CN102921428B - Sulfur-containing coking liquefied gas high-temperature hydrogenation catalyst and its preparation method and use - Google Patents
Sulfur-containing coking liquefied gas high-temperature hydrogenation catalyst and its preparation method and use Download PDFInfo
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Abstract
The invention relates to a sulfur-containing coking liquefied gas high-temperature hydrogenation catalyst and its preparation method and use. The sulfur-containing coking liquefied gas high-temperature hydrogenation catalyst utilizes gamma-alumina as a carrier, comprises active components of 10.0 to 20.0% of Mo2O3 and 6.0 to 18.0% of NiO, is in a shape of a strip, a whitetip clover or a ball having the size of dia. 3*(3-5)mm and has a specific surface area of 100 to 200m<2>/g. The preparation method comprises the following steps of molybdenum loading, nickel loading, drying and calcination. The sulfur-containing coking liquefied gas high-temperature hydrogenation catalyst can be used for high-temperature hydrogenation saturation of coking liquefied gas and coking residual C4, avoids catalyst pre-vulcanization, can be directly used for high-temperature hydrogenation of coking liquefied gas and coking residual C4 after hydrogen atmosphere reduction, and avoids pre-treatment on coking liquefied gas and coking residual C4. A hydrogenation reaction feeding temperature is in a range of 180 to 230 DEG C; a reaction temperature is in a range of 280 to 300 DEG C; reaction pressure is in a range of 2.3 to 3.5MPa; a liquid hourly space velocity is in a range of 1.5 to 8.0h<-1>; a hydrogen/olefin mole ratio is (1.2 to 1.8): 1; and olefin content is less than 1% after hydrogenation.
Description
Technical field
The present invention relates to a kind of preparation and application process thereof of catalyst of coking liquefied gas high-temperature hydrogenation of Catalysts and its preparation method and application, particularly sulfur-bearing for sulfur-bearing liquefied gas hydrogenation.
Background technology
Often decompression of refinery, catalytic cracking, delayed coking, a large amount of liquefied gas of hydrocracking unit by-product.Normal decompression, hydrocracking liquefied gas saturation degree are high, and most domestic enterprise is all used as ethylene cracking material.Catalytic cracking liquefied gas is generally isolated propane, propylene, residue C
4because iso-butane content is higher, and be more or less the same with butenes ratio, generally produce alkylate oil, also have for producing ethylene cracking material through hydrogenation.Catalytic cracking residue C
4sulfur content is lower, and low temperature hydrogenation desulphurization cost is lower, can adopt low temperature hydrogenation explained hereafter ethylene cracking material.Delayed coking unit is taking normal decompression residuum, catalytic slurry as raw material, because the more high reason of sulfur content in raw material heaviness and crude oil, cause delayed coking liquefied gas sulfur content higher, after the desulfurization such as amine absorption, alkali cleaning, washing are processed, sulfur content is still higher, particularly isolates the delayed coking residue C after propane, propylene
4sulfur content is higher, has limited it and has developed, and generally as industry or domestic fuel, chemical utilization rate is not high.
Delayed coking residue C
4n-alkane 70 ~ 75%, olefin(e) centent 30 ~ 36%, compared with catalytic cracking residue C
4producing ethylene cracking material through hydrogenation hydrogen consumption is low, product cracking triolefin yield is high, therefore delayed coking residue C
4the saturated production ethylene cracking material of hydrogenation is that one is utilized approach preferably, both can make ethylene raw lighting, has realized again coking residual C
4chemical utilization.
Delayed coking unit is taking normal decompression residuum, catalytic slurry as raw material, and the heaviness of raw material causes sulphur in its liquefied gas product, metal impurities content higher, has therefore limited its hydrogenation technique.In the LPG of GB 1174-1997 regulations, total sulfur mass fraction is less than 343mg/m
3.Coking liquefied gas in refinery's extracts H through amine liquid
2s, carry out alkali cleaning with 10%NaOH, wash away the H that not extracting is gone
2s and low-grade thioalcohol, the alkali lye that contains sodium mercaptides carries out oxidation regeneration, sedimentation with cobalt sulfonated phthalocyanine and removes after the disulphide that mercaptan oxidation generates lixiviating and wash systemic circulation and use, and after desulfurization is processed, coking liquefied gas sulfur content is generally at 600 ~ 800mg/m
3, and sulfur speciation is taking disulphide as main.Many devices undergo technological transformation to coking desulfuration of liquefied gas device for this reason, adopt tunica fibrosa alkali cleaning to replace traditional static mixer or absorption tower caustic wash desulfuration alcohol technique, increase solvent naphtha tunica fibrosa regenerating alkali liquid extraction system, reduce the sulfur content in coking liquefied gas by methods such as the disulphide in treated gasoline or refined diesel oil extraction regeneration alkali lye, but sulfur content in coking liquefied gas is still at 100 ~ 200mg/m
3, sulfur speciation is still taking disulphide as main.
To sulfur-bearing liquefied gas component hydrogenation, generally adopt molybdenum and/or tungsten, cobalt and/or Raney nickel high-temperature hydrogenation technique, or adopt noble metal catalyst or high-nickel catalyst low temperature hydrogenation technique.Adopt traditional molybdenum and/or tungsten, cobalt and/or Raney nickel high-temperature hydrogenation technique, catalyst need to become sulphided state through presulfurization, and the temperature required height of presulfiding of catalyst process, the time is long.Adopt noble metal catalyst or high-nickel catalyst low temperature hydrogenation technique, further carry out desulfurization, dehydration, dearsenification processing to raw material, to prevent catalyst poisoning.Although high-nickel catalyst increases compared with noble metal catalyst sulfur resistance, when low temperature hydrogenation, still need desulfurization, dearsenification.And coker feedstocks is the heavy charges such as decompression residuum, catalytic slurry, sulphur in coking liquefied gas, arsenic content are high, and desulfurization, sulfur speciation be taking disulphide as main, and desulfurization, dearsenification cost are high.
CN 101433853A discloses a kind of hydrogenation catalyst, preparation method and application thereof, and this catalyst is taking aluminium oxide as carrier, active component palladium 0.3 ~ 0.5wt%, auxiliary agent X
11.0 ~ 3.0wt%, is selected from one or more in B, P, Si, auxiliary agent X
20.01 ~ 5wt%, is selected from one or more in Ag, Pb, Au, Co, Cu, Bi, Ni, Pt, Ti, alkali metal and/or alkaline-earth metal 0.5 ~ 4.0wt%; Catalyst surface area 50 ~ 150m
2/ g, specific pore volume 0.2 ~ 1.0ml/g.This catalyst is specially adapted to the C of catalytic cracking process and steam cracking byproduct in process
4cut fraction hydrogenation is saturated.This catalyst is taking precious metal palladium as active component, and cost is high.And noble metal requires strict to the poisonous substance such as sulphur, arsenic in raw material.
CN 1508103A, ZL01114177.8 disclose respectively and have been applicable to C
4the catalyst of cut fraction hydrogenation, but they are taking noble metal as active component, exist equally catalyst cost high, and the poisonous substance such as sulphur, arsenic in raw material is required to strict defect.
CN 101037613A discloses a kind of preparation method of nickel series hydrogenating catalyst, this catalyst taking aluminium oxide and or silica as carrier, adopt the method for co-precipitation to make, main active component is Ni, La, auxiliary agent X
1with carrier X
2o composition, the weight percentage in catalyst composition: NiO 40 ~ 70%, La
2o
32 ~ 5%, X
1o 2 ~ 5%, X
2o 20 ~ 50%, wherein X
1be selected from Cu, Mg, Zr, X
2be selected from Al, Si; Its specific area 80 ~ 200m
2/ g, specific pore volume 0.4 ~ 0.8ml/g, this catalyst is applicable to monoolefin hydrogenation, is particularly useful for C
9cut fraction hydrogenation, there is higher hydrogenation activity, also there is certain sulfur poisoning-resistant, anti-coking performance, but high-nickel catalyst adopts coprecipitation method to produce, will pass through raw material dissolving, precipitation, filtration, washing, oven dry, moulding, roasting making step, technical process is relatively loaded down with trivial details.
In " petrochemical technology and application " " a kind of preparation of New Nickel series catalysts and application study thereof ", introduce a kind of high nickel content Ni/Al in Lanzhou petrochemical engineering (designing) institute
2o
3-Si
2o catalyst, adopts coprecipitation preparation, is particularly suitable for C
4cut fraction hydrogenation.According to " scientific and technological information " the 8th interim " C in 2006
4alkene is produced the technology research of normal butane " introduce the C of Lan Hua designing institute
4hydrogenation high-nickel catalyst, need to control H in raw material
2s≤50ppm, arsenic≤50ppb, raw material need to carry out the pretreatment such as front adsorption dewatering, adsorption desulfurize hydrogen, absorption dearsenification.
CN 10172200014A discloses a kind of Hydrobon catalyst and preparation method and application, major catalyst is one or both in W and Mo, helping hydrogenation activity component is one or both in Ni and Co, main hydrogenation activity component exists with sulphided state, helps hydrogenation activity component to exist with the form of oxide or salt.230 ~ 330 DEG C of reaction temperatures, are mainly used in catalytically cracked gasoline, catalytic cracking gasoline, coker gasoline, pressure gasoline hydrodesulfurization, and hydrodesulfurization is selectively high, but poor to olefins hydrogenation, to be conducive to keep the octane number of gasoline products.
CN 101081998B discloses a kind of C
4the method of cut fraction hydrogenation, fills in the series connection of hydrogenation catalyst I and hydrogenation catalyst II or segmentation in one or two fixed bed reactors C
4after cut and hydrogen mix, first contact with catalyst I that to carry out diene hydrogenation saturated, then contact and carry out impurity removal and olefin saturated with hydrogenation catalyst II.Hydrogenation catalyst I is taking a kind of aluminium oxide as carrier, contains 0.5 ~ 8% heavy cobalt and/or nickel, 2 ~ 15% heavy molybdenums and/or tungsten, 2 ~ 8% heavy alkali metal; Hydrogenation catalyst II is taking aluminium oxide as carrier, and active component is in oxide and taking catalyst as benchmark, and its content is: tungsten 10 ~ 30% is heavy, nickel 1 ~ 7% is heavy, cobalt 0.01 ~ 1.0% is heavy, co-catalyst 0.1 ~ 10% weight, is selected from arbitrary element in magnesium, zinc, iron, calcium.Two kinds of anti-sulphur of catalyst, anti-arsenic better performances, but catalyst I, II all need through presulfurization before using, and under hydrogen atmosphere, injects CS
2or DMDS carries out presulfurization at 230 ~ 370 DEG C, cure time 8 ~ 32 hours, curing temperature is high, and the time is long.
US Patent No. P4482767 discloses a kind of Pd/Al
2o
3catalyst, for C
3cut fraction hydrogenation.
In sum, classify according to active component, at present to mainly contain palladium system, nickel system, cobalt-molybdenum-nickel be three classes to olefin hydrogenation catalyst.Cobalt-molybdenum-nickel catalyst needs sulfuration before using, curing temperature high (200 ~ 360 DEG C), and the time is long; Palladium series catalyst reaction temperature is low, but noble metal catalyst cost is high, easily poisoning; High-nickel catalyst, needs to adopt coprecipitation preparation, and compared with load method preparation, catalyst preparation process complexity, loaded down with trivial details, also requires raw material to carry out the pretreatment such as front adsorption dewatering, adsorption desulfurize hydrogen, absorption dearsenification.
For delayed coking liquefied gas or delayed coking residue C
4, adopt high-temperature hydrogenation technology to carry out when saturated, the catalyst of present disclosed liquefied gas high-temperature hydrogenation, must carry out numerous and diverse presulfurization.
For delayed coking liquefied gas or delayed coking residue C
4, adopt low temperature hydrogenation technology to carry out when saturated, high-nickel catalyst, preparation process complexity, loaded down with trivial details; Adopt the noble metal catalyst taking palladium as active component, catalyst cost is high.Two kinds of catalyst all need raw material to carry out the pretreatment such as front adsorption dewatering, adsorption desulfurize, absorption dearsenification, control the impurity contents such as sulphur, As, water.And delayed coking liquefied gas or delayed coking residue C
4feature be that sulfur content is high, sulfur speciation is taking disulphide as main, smart desulphurization cost is high, from economic considerations, can bring certain difficulty to industrial applications.
The invention provides a kind of low cost of manufacture, active high, preparation process, the simple hydrogenation catalyst of preprocessing process and application process thereof, for sulfur-bearing coking C
4high-temperature hydrogenation is saturated, and catalyst, after hydrogen atmosphere reduction, does not need presulfurization to process and can be used for hydrogenation reaction, coking liquefied gas or coking residual C
4raw material does not need to carry out the pretreatment such as desulfurization, dearsenification.
Summary of the invention
The invention provides a kind of Catalysts and its preparation method and application for coking liquefied gas high-temperature hydrogenation.Main purpose is need to carry out presulfurization processing while carrying out sulfur-bearing liquefied gas high-temperature hydrogenation for existing catalyst, or high-nickel catalyst preparation process complexity when sulfur-bearing liquefied gas low temperature hydrogenation, loaded down with trivial details, noble metal catalyst cost is high, when low temperature hydrogenation, all need desulfurization of raw material, the problems such as dearsenification pretreatment, provide a kind of cost low, hydrogenation activity is high, preparation process is relatively simple, catalyst is after hydrogen atmosphere reduction, do not need presulfurization processing, raw material does not need catalyst and the application process of the high-temperature hydrogenation of desulfurization processing, for sulfur-bearing delayed coking liquefied gas and coking residual C
4high-temperature hydrogenation is saturated.
Technical scheme of the present invention is as follows:
A kind of coking liquefied gas high-temperature hydrogenation catalyst, is characterized in that: catalyst is taking gama-alumina as carrier, and catalyst activity component is molybdenum, nickel, in total catalyst weight 100%, containing Mo
2o
310.0% ~ 20.0%, NiO 6.0% ~ 18.0%, catalyst is stripe shape, trifolium-shaped or the ball-type of Ф 3 × 3 ~ 5mm, specific area 100 ~ 200m
2/ g.
The content of active component is in total catalyst weight 100%, preferably Mo
2o
313.0% ~ 16.0%, NiO10.0% ~ 13.0%.
The preparation method of catalyst of the present invention, catalyst, taking gama-alumina as carrier, on the carrier after moulding, makes active constituent loading by the mode of dipping through oven dry, roasting.
Active component is introduced in the mode of salting liquid, and the soluble-salt of nickel is nitrate, acetate, formates; The soluble-salt of molybdenum is ammonium molybdate.
Active component simultaneously or step load on carrier, then make finished catalyst after drying, roasting.Preferably step load active component.
Catalyst is prepared step load on carrier, first load active component molybdenum, and load active component nickel again after oven dry, then makes finished catalyst after drying, roasting.
When load active component, 115 ~ 125 DEG C of bake out temperatures, 350 ~ 450 DEG C of sintering temperatures.Preferably 118 ~ 120 DEG C of bake out temperatures, 350 ~ 375 DEG C of sintering temperatures.
The application of catalyst of the present invention, catalyst reduces before using in hydrogen atmosphere, first rises to 120 DEG C with 5 DEG C/min, insulation 2h, then rise to 300 DEG C with 5 DEG C/min, insulation 4h, then in hydrogen atmosphere, bed temperature is down to 180 DEG C, for sulfur-bearing liquefied gas hydrogenation reaction.
The hydrogenation reaction of sulfur-bearing liquefied gas is in thermal insulation or calandria type fixed bed reactor, and its process conditions are: 180 ~ 230 DEG C of feeding temperatures, 280 ~ 300 DEG C of reaction temperatures, reaction pressure 2.3 ~ 3.5MPa, volume liquid hourly space velocity (LHSV) 1.5 ~ 8.0h
-1, hydrogen/olefin molar ratio 1.2 ~ 1.8:1, after hydrogenation, olefin(e) centent all can be less than 1%.
The application process of the described catalyst for sulfur-bearing coking liquefied gas high-temperature hydrogenation, is applicable to refinery's coking liquefied gas, coking residual C
4deng sulfur-bearing liquefied gas high-temperature hydrogenation, after hydrogenation, olefin(e) centent is less than 1%.
Advantage of the present invention is: the prepared catalyst of the present invention is specially adapted to sulfur-bearing liquefied gas fraction high-temperature hydrogenation, hydrogenation carries out in thermal insulation or calandria type fixed bed reactor, catalyst is after hydrogen atmosphere reduction, directly carry out hydrogenation reaction, do not need through vulcanizing treatment, raw material does not need to carry out pre-desulfurization.
Catalyst of the present invention, is carried on active component on the gamma-aluminium oxide carrier after moulding by the mode of dipping, through oven dry, roasting, makes required delayed coking liquefied gas or/and coking residual C
4cut high-temperature hydrogenation catalyst.
After only need reducing before catalyst of the present invention uses, can be used for hydrogenation reaction in hydrogen atmosphere.
Detailed description of the invention
Further illustrate the present invention below by embodiment, but the present invention is not limited to embodiment, authority of the present invention is as the criterion with claims.
The preparation of catalyst: take the gamma-aluminium oxide carrier after a certain amount of moulding, make and the isopyknic load solution of carrier with the soluble-salt of nickel, the soluble-salt of molybdenum, at room temperature carrier is soaked in to certain hour in this load solution, incline and residue soak, after oven dry, roasting, make required catalyst.
Evaluating catalyst condition: 180 ~ 230 DEG C of feeding temperatures, 280 ~ 300 DEG C of reaction temperatures, reaction pressure 2.3 ~ 3.5MPa, volume liquid hourly space velocity (LHSV) 1.5 ~ 8.0h
-1, hydrogen/olefin molar ratio 1.2 ~ 1.8:1.
The required raw material of evaluating catalyst is divided into coking liquefied gas and coking residual C
4two kinds, composition is in table 1.
Table 1 coking liquefied gas and coking residual C
4composition
| Form (v) % | Coking liquefied gas | Coking residual C 4 |
| Propylene | 10.478 | 0.02 |
| Propane | 38.562 | 0.041 |
| Iso-butane | 8.626 | 16.915 |
| Butane | 24.597 | 48.233 |
| Anti-2 butylene | 2.164 | 4.243 |
| 1-butylene | 6.885 | 13.501 |
| Isobutene | 5.071 | 9.944 |
| Along 2 butylene | 1.375 | 2.696 |
| Isopentane | 0.031 | 0.061 |
| Pentane | 1.017 | 1.994 |
| C 5 + | 1.2 | 2.353 |
| ∑C = | 25.993 | 30.385 |
| Hydrogen sulfide, mg/m 3 | 0.5 ----- | |
| Methyl mercaptan, mg/m 3 | 0.5 ----- | |
| COS,mg/m 3 | 8.6 | 9.0 |
| Ethyl mercaptan, mg/m 3 | 1.8 | 3.5 |
| Thiophene, mg/m 3 | 0.1 | 0.15 |
| Methyl sulfide, mg/m 3 | 3.2 | 6.4 |
| Dimethyl disulfide, mg/m 3 | 152.3 | 300 |
| Total sulfur, mg/m 3 | 167 | 319.05 |
Embodiment 1
Take the strip gamma-aluminium oxide carrier 60g (about 90ml) after moulding, according to Mo on final catalyst
2o
3content 13.0%, NiO content 10.0% quantitatively takes four water ammonium molybdates, six water nickel nitrates, is made into 90ml solution.At room temperature carrier is soaked in solution to 12 hours, inclines and residue soak.After 125 DEG C of oven dry, be divided into three parts, respectively at 350,375 DEG C, 400 DEG C, 450 DEG C roasting 6h.The catalyst of preparation is 1#, 2#, 3#, 4#.Specific surface area of catalyst 166.2m
2/ g, 169.8m
2/ g, 166.2m
2/ g, 146.8m
2/ g.
1#, 2#, 3#, 4# catalyst to preparation are evaluated, and evaluating raw material is coking liquefied gas, the results are shown in Table 2.
Catalyst performance prepared by the different sintering temperatures of table 2
Embodiment 2
Take the strip gamma-aluminium oxide carrier 60g (about 90ml) after moulding, quantitatively take six water nickel nitrates according to NiO content 18.0% on final catalyst and be made into 90ml solution, at room temperature carrier is soaked in solution to 12 hours, inclines and residue soak, in 115 DEG C of oven dry; Again according to Mo on final catalyst
2o
3content 20.0%, takes four water ammonium molybdates and is made into 90ml solution, at room temperature the carrier after nickel-loaded is soaked in ammonium molybdate solution to 12 hours, and incline and residue soak, in 120 DEG C of oven dry, 350 DEG C of roasting 6h.The catalyst of preparation is 5#.Specific surface area of catalyst 150.2m
2/ g.
5# catalyst is evaluated, and evaluating raw material is coking liquefied gas, the results are shown in Table 3.
Embodiment 3
Take the strip gamma-aluminium oxide carrier 60g (about 90ml) after moulding, according to Mo on final catalyst
2o
3content 16% takes four water ammonium molybdates and is made into 90ml solution, at room temperature carrier is soaked in solution to 12 hours, inclines and residue soak, in 118 DEG C of oven dry; Take six water nickel nitrates according to NiO content on final catalyst 13.0% again and be made into 90ml solution, at room temperature the carrier after load molybdenum is soaked in nickel nitrate solution to 12 hours, incline and residue soak.In 120 DEG C of oven dry, 350 DEG C of roasting 6h.The catalyst of preparation is 6#.Specific surface area of catalyst 199.8m
2/ g.
6# catalyst is evaluated, and evaluating raw material is coking liquefied gas, and evaluation result is in table 3.
The standby catalyst performance of table 3 active component different loads sequential system
Embodiment 4
Take the trifolium-shaped gamma-aluminium oxide carrier III 60g (about 90ml) after moulding, according to Mo on final catalyst
2o
3content 14% takes four water ammonium molybdates and is made into 90ml solution, at room temperature carrier is soaked in solution to 6 hours, inclines and residue soak, in 120 DEG C of oven dry; Take six water nickel nitrates according to NiO content on final catalyst 12% again, be made into 90ml solution, at room temperature the carrier after load molybdenum is soaked in nickel nitrate solution to 6 hours, incline and residue soak.In 120 DEG C of oven dry, 350 DEG C of roasting 6h.The catalyst of preparation is 7#.Specific surface area of catalyst 188.4m
2/ g.
7# is evaluated, and evaluating raw material is coking liquefied gas, and evaluation result is in table 4.
Embodiment 5
Take the gamma-aluminium oxide carrier III 60g (about 90ml) after moulding, according to Mo on final catalyst
2o
3content 12% takes four water ammonium molybdates and is made into 90ml solution, at room temperature carrier is soaked in solution to 4 hours, inclines and residue soak, in 120 DEG C of oven dry; Take six water nickel nitrates according to NiO content on final catalyst 8.0% again, be made into 90ml solution, at room temperature the carrier after load molybdenum is soaked in nickel nitrate solution to 4 hours, incline and residue soak.In 120 DEG C of oven dry, 350 DEG C of roasting 6h.The catalyst of preparation is 8#.Specific surface area of catalyst 192.8m
2/ g.
8# is evaluated, and evaluating raw material is coking liquefied gas, and compares with 6#, 7#, and evaluation result is in table 4.
The catalyst performance of table 4 different loads amount
Embodiment 6
Take the gamma-aluminium oxide carrier III 60g (about 90ml) after moulding, according to Mo on final catalyst
2o
3content 12% takes four water ammonium molybdates and is made into 90ml solution, at room temperature carrier is soaked in solution to 6 hours, inclines and residue soak, in 120 DEG C of oven dry; Take four water acetic acid nickel according to NiO content on final catalyst 8.0% again and be made into 90ml solution, at room temperature the carrier after load molybdenum is soaked in nickel nitrate solution to 6 hours, incline and residue soak.In 120 DEG C of oven dry, 350 DEG C of roasting 6h.The catalyst of preparation is 9#.Specific surface area of catalyst 190.6m
2/ g.
9# catalyst is evaluated, and compared with 8# evaluating catalyst result, evaluation result is in table 5.
Catalyst performance prepared by table 5 different material
Catalyst application
Application examples 1
Refinery's coking liquefied gas raw material is directly carried out to continously hydrogen adding, use respectively coking liquefied gas, coking residual C in table 1
4for raw material, carry out continously hydrogen adding with the 6# catalyst that embodiment 3 methods make and investigate catalyst life.Investigation the results are shown in Table 6.
The Hydrogenation of table 6 catalyst
Claims (9)
1. a sulfur-bearing coking liquefied gas high-temperature hydrogenation catalyst, is characterized in that: catalyst is taking gama-alumina as carrier, and catalyst activity component is molybdenum, nickel, in total catalyst weight 100%, Mo
2o
313.0%～16.0%, NiO10.0%～13.0%, catalyst is stripe shape, trifolium-shaped or the ball-type of Φ 3 × 3～5mm, specific area 100～200m
2/ g.
2. catalyst as claimed in claim 1, is characterized in that, active component is introduced in the mode of salting liquid, and the soluble-salt of nickel is nitrate, acetate, formates; The soluble-salt of molybdenum is ammonium molybdate.
3. the preparation method of catalyst described in claim 1, is characterized in that catalyst is taking gama-alumina as carrier, by the mode of dipping, active constituent loading, on the carrier after moulding, is made through oven dry, roasting.
4. method as claimed in claim 3, it is characterized in that active component simultaneously or step load on carrier, then make finished catalyst after drying, roasting.
5. method as claimed in claim 4, is characterized in that catalyst prepares step load on carrier, first load active component molybdenum, and load active component nickel again after oven dry, then makes finished catalyst after drying, roasting.
6. method as claimed in claim 3, while it is characterized in that load active component, 115～125 DEG C of bake out temperatures, 350～450 DEG C of sintering temperatures.
7. method as claimed in claim 6, while it is characterized in that load active component, 118～120 DEG C of bake out temperatures, 350～375 DEG C of sintering temperatures.
8. the application of catalyst described in claim 1, it is characterized in that in hydrogen atmosphere, reducing before catalyst uses, first rise to 120 DEG C with 5 DEG C/min, insulation 2h, rise to 300 DEG C with 5 DEG C/min again, insulation 4h is then down to bed temperature 180 DEG C, for sulfur-bearing liquefied gas hydrogenation reaction in hydrogen atmosphere.
9. the application of catalyst according to claim 8, it is characterized in that: the hydrogenation reaction of sulfur-bearing liquefied gas is in thermal insulation or calandria type fixed bed reactor, its process conditions are: 180～230 DEG C of feeding temperatures, 280～300 DEG C of reaction temperatures, reaction pressure 2.3～3.5MPa, volume liquid hourly space velocity (LHSV) 1.5～8.0h-1, hydrogen/olefin molar ratio 1.2～1.8:1, after hydrogenation, olefin(e) centent is all less than 1%.
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