite with five-membered ring structure that it is characterized in that described phosphorous and rare earth is through the Fe modification.
9, according to claim 1,5,6, one of 7 or 8 catalyst, it is characterized in that described phosphorous and five-membered ring structure high-silicon zeolite rare earth carries out modification as follows: adopt the nitrate of selected metal or the halide salt solution dipping is phosphorous and the silica-rich zeolite with five-membered ring structure of rare earth, the five-membered ring silica-rich zeolite behind the dipping was at 300-600 ℃ of roasting 0.5-6 hour.
10, according to the catalyst of claim 1, it is characterized in that described phosphorous and rare-earth five-membered ring silica-rich zeolite be with aluminum phosphate handle obtain contain the rare-earth five-membered ring silica-rich zeolite, with P
2O
5Meter, the heavy % of phosphorous 2-20 in this zeolite.
11, according to the catalyst of claim 10, it is characterized in that described phosphorous and rare-earth five-membered ring silica-rich zeolite be with aluminum phosphate handle obtain contain the rare-earth five-membered ring silica-rich zeolite, with P
2O
5Meter, the heavy % of phosphorous 2-10 in this zeolite.
12, according to the catalyst of claim 10 or 11, it is characterized in that the described x-ray diffraction spectra that the rare-earth five-membered ring silica-rich zeolite has ZSM-5 zeolite family that contains, its anhydrous chemical composition expression formula is: 0.01-0.30RE
2O
30.4-1.0Na
2OAl
2O
320-150SiO
2
13,, it is characterized in that described to handle the method contain the rare-earth five-membered ring silica-rich zeolite with aluminum phosphate as follows: zeolite is exchanged processing in advance with ammonium ion, make it with Na according to the catalyst of claim 10 or 11
2The sodium content of O meter is reduced to and is not more than 0.1 heavy %, will form Al
2O
3: P
2O
5=1: the aluminum phosphate colloid of 1-3 is according to P
2O
5: the weight ratio of zeolite=1: 5-99 and this zeolite mix, in the presence of 300-600 ℃, 10-100% steam roasting 0.5-6 hour.
14, according to the catalyst of claim 1, it is characterized in that this method for preparing catalyst is as follows: the rectorite slurries behind the precursor of inorganic oxide and clay and the modulation are mixed by preset blending ratio, stir, slurries PH is transferred to 2-4, keep this pH value with inorganic acid, the zeolite slurry that after leaving standstill 0-2 hour under 20-80 ℃, adds scheduled volume, and it is mixed with the slurries of the heavy % of solid content 15-25, homogeneous, spray-drying with decationized Y sieve water, the flush away free sodium ion, drying.
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| KR102079063B1 (en) * | 2018-06-20 | 2020-04-13 | 한국화학연구원 | Catalyst for manufacturing light olefin, method for manufacturing the same, and method for manufacturing light olifin using the same |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US6222087B1 (en) * | 1999-07-12 | 2001-04-24 | Mobil Oil Corporation | Catalytic production of light olefins rich in propylene |
| CN1354223A (en) * | 2000-11-17 | 2002-06-19 | 中国石油化工股份有限公司 | Catalytic cracking catalyst for producing gasoline richly-containing paraffinic hydrocarbon |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US6222087B1 (en) * | 1999-07-12 | 2001-04-24 | Mobil Oil Corporation | Catalytic production of light olefins rich in propylene |
| CN1354223A (en) * | 2000-11-17 | 2002-06-19 | 中国石油化工股份有限公司 | Catalytic cracking catalyst for producing gasoline richly-containing paraffinic hydrocarbon |
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