CN107754846B - The reformate olefin-reducing catalyst for aromatic hydrocarbons of long-term operation - Google Patents
The reformate olefin-reducing catalyst for aromatic hydrocarbons of long-term operation Download PDFInfo
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- CN107754846B CN107754846B CN201610710680.5A CN201610710680A CN107754846B CN 107754846 B CN107754846 B CN 107754846B CN 201610710680 A CN201610710680 A CN 201610710680A CN 107754846 B CN107754846 B CN 107754846B
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- B—PERFORMING OPERATIONS; TRANSPORTING
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- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J29/00—Catalysts comprising molecular sieves
- B01J29/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites
- B01J29/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
- B01J29/08—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the faujasite type, e.g. type X or Y
- B01J29/085—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the faujasite type, e.g. type X or Y containing rare earth elements, titanium, zirconium, hafnium, zinc, cadmium, mercury, gallium, indium, thallium, tin or lead
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- B—PERFORMING OPERATIONS; TRANSPORTING
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- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J29/00—Catalysts comprising molecular sieves
- B01J29/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites
- B01J29/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
- B01J29/08—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the faujasite type, e.g. type X or Y
- B01J29/16—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the faujasite type, e.g. type X or Y containing arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
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- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G29/00—Refining of hydrocarbon oils, in the absence of hydrogen, with other chemicals
- C10G29/16—Metal oxides
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/10—Feedstock materials
- C10G2300/1037—Hydrocarbon fractions
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Abstract
The present invention relates to a kind of reformate olefin-reducing catalyst for aromatic hydrocarbons of long-term operation, mainly solve to cause catalyst inactivation very fast because activated centre matches bad with Reaction-diffusion terms existing for current techniques, the short problem of service life.The olefin-reducing catalyst for aromatic hydrocarbons of long-term operation of the invention, in terms of catalyst weight percent, including following component: or mixtures thereof 0.01~15% lanthanide series；0.01~8% oxide selected from one or more of Na, K, Mg, Ca, Sr, Ba element；0.01~10% is one or more of selected from Ga, Sn, In, Ge, Bi element；The technical solution of 40~90% Y type molecular sieve, preferably solves the problems, such as this, active good, and the advantage of service life length can be used in the industrial production of aromatic hydrocarbons Olefin decrease.
Description
Technical field
The invention belongs to a kind of reformate olefin-reducing catalyst for aromatic hydrocarbons.
Background of invention
The present invention relates to a kind of reformate olefin-reducing catalyst for aromatic hydrocarbons, the catalyst service life is specifically improved.
Aromatic hydrocarbons is the base stock of petrochemical industry, it mostlys come from Aromatic Hydrocarbon United Plant.After catalytic reforming reaction
Reformate aromatic hydrocarbon product contain a certain amount of olefin impurity.Alkene chemistry property is active, is not only easy polymerization and forms colloid,
But also easily react with other components, undesirable components are generated, so that the quality and device operation to aromatic hydrocarbon product generate
Larger impact.
The aromatic hydrocarbons subsequent production technique such as dimethylbenzene adsorption separation process that reformate or other drippolenes generate is to alkene
It is especially sensitive, even if the content of olefin impurity is a small amount of, can also very detrimental effect be generated to technical process.It is qualified in order to obtain
Subsequent production needed for industrial chemicals and guarantee the stable operation of subsequent technique, have removing trace amounts of olefin impurity unit.
Since refining step all in most Aromatic Hydrocarbon United Plants is all made of carclazyte as refining agent, as low pressure is reformed
Popularization, gum level increases in reformate, and the puzzlement of carclazyte bring will be more serious, substitutes the efficient deolefination of industrial carclazyte
Catalyst and application technology have become trend.
Clay-filtered is to contact aroamtic hydrocarbon raw material with atlapulgite, reaches de- using the suction-operated and catalytic action of carclazyte
Except the purpose of olefin impurity.Carclazyte has acid centre, under the conditions of high pressure liquid phase, 150~200 DEG C, has certain catalysis
Overlapping ability and duct adsorption capacity can make the trace amounts of olefin contained in reformate that the reaction such as hydrocarbonylation, polymerization occur, generate high boiling
Point compound, then by bleaching earth adsorption, or removes in later separation process.Typical catalyst CN102091648A,
It is described in the patents such as CN1232862, CN102658196A, and is cited in full text herein.Although carclazyte has removing alkene
Ability, but since its specific surface area is smaller, pore structure is undeveloped, therefore inactivate very fast, the service life is shorter, and due to inactivation after
Carclazyte high temperature regeneration pore structure is obviously reduced, and causes the decline of deolefination ability larger, and regenerability is poor, causes carclazyte frequently more
It changes, and the carclazyte after inactivation can only cause environmental pollution by buried processing.
Alkene is removed under the conditions of separately having deolefination technique to use noble metal hydrogenation.Hydrofinishing route there are hydrogen recycle and
The separation problem of hydrogen and oil product needs to add the equipment such as compressor, gas-liquid separator and stripper, and the process is more complicated, energy
Consumption is high, and used catalyst is mostly noble metal catalyst, expensive.
Hydrofinishing is carried out to aroamtic hydrocarbon raw material " rear to add using noble metal platinum or palladium catalyst after petroleum reforming technique
Hydrogen process ", make alkene be saturated and remove olefin impurity, typical catalyst CN85100760A, CN85100215A,
In the patents such as CN1448474A, CN101260320A.But the wide component of aromatic hydrocarbons simultaneously containing benzene, toluene and dimethylbenzene is come
Say, hydrogenation reaction depth is difficult to take into account comprehensively, when special C9 aromatic or more plus form the aromatic hydrocarbons such as low boiling point toluene after hydrogen,
Keep the loss of aromatic hydrocarbon product larger.
Molecular sieve is the artificial synthesized alumionsilicate crystalline body with spacious multidimensional structure.Compared with carclazyte, molecular sieve
Specific surface area is high, has higher appearance charcoal ability, lasts a long time；The acidity of molecular sieve is produced by the unsaturated coordination of skeletal atom
Raw, therefore acidity is basically unchanged after high temperature regeneration, reproducibility is preferable, thus molecular sieve catalyst have preferable stability and compared with
The long service life.In view of the above-mentioned advantage of molecular sieve catalyst, it has been disclosed that many research achievements and using molecular sieve as main component
The olefinic hydrocarbon expelling catalyzer of preparation.EP0895977A1 is disclosed using 80% molecular sieve as based on active component and 20% aluminium oxide,
Extrusion is mediated by binder of acid Alusil, the particle that 20-40 mesh is ground into after drying and roasting is finished catalyst.WO 01/
Being described in 30942A1 using mesoporous molecular sieve MCM-22 is that active component and clay carrier molding prepare catalyst removal alkene
The extrusion rate of hydrocarbon, alkene is higher than 95%.CN1618932A, CN 103495435A are described under conditions of non-hydrogen, using molecular sieve
For active component, the method that aluminium oxide or kaolin prepare catalyst for carrier, catalyst has renewable recycling.
It is main active component that one kind is described in CN102008976A by high silica alumina ratio ReUSY molecular sieve, with mordenite molecular sieve
For the second active component, aluminium oxide is binder component, and inorganic acid is added or organic acid carries out kneading extrusion, drying roasting obtains
Catalyst.But in the above-mentioned patent of invention having disclosed, the acidity of catalyst is mainly supplied by molecular sieve, this is for weight
It is whole oil in trace amounts of olefin by alkylated reaction remove for be it is weaker, higher reaction temperature ability is needed in use process
Achieve the purpose that completely remove alkene, do not only result in energy consumption increase, also results in coking carbon distribution, the reaction of aromatic hydrocarbons dealkylation, aromatic hydrocarbons
The generation of the side reactions such as cracking, leads to the loss of aromatic hydrocarbons.
Chinese patent CN1618932 describes one kind catalytic refining reforming aromatic oil catalyst under conditions of non-hydrogen.It should
Catalyst is non-loading type solid acid catalyst, using the catalyst treatment reforming aromatic oil, at 100~300 DEG C of reaction temperature,
0.5~3.0MPa of reaction pressure, when air speed 0.5~40-1Under the conditions of, the trace amounts of olefin in energy Arene removal, however although this is urged
Agent can regenerate reuse, but its single pass life is still too short, when air speed is 15-1Under the conditions of check and rate 18 hours after,
Its activity is just reduced to 50%, thus industrial application is very limited.
The purpose of the invention is to overcome the problems, such as that the previous catalyst for removing olefins from reforming oil service life is low, since molecular sieve is general
All over using it is transition metal modified it is acid adjust, a kind of service life that the modification of element is difficult to reach catalyst extends, and multiple element is difficult
To form more effective modified effect, therefore the problem of the service life can not form better effects.
Summary of the invention
The present invention relates to reformate aromatic hydrocarbons olefinic hydrocarbon expelling catalyzer, mainly solve the previous catalyst for removing olefins from reforming oil service life compared with
Low problem.Through effective ways when molecular sieve is modified, major element is by molecular sieve modified after addition, preferably
It solves the problems, such as, catalyst has the advantages that the service life long.
The present invention uses a kind of reformate olefin-reducing catalyst for aromatic hydrocarbons of long-term operation, with catalyst weight percent
Meter, including following component:
A) mixture of one or more of 0.01~15% lanthanide series；
B) 0.01~8% oxide selected from one or more of Na, K, Mg, Ca, Sr, Ba element；
C) 0.01~10% is one or more of selected from Ga, Sn, In, Ge, Bi element；
D) 40~90% Y type molecular sieve；
E) one or more selected from aluminium oxide, silica.
For in above-mentioned offer technical solution:
Y molecular sieve is to adjust cellular structure and acidity with larger range, as chain carrier supplier and carrier,
It is 40~90% that its content, which accounts for catalyst, and accounting for by weight percentage for optimization contains 50~85% Y type molecular sieve.Generally
Industrial production is NaY, can obtain HY or USY molecular sieve by ion exchange or subsequent processing.Therefore catalyst molecule
Sieve is the one or more of NaY, HY, USY.Various molecular sieves are obtained by hydro-thermal process, the modification of soda acid processing method
In above-mentioned technical proposal, the mixture containing one or more of 0.01~15% lanthanide series, optimization contains 0.3
Or mixtures thereof~10% lanthanide series.
In above-mentioned technical proposal, one or more of selected from Ga, Sn, In, Ge, Bi element containing 0.5~5%, optimization contains
0.5~3% oxide selected from the rear major element of one or more of Na, K, Mg, Ca, Sr, Ba.The element is forming
Before, in molding, after molding simultaneously or it is different when in introduce.
In above-mentioned technical proposal, salic in catalyst and silica.
The molecular sieve catalyst held containing certain metering-orifice is obtained after molecular sieve and silica or alumina binder shaping and roasting.
Silica or account for 10~60% or so of weight with aluminium oxide in the catalyst.Preferable range silica or and aluminium oxide
Account for overall catalyst weight 12~40%.
Catalyst is prepared according to the technical program, the described reformate Olefin decrease reaction condition that is used for is in temperature 130~260
DEG C, 0.3~5.0MPa of pressure, 0.1~10h of weight space velocity-1。
In aromatic hydrocarbons catalyst for removing olefins from reforming oil, catalyst is modified and adjusted using rear major element, generally
It is adjusted using transition elements and alkaline element, to obtain preferable catalyst, but due to the above transition elements and alkalinity
Element, which be combined with each other, to be not easy, cause catalyst active center with to react matching inadequate.The present invention passes through rear major element, Ke Yiyu
Lanthanide series and alkaline element interaction, reach preferable activity, catalyst active center are made to have preferable reactivity worth
And uniformity, so that the generation of side reaction is reduced, to extend the service life of catalyst.The catalyst of invention preparation passes through coordination
It is modified and reacts matched method, solve the problems, such as that the service life of previous catalyst is shorter.
By using following example, the invention will be further elaborated:
Specific embodiment
[embodiment 1]
Containing 3.0wt%LaO, 1.0wt%Na2USY (the SiO of O2/Al2O37.0) and the aluminium oxide of 25.0wt% than
Catalyst 60.0g, using SnSO4Solution (containing Sn3.0wt%), 38g incipient impregnation used after dry 550 DEG C of roastings 3 hours
Mg(NO3)2Solution (1.0wt% containing Mg) 35g incipient impregnation, dry 520 DEG C of roastings obtain catalyst A in 3.0 hours.
3.0g catalyst is taken to carry out the test of reformate non-hydrogen deolefination in fixed bed reactors, raw material is to reform
Oil, bromine index are 1200 milligrams of Br/100 grams of oil (reaction raw materials evaluation that following all examples uses).Activity calculates public
Formula is as follows:
Reaction pressure: 2.0MPa, temperature: 160 DEG C, air speed: when 10.0-1, Activity Results 2 hours 95%, 100 hours
90.5%, 200 hours 82.0%.
[embodiment 2]
Containing 2.0wt%LaO and 2.0wt%CeO2, 0.5wt%Na2USY (the SiO of O2/Al2O3Than 12.0), and
The catalyst 60.0g of the aluminium oxide of 25.0wt%, using Ga (NO3)3Solution (1.5wt% containing Ga) 40g incipient impregnation, it is dry
After 500 DEG C roast 4 hours, using Ca (NO3)2Solution (0.5wt% containing Ca) 36g incipient impregnation, dry 550 DEG C of roastings 2.5
Hour obtains catalyst B.
3.0g catalyst is taken to carry out the test of reformate non-hydrogen deolefination in fixed bed reactors, reaction pressure:
5.0MPa, temperature: 180 DEG C, air speed: when 8.0-1, Activity Results 2 hours 95.0%, 100 hours 88.0%, 200 hours
80.1%.
[embodiment 3]
Containing 2.0wt%LaO and 2.0wt%CeO2, 0.5wt%Na2USY (the SiO of O2/Al2O3Than 12.0), and
The catalyst 60.0g of the aluminium oxide of 10.0wt%, using Ga (NO3)3Solution (1.5wt% containing Ga) 40g incipient impregnation, it is dry
After 500 DEG C roast 4 hours, using Ca (NO3)2Solution (0.5wt% containing Ca) 36g incipient impregnation, dry 600 DEG C of roastings 2.0
Hour obtains catalyst C.
3.0g catalyst is taken to carry out the test of reformate non-hydrogen deolefination in fixed bed reactors, reaction pressure:
3.0MPa, temperature: 170 DEG C, air speed: when 5.0-1, Activity Results 2 hours 96.0%, 100 hours 92.0.0%, 200 hours
89.0%.
[embodiment 4]
Containing 0.01wt%LaO, 0.3wt%Na2USY (the SiO of O2/Al2O312.0) and the aluminium oxide of 35.0wt% than
Catalyst 60.0g, using Ga (NO3)3Solution (1.5wt% containing Ga) 40g incipient impregnation, dry 500 DEG C roast 4 hours
Afterwards, using Ca (NO3)2Solution (0.5wt% containing Ca) 36g incipient impregnation, dry 550 DEG C of roastings obtain catalyst in 3.0 hours.
3.0g catalyst is taken to carry out the test of reformate non-hydrogen deolefination in fixed bed reactors, reaction pressure:
3.0MPa, temperature: 260 DEG C, air speed: when 8.0-1, as a result 2 hours 96.0%, 100 hours 95.0%, 200 hours 91.0%.
[embodiment 5]
Containing 0.01wt%LaO, 0.01wt%Na2USY (the SiO of O2/Al2O312.0) and the aluminium oxide of 25.0wt% than
Catalyst 60.0g, using Bi (NO3)3Solution (5.0wt% containing Bi) 40g incipient impregnation, dry 500 DEG C roast 4 hours
Afterwards, using Sr (NO3)2Solution (0.01wt% containing Sr) 36g incipient impregnation, dry 600 DEG C of roastings are catalyzed for 1.5 hours
Agent.
3.0g catalyst is taken to carry out the test of reformate non-hydrogen deolefination in fixed bed reactors, reaction pressure:
1.0MPa, temperature: 130 DEG C, air speed: when 5.0-1, as a result 2 hours 96.0%, 100 hours 91.0%, 200 hours 86.5%.
[embodiment 6]
Containing 1.6wt%Na2USY (the SiO of O2/Al2O3Than 5.0), the aluminium oxide of 0.9wt%GeO and 25.0wt% are urged
Agent 60.0g is handled 3 hours using at 500g90 DEG C of 1M acetic acid solution, after dry 500 DEG C of roastings 4 hours, using (the NO containing K3)2
Solution (0.3wt% containing K) and (NO containing Sn3)2Solution (2.0wt% containing Sn) 200g dipping filters 500 DEG C of roastings and obtains for 3 hours
Catalyst.
3.0g catalyst is taken to carry out the test of reformate non-hydrogen deolefination in fixed bed reactors, reaction pressure:
0.3MPa, temperature: 130 DEG C, air speed: when 3.0-1, Activity Results 2 hours 98.0%, 100 hours 97.0%, 200 hours
92.8%.
[embodiment 7]
Containing 0.2wt%Na2USY (the SiO of O2/Al2O3Than 18.0), the aluminium oxide of 15.0wt%LaO and 45.0wt%
Catalyst 60.0g, using being handled 3 hours at 90 DEG C of 0.3M sulfuric acid solution 500g, it is dry after 600 DEG C after roasting 4 hours, use
Sn(NO3)2Solution (8.0wt% containing Sn) 200g dipping filters 700 DEG C of roastings and obtains catalyst in 1 hour.
3.0g catalyst is taken to carry out the test of reformate non-hydrogen deolefination in fixed bed reactors, reaction pressure:
2.0MPa, temperature: 170 DEG C, air speed: when 2.0-1, as a result 2 hours 95.0%, 100 hours 94.5%, 200 hours 93.8%.
[embodiment 8]
Containing 0.5wt%Na2HY (the SiO of O2/Al2O3Than 4.5), the silica of 8.0wt%BaO and 20.0wt%
Catalyst 60.0g, using being handled 2 hours at 90 DEG C of 0.2M citric acid solution 300g, it is dry after 450 DEG C after roasting 4 hours, adopt
With Sb (NO3)2Solution (2.0wt% containing Sb) 150g dipping filters 550 DEG C of roastings and obtains catalyst in 2 hours.
3.0g catalyst is taken to carry out the test of reformate non-hydrogen deolefination in fixed bed reactors, reaction pressure:
3.0MPa, temperature: 170 DEG C, air speed: when 1.0-1, as a result 2 hours 93.0%, 200 hours 91.8%.
[embodiment 9]
Containing 1.2wt%Na2NaHY (the SiO of O2/Al2O3Than 5.0), the silica of 10wt%GaO and 15.0wt% and
The catalyst 60.0g of 5% aluminium oxide, after normal pressure lower 600 DEG C of water vapours (moisture vapor 0.08MPa) processing processing 2 hours,
Using (the NO containing Sn3)2Solution (2.0wt% containing Sn) and (NO containing Bi3)3Solution (6.0wt% containing Bi) 150g dipping, filtering 550
DEG C roasting obtains catalyst in 2 hours.
3.0g catalyst is taken to carry out the test of reformate non-hydrogen deolefination in fixed bed reactors, reaction pressure:
2.0MPa, temperature: 170 DEG C, air speed: when 2.0-1, Activity Results 2 hours 96.8.0%, 100 hours 95.8%, 200 hours
95.0%.
[embodiment 10]
Containing 0.3wt%Na2USY (the SiO of O2/Al2O3Than 11.0), the catalyst of 1.0wt%CaO and 15% aluminium oxide
60.0g, after normal pressure lower 700 DEG C of water vapours (moisture vapor 0.05MPa) processing processing 1 hour, using Sn (NO3)2Solution
(3.2wt% containing Sn) 190g dipping filters 550 DEG C of roastings and obtains catalyst in 2 hours.
3.0g catalyst is taken to carry out the test of reformate non-hydrogen deolefination in fixed bed reactors, reaction pressure:
3.0MPa, temperature: 170 DEG C, air speed: when 0.1-1, as a result 2 hours 98.50%, 200 hours 98.4%.
3.0g catalyst is taken to carry out the test of reformate non-hydrogen deolefination in fixed bed reactors, reaction pressure:
5.0MPa, temperature: 260 DEG C, air speed: when 6.0-1, as a result 2 hours 98.00%, 200 hours 94.4%.
[embodiment 11]
Containing 0.8wt%Na2USY (the SiO of O2/Al2O3Than 10.0), the catalyst of 1.9wt%CeO and 15% aluminium oxide
60.0g, using Sn (NO3)2Solution (3.2wt% containing Sn) 190g dipping filters 550 DEG C of roastings and obtains catalyst in 2 hours.
3.0g catalyst is taken to carry out the test of reformate non-hydrogen deolefination in fixed bed reactors, reaction pressure:
3.0MPa, temperature: 170 DEG C, air speed: 2.0-1, as a result 2 hours 96.50%, 200 hours 95.4%.
Claims (10)
1. a kind of reformate olefin-reducing catalyst for aromatic hydrocarbons of long-term operation, in terms of catalyst weight percent, including it is following several
A component:
A) mixture of one or more of 0.01~15% lanthanide series；
B) 0.01~8% oxide selected from one or more of Na, K, Sr, Ba element；
C) 0.01~10% is one or more of selected from Ga, Sn, In, Ge, Bi, Sb element；
D) 40~90% Y type molecular sieve；
E) 10~60% one or more selected from aluminium oxide, silica.
2. the reformate olefin-reducing catalyst for aromatic hydrocarbons of long-term operation according to claim 1, it is characterised in that with weight hundred
Divide than meter, the mixture containing one or more of 0.3~10% lanthanide series.
3. the reformate olefin-reducing catalyst for aromatic hydrocarbons of long-term operation according to claim 1, it is characterised in that with weight hundred
Divide the oxide than meter, containing 0.5~3% selected from one or more of Na, K, Sr, Ba element.
4. the reformate olefin-reducing catalyst for aromatic hydrocarbons of long-term operation according to claim 1, it is characterised in that with weight hundred
Divide than meter, selects Ga, Sn, In, Ge, Bi element one or more of containing 0.5~5%.
5. the reformate olefin-reducing catalyst for aromatic hydrocarbons agent of long-term operation according to claim 1, it is characterised in that with weight
Percentages contain 50~85% Y type molecular sieve.
6. the reformate olefin-reducing catalyst for aromatic hydrocarbons of long-term operation according to claim 1, it is characterised in that described Y type point
Son sieve is the one or more of NaY, HY, USY.
7. the reformate olefin-reducing catalyst for aromatic hydrocarbons of long-term operation according to claim 1, it is characterised in that Y molecular sieve is logical
It is modified to cross hydro-thermal process, ion exchange, soda acid processing method.
8. the reformate olefin-reducing catalyst for aromatic hydrocarbons of long-term operation according to claim 1, it is characterised in that the group
Element in point a), b) and c) before the forming, in molding, after molding simultaneously or it is different when in introduce.
9. the reformate olefin-reducing catalyst for aromatic hydrocarbons of long-term operation according to claim 1, it is characterised in that in catalyst
Salic and silica.
10. a kind of method of the reformate aromatic hydrocarbons Olefin decrease of long-term operation is catalyzed using any one in claim 1~9
Agent, it is characterised in that it is described for reformate Olefin decrease at 130~260 DEG C of temperature, 0.3~5.0MPa of pressure, weight space velocity 0.1
~10h-1。
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| CN104549472A (en) * | 2013-10-28 | 2015-04-29 | 中国石油化工股份有限公司 | Aromatic alkyl transferring and deolefination catalyst and application thereof |
| CN105080592A (en) * | 2014-05-14 | 2015-11-25 | 中国石油化工股份有限公司 | Aromatic olefin-reducing catalyst and use thereof |
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|---|---|---|---|---|
| CN104549472A (en) * | 2013-10-28 | 2015-04-29 | 中国石油化工股份有限公司 | Aromatic alkyl transferring and deolefination catalyst and application thereof |
| CN105080592A (en) * | 2014-05-14 | 2015-11-25 | 中国石油化工股份有限公司 | Aromatic olefin-reducing catalyst and use thereof |
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| CN107754846A (en) | 2018-03-06 |
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