CN106147842A - A kind of passivation start-up method containing molecular sieve gasoline hydrogenation modifying catalyst - Google Patents
A kind of passivation start-up method containing molecular sieve gasoline hydrogenation modifying catalyst Download PDFInfo
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- CN106147842A CN106147842A CN201510245964.7A CN201510245964A CN106147842A CN 106147842 A CN106147842 A CN 106147842A CN 201510245964 A CN201510245964 A CN 201510245964A CN 106147842 A CN106147842 A CN 106147842A
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Abstract
The present invention relates to a kind of passivation start-up method containing molecular sieve gasoline hydrogenation modifying catalyst, in gasoline hydrogenation modifying reactor, the oxidized catalyst of filling is after vulcanizing treatment, reduce reactor inlet temperature, using the mixture of low alkene light-end products and gasoline stocks as passivator, by swing type ladder-elevating temperature, make gasoline proportionality in passivated oil match with passivation temperature, complete to be passivated start-up process.The present invention uses gasoline stocks that low alkene light-end products dilute as passivator, and passivating process has permanent passivation and reversibility passivation concurrently, the purpose of the catalyst activity stability that reaches stably to go into operation, improve.Meanwhile, stepping up the ratio of catalytic gasoline raw material in passivating process, passivating process terminates to complete the incision of raw oil simultaneously, eliminates the raw material after passivation terminates and introduces process.
Description
Technical field
The present invention relates to a kind of passivation start-up method containing molecular sieve gasoline hydrogenation modifying catalyst, the most logical
Cross use low olefin-content raw material oil product as passivator by swing type ladder-elevating temperature in device sulfuration after
Catalyst for hydro-upgrading be passivated, reach to avoid the purpose of temperature runaway, it is adaptable to all kinds contain molecular sieve
The passivation start-up process of gasoline hydrogenation modifying catalyst, be particularly well-suited to produce clean gasoline with high octane and adjust
Hydro-upgrading with component.
Background technology
Catalytic gasoline, coker gasoline etc. all contain a large amount of sulfide, need to process could use through hydrodesulfurization
Make gasoline blend component.Wherein, catalytic gasoline and coker gasoline olefin(e) centent are in 30-50v%, hydrodesulfurization
Hydrocarbon fraction can be caused saturated and reduce octane number, the compound catalyst of preparing by metal Yu molecular sieve can
Reach hydrodesulfurization and isomerization, the purpose of aromatisation minimizing loss of octane number.Wherein, active metal is
Co, Mo, Ni etc., be supported on the alumina support containing molecular sieve, and hydrodesulfurization, different mainly occurs
Structure and aromatization, have certain reaction heat to release in course of reaction, needs to carry out reduced sulphur before using
Change processes；Catalyst for hydro-upgrading containing molecular sieve, while hydrodesulfurization, is reacted by isomery and aromatization
The octane number of product can be improved, but owing to the acidity of catalyst containing molecular sieve is relatively strong, particularly make
With the initial stage, the acidic site that molecular sieve pores road junction exposes is more, and does not has duct to limit, and one side is to reaction
Thing and product do not have adsorption/desorption selectivity, on the other hand have stronger lytic activity and certain polymerization is lived
Property.If being introduced directly into raw material after catalyst reduction vulcanizes, owing to catalyst initial activity is too high, cause temperature
Rising relatively big, be likely to result in system temperature runaway, it is on the low side that cracking simultaneously can cause product liquid to receive.Therefore, catalyst sulfur
Change after terminating, need to be passivated and after raw material hand-off process, could come into operation raw oil according to design data.
At present, hydrogenation plant is in order to solve the too high problem brought of catalyst initial activity, most by adjusting sulfur
Agent and the combination of sulfurized oil and use the method for sulfuration outside device to reduce the initial activity of catalyst, after sulfuration,
Commonly used low temperature, inertia naphthas raw material go into operation, by gradually cutting the side of raw material in inertia oil product
Method, reduces driving temperature runaway risk, or adds cold hydrogen by entrance in reactor design process, reach to fly
The purpose of temperature post-reactor fast cooling.
CN200510047487.X discloses the side of going into operation of a kind of FCC gasoline hydrodesulfurization Olefin decrease technology
Method.On the basis of conventional wet lay sulfidation, select reformed oil as sulfurized oil, vulcanize after terminating,
Strictly control reaction bed temperature, be stepped up FCC gasoline raw material in proportion.This inventive method is permissible
It is applicable to the various sulfidation containing molecular sieve gasoline reforming catalyst, is particularly well-suited to macromolecule sieve content
The sulfidation of gasoline reforming catalyst.Shortcoming is that sulfuration terminates the strict control of switching raw material process needs in proportion
Reaction bed temperature processed, prevents temperature runaway.
At present for the catalyst containing molecular sieve, anhydrous liquid ammonia is a kind of conventional catalyst initial activity passivation
Agent.In device start-up process, injecting a certain amount of anhydrous liquid ammonia, it is adsorbed by acidity of catalyst position after decomposing,
Along with raising and the continuity of the duration of runs of reaction temperature, adsorption potential occurs to resolve reaction, catalyst activity by
Step is recovered, thus reaches the purpose steadily driven.But owing to anhydrous liquid ammonia is that a kind of compressibility liquefaction is poisonous
Gas, has inflammable and explosive feature, needs special storage to transport.Meanwhile, ammonia is adsorbed as reversible reaction,
Therefore passivating process is reversible, although this passivating method is able to ensure that and goes into operation steadily, but cannot remove catalyst
The active sites that upper part is stronger is along with the recovery of catalyst activity, stronger at molecular sieve catalyst opening of the channel
Active sites easily causes the generation of side reaction because not having duct to limit, it is difficult to ensure the activity stabilized of catalyst
Property.
CN201110321354.2 discloses the Startup passivation method of a kind of hydrocracking catalyst, sulfuration knot
Shu Hou, introduces high nitrogen oil in response system, by the ammonia gas absorption of hydrodenitrogeneration reaction generation at catalyst
On complete passivating process.This method avoid the use of anhydrous liquid ammonia, simple to operate.
CN201210432673.5 discloses a kind of hydrocracking unit start-up method, at hydrocracking unit
Load sulfurized hydrogenation catalyst in reaction zone, start-up process: the activation oil that first goes into operation by heat exchange and/or
Heating reaches uniform temperature and passes through beds, is continuously heating to 230 ± 15 DEG C of constant temperature activation, and temperature is extremely
245 ± 15 DEG C introduce nitrogenous light distillates, temperature to 290 ± 15 DEG C or above time, change to nitrogenous heavy distillat
Oil, during temperature to 320 ± 15 DEG C, swap-in raw oil step by step, proceed to normally produce.The method is not injected into liquid
Nitrogen is passivated, but before substep cuts into raw oil, need to introduce respectively low olefin-content nitrogenous light,
Heavy distillate suppresses the initial activity of catalyst as passivator.
Passivating process in CN201110321354.2 and CN201210432673.5 is reversible process,
It is difficult to ensure that the activity stability of catalyst, and all employ the initial boiling point heavy oil product work more than 200 DEG C
For passivated oil, therefore it is not used to the passivation of the relatively low gasoline fraction of the end point of distillation.
Summary of the invention
It is an object of the invention to develop a kind of passivation side of going into operation containing molecular sieve gasoline hydrogenation modifying catalyst
Method, uses the gasoline stocks after the dilution of low alkene light-end products as passivator, enters by controlling gasoline stocks
Doses and the means using temperature swing, staged to heat up control hydrogenation process, utilize course of reaction
On the coke covering catalyst of middle generation, superpower active sites, macromole aromatic hydrocarbons covering catalyst opening of the channel, reach
The purpose of catalyst structure.Catalyst after being passivated by control covers carbon amounts, obtains initial activity suitable, active
The catalyst of excellent in stability, goes into operation steadily ensure that, can be used for containing molecular sieve gasoline hydrogenation modifying
The passivation of catalyst goes into operation.
The technical problem to be solved is that the catalytic gasoline only using low alkene light-end products to dilute is former
Expect as passivator, by catalyst activity position being passivated process, it is ensured that go into operation and operation process is urged
Agent activity is suitable, stable.
A kind of passivation start-up method containing molecular sieve gasoline hydrogenation modifying catalyst, it is characterised in that gasoline adds
Hydrogen reforming reactor loads oxidized catalyst, after vulcanizing treatment, first reduces hydro-upgrading reactor
Inlet temperature to 220-270 DEG C, by gasoline stocks and the low alkene light oil of surplus of 30-50wt%
Product introduce response system as charging, improve hydro-upgrading reactor according to the heating rate of 1-40 DEG C/h
Inlet temperature, when inlet temperature reaches 300-320 DEG C, then drops the inlet temperature of hydro-upgrading reactor
Low 10-30 DEG C；Then the ratio of gasoline stocks in charging is improved to 50-70wt%, according to 1-40 DEG C/h
Heating rate when gradually stepping up the inlet temperature of hydro-upgrading reactor to 320-350 DEG C, again will hydrogenation
The inlet temperature of reforming reactor reduces 10-30 DEG C, then the ratio of gasoline stocks in charging is improved extremely
100wt%, gradually steps up the inlet temperature of reactor to 350-380 DEG C according to the heating rate of 1-40 DEG C/h,
Passivating process terminates, and proceeds to normal gasoline upgrading process after adjusting reactor inlet temperature.In passivating process,
Preferably improve reactor inlet temperature with 1-20 DEG C/h heating rate.
In described passivating process, hydro-upgrading reactor operating procedure condition is: reaction pressure 1.5-2.2MPa,
Volume space velocity 1.5-3.0h-1, hydrogen to oil volume ratio 150-500:1.
Described gasoline stocks is that sulfur content 50-1500mg/kg, olefin(e) centent 35-55v%, arsenic content are less than
The gasoline stocks of 500 μ g/kg, can be catalytically cracked gasoline, catalytic cracking gasoline, coker gasoline, heat
Cracking gasoline or its mixture.
Described low alkene light-end products are that sulfur content is less than 50mg/kg, olefin(e) centent less than 5v%, arsenic content
It is not more than the oil product of 240 DEG C less than 20 μ g/kg, the end point of distillation, can be Petroleum, catalytic reformate, add
Hydrogen refined oil or its mixture.
Described can be regular price gasoline hydrodesulfurization isomerization virtue containing molecular sieve gasoline hydrogenation modifying catalyst
Structure catalyst, generally with aluminium oxide or silicon-containing alumina as carrier, comprises vib and/or VIII
Race's metal and molecular sieve, on the basis of the weight of catalyst, the content of molecular sieve is 5-70wt%, with oxygen
Compound meter, group vib tenor is 2-10wt%, and group VIII metal content is 1-5wt%.
Described containing molecular sieve gasoline hydrogenation modifying catalyst, its molecular sieve can be ZSM-5 and/or
SAPO-11, on the basis of catalyst weight, molecular sieve content is 5-70wt%, preferably 30-65wt%,
Tungsten and/or molybdenum count content as 2-10wt% with oxide, and preferably 2-5wt%, nickel and/or cobalt contain in terms of oxide
Amount is 1-5wt%, preferably 1-3wt%.
In passivation start-up method of the present invention, after passivating process terminates, hydro-upgrading reactor is hydrogenated with
The operating procedure condition of upgrading processes is: reaction pressure 1.5-2.2MPa, reaction temperature 220-450 DEG C, body
Long-pending air speed 1.5-3.0h-1, hydrogen to oil volume ratio 150-500:1；Preferably operating procedure condition is: reaction pressure
1.6-2.0MPa, reaction temperature 220-400 DEG C, volume space velocity 1.7-2.2h-1, hydrogen to oil volume ratio 300-400:1.
Containing molecular sieve gasoline hydrogenation modifying catalyst with isomerization and aromatisation function, according to catalyst
This feature, the present invention utilizes and proportionally switches the process of gasoline stocks catalyst is passivated place
Reason, passivated oil is a certain proportion of gasoline stocks and the mixture of lightweight low alkene oil product.Vapour in passivated oil
When oil ratio is relatively low, olefin(e) centent is the highest, carrying out low-temperature passivation, the coke utilizing side reaction to produce covers urges
In agent, superpower active sites produces permanent passivation effect；In passivated oil, catalytic gasoline ratio is higher, alkene,
During arene content height, carry out high temperature passivation, aromatisation and isomerization reaction now occur on catalyst simultaneously,
It is blunt that the macromole aromatic hydrocarbons utilizing side reaction to produce covers abnormal activity position generation reversibility on molecular sieve pores road junction
Change effect.
In passivation start-up method of the present invention, make gasoline proportionality and passivation temperature phase in passivated oil
Join, controlling in passivating process that catalyst covers carbon amounts is 2-5%, it is to avoid low when catalytic gasoline ratio is higher
Temperature is held time the longer excessive carbon distribution causing catalyst, thus what the irreversibility avoiding carbon distribution to react caused
Loss of catalyst activity.
Compared with prior art, the present invention uses gasoline stocks that low alkene light-end products dilute as passivation
Agent, passivating process has permanent passivation and reversibility passivation concurrently, utilizes activity at molecular sieve catalyst opening of the channel
Position stronger feature more, active, uses carbon distribution, macromole aromatic hydrocarbons to cover the passivation mode of superpower active sites
Preferential passivation does not have selective molecular sieve pore passage surface, reaches stably to go into operation, to improve catalyst activity steady
Purpose qualitatively.Meanwhile, stepping up the ratio of catalytic gasoline raw material in passivating process, passivating process terminates
Complete the incision of raw oil simultaneously, eliminate the raw material after passivation terminates and introduce process.The employing present invention's is blunt
When changing start-up method, passivating process reaction temperature rising is less than 50 DEG C.
Detailed description of the invention
The present invention relates to a kind of passivation start-up method containing molecular sieve gasoline hydrogenation modifying catalyst, specifically real
Under executing such as, wherein, containing molecular sieve gasoline hydrogenation modifying catalyst for using skill as well known to those skilled in the art
Load hydrogenation modifying catalyst prepared by art, its composition is shown in Table 3, gasoline stocks and low alkene light-end products
Character is shown in Table 4, table 5.
Embodiment 1
Gasoline hydrogenation modifying catalyst A is applied to the catalytic gasoline hydrogenation device of 400,000 tons/year,
After catalyst vulcanization process terminates, the inlet temperature of hydro-upgrading reactor is down to 260 DEG C, according to catalysis
Cracking gasoline feedstock flow 21t/h, hydrofined oil oil product flow 26t/h, by catalytically cracked gasoline and hydrogenation
Refined oil is simultaneously introduced response system, and simultaneity factor sends product 47t/h outside；Reactor is improved according to 20 DEG C/h
Inlet temperature, until the inlet temperature of reactor reaches 310 DEG C；
The inlet temperature of hydro-upgrading reactor is down to 300 DEG C, according to catalytically cracked gasoline material flow
33t/h, hydrofined oil oil product flow 14t/h, be simultaneously introduced catalytically cracked gasoline and hydrofined oil instead
System, simultaneity factor is answered to send product 47t/h outside；The inlet temperature of reactor is improved according to 8 DEG C/h, until
The inlet temperature of reactor reaches 340 DEG C；
The inlet temperature of hydro-upgrading reactor is down to 330 DEG C, according to catalytically cracked gasoline material flow
47t/h introduces response system, and simultaneity factor sends product 47t/h outside；The entrance of reactor is improved according to 8 DEG C/h
Temperature, until the inlet temperature of reactor reaches 370 DEG C；Passivating process terminates.Catalytically cracked gasoline raw material
It is fully introduced into response system, passivating process reactor bed maximum temperaturerise 40 DEG C.
In passivating process, the operating procedure condition of hydro-upgrading reactor is: reaction pressure 1.9MPa, body
Long-pending air speed 1.8h-1, hydrogen to oil volume ratio 260:1.
At the catalyst runs initial stage, the sulfur content of hydrogenated products is 7mg/kg, 0.5 unit of loss of octane number.
After catalyst runs three months, the sulfur content of hydrogenated products is 9mg/kg, 0.2 unit of loss of octane number.
Embodiment 2
500ml gasoline hydrogenation modifying catalyst A is filled in 500ml adiabatic reactor hydrogenation reactor, treats
After catalyst vulcanization terminates, the inlet temperature of reactor is down to 250 DEG C, 35wt% catalytic cracking vapour will be contained
The Petroleum of oil introduces response system；Heating rate according to 3 DEG C/h improves the inlet temperature of reactor, directly
Inlet temperature to reactor reaches 315 DEG C；
The inlet temperature of reactor is down to 300 DEG C, is introduced by the Petroleum containing 62wt% catalytically cracked gasoline
Response system；The inlet temperature of reactor is improved, until the inlet temperature of reactor reaches according to 3 DEG C/h
340℃；
The inlet temperature of reactor is down to 320 DEG C, the catalytically cracked gasoline raw material of 100wt% is introduced anti-
Answer system；The inlet temperature of reactor is improved, until the inlet temperature of reactor reaches 370 according to 3 DEG C/h
DEG C, passivating process terminates.In passivating process, the operating procedure condition of reactor is: reaction pressure 1.7MPa,
Volume space velocity 2.0h-1, hydrogen to oil volume ratio 300:1.Catalytically cracked gasoline raw material is fully introduced into response system,
Reactor inlet temperature is adjusted to 320 DEG C, and reaction pressure, volume space velocity, hydrogen-oil ratio are constant, to catalysis
Cracking gasoline carries out hydro-upgrading.
500ml gasoline hydrogenation modifying catalyst B is filled in 500ml adiabatic reactor hydrogenation reactor, weight
Multiple above-mentioned passivation start-up process.
Comparative example 1
500ml gasoline hydrogenation modifying catalyst A is filled in 500ml adiabatic reactor hydrogenation reactor, urges
After agent sulfuration terminates, the inlet temperature of reactor is down to 320 DEG C, catalytically cracked gasoline raw material is introduced
Response system；The operating procedure condition of reactor is: reaction pressure 1.7MPa, volume space velocity 2.0h-1,
Hydrogen to oil volume ratio 300:1.
500ml gasoline hydrogenation modifying catalyst B is filled in 500ml adiabatic reactor hydrogenation reactor, weight
Multiple above-mentioned hydro-upgrading course of reaction.
Table 1 embodiment 2 and comparative example thereof go into operation operation properties of product
Embodiment 3
500ml gasoline hydrogenation modifying catalyst C is filled in 500ml adiabatic reactor hydrogenation reactor, urges
After agent sulfuration terminates, the inlet temperature of reactor is down to 230 DEG C, by urging containing 41wt% coker gasoline
Change reformate and be simultaneously introduced response system；The inlet temperature of reactor is improved according to 10 DEG C/h, until reaction
The inlet temperature of device reaches 310 DEG C；
The inlet temperature of reactor is down to 285 DEG C, will draw containing the catalytic reformate of 65wt% coker gasoline
Enter response system；The inlet temperature of reactor is improved, until the inlet temperature of reactor reaches according to 5 DEG C/h
340℃；
The inlet temperature of reactor is down to 315 DEG C, 100wt% coker gasoline raw material is introduced response system；
The inlet temperature of reactor is improved, until the inlet temperature of reactor reaches 360 DEG C according to 5 DEG C/h；Passivation
Process terminates.In passivating process, the operating procedure condition of reactor is: reaction pressure 2.0MPa, volume
Air speed 1.6h-1, hydrogen to oil volume ratio 400:1.Coker gasoline raw material is fully introduced into response system, by reactor
Inlet temperature is adjusted to 340 DEG C, and reaction pressure, volume space velocity, hydrogen-oil ratio are constant, carries out coker gasoline
Hydro-upgrading.
500ml gasoline hydrogenation modifying catalyst D is filled in 500ml adiabatic reactor hydrogenation reactor, weight
Multiple above-mentioned passivation start-up process.
Comparative example 2
500ml gasoline hydrogenation modifying catalyst C is filled in 500ml adiabatic reactor hydrogenation reactor, urges
After agent sulfuration terminates, the inlet temperature of reactor is down to 320 DEG C, by urging containing 41wt% coker gasoline
Change reformate and introduce response system；After reactor bed temperature rise is not further added by, 65wt% coking vapour will be contained
The catalytic reformate of oil introduces response system；After reactor bed temperature rise is not further added by, 100wt% is burnt
Change gasoline and introduce response system；After reactor bed temperature rise is not further added by, reactor inlet temperature is adjusted
It is 340 DEG C, coker gasoline is carried out hydro-upgrading.The operating procedure condition of reactor is: reaction pressure
2.0MPa, volume space velocity 1.6h-1, hydrogen to oil volume ratio 400:1.
500ml gasoline hydrogenation modifying catalyst D is filled in 500ml adiabatic reactor hydrogenation reactor, weight
Multiple above-mentioned start-up process.
Table 2 embodiment 3 and comparative example thereof go into operation operation properties of product
Table 3 gasoline hydrogenation modifying catalyst and composition thereof
| Composition, % | Catalyst A | Catalyst B | Catalyst C | Catalyst D |
| Nickel oxide | - | - | - | 3.0 |
| Magnesium oxide | - | - | - | 0.5 |
| Molybdenum oxide | 3.5 | 4.5 | 8 | - |
| Cobalt oxide | 1.5 | 2.8 | 5 | - |
| ZSM-5 | 45 | 55 | 40 | 35 |
| SAPO-11 | 15 | 15 | 30 | - |
| Aluminium oxide | Surplus | Surplus | Surplus | Surplus |
Table 4 gasoline stocks and character thereof
| Analysis project | Unit | Catalytically cracked gasoline | Coker gasoline | Analysis method |
| Boiling range FBP | ℃ | 198 | 205 | GB/T 6536 |
| Alkene | Vol% | 45.0 | 35 | GB/T 11132 |
| Sulfur content | mg/kg | 300 | 3000 | SH/T 0689-2000 |
| Arsenic content | μg/kg | 10 | 150 | SH/T 0629-1996 |
Table 5 low alkene light-end products and character thereof
| Analysis project | Unit | Petroleum | Catalytic reformate | Hydrofined oil | Analysis method |
| Boiling range FBP | ℃ | 200 | 198 | 199 | GB/T 6536 |
| Alkene | Vol% | 1.0 | 2.0 | 1.0 | GB/T 11132 |
| Sulfur content | mg/kg | 50 | 10 | 5 | SH/T 0689-2000 |
| Arsenic content | μg/kg | 5 | 2 | 1 | SH/T 0629-1996 |
Claims (10)
1. the passivation start-up method containing molecular sieve gasoline hydrogenation modifying catalyst, it is characterised in that vapour
In oil hydro-upgrading reactor, the oxidized catalyst of filling is after vulcanizing treatment, first reduces hydro-upgrading anti-
Answer the inlet temperature of device to 220-270 DEG C, by light to the gasoline stocks of 30-50wt% and the low alkene of surplus
Matter oil product introduces reactor as charging, improves hydro-upgrading reactor according to the heating rate of 1-40 DEG C/h
Inlet temperature, when inlet temperature reaches 300-320 DEG C, then the inlet temperature by hydro-upgrading reactor
Reduce 10-30 DEG C；Then the ratio of gasoline stocks in charging is improved to 50-70wt%, according to 1-40 DEG C/h
Heating rate when gradually stepping up the inlet temperature of hydro-upgrading reactor to 320-350 DEG C, again will hydrogenation
The inlet temperature of reforming reactor reduces 10-30 DEG C, then the ratio of gasoline stocks in charging is improved extremely
100wt%, gradually steps up the inlet temperature of reactor to 350-380 DEG C according to the heating rate of 1-40 DEG C/h,
Passivating process terminates；In passivating process, preferably improve reactor inlet temperature with 1-20 DEG C/h heating rate.
The passivation side of going into operation containing molecular sieve gasoline hydrogenation modifying catalyst the most according to claim 1
Method, it is characterised in that in described passivating process, hydro-upgrading reactor operating procedure condition is: reaction
Pressure 1.5-2.2MPa, volume space velocity 1.5-3.0h-1, hydrogen to oil volume ratio 150-500:1.
Passivation start-up method containing molecular sieve gasoline hydrogenation modifying catalyst the most according to claim 1,
It is characterized in that, described gasoline stocks is sulfur content 50-1500mg/kg, olefin(e) centent 35-55v%, arsenic
The content gasoline stocks less than 500 μ g/kg.
Passivation start-up method containing molecular sieve gasoline hydrogenation modifying catalyst the most according to claim 3,
It is characterized in that, described gasoline stocks select free catalytically cracked gasoline, catalytic cracking gasoline, coker gasoline and
At least one in the group that pressure gasoline is constituted.
Passivation start-up method containing molecular sieve gasoline hydrogenation modifying catalyst the most according to claim 1,
It is characterized in that, described low alkene light-end products be sulfur content be less than 50mg/kg, olefin(e) centent less than 5v%,
Arsenic content is not more than the oil product of 240 DEG C less than 20 μ g/kg, the end point of distillation.
Passivation start-up method containing molecular sieve gasoline hydrogenation modifying catalyst the most according to claim 5,
It is characterized in that, described low alkene light-end products select free Petroleum, catalytic reformate and hydrofined oil institute
At least one in the group constituted.
Passivation start-up method containing molecular sieve gasoline hydrogenation modifying catalyst the most according to claim 1,
It is characterized in that, the described catalyst for hydro-upgrading containing molecular sieve with aluminium oxide or silicon-containing alumina as carrier,
Comprise vib and/or group VIII metal and molecular sieve, on the basis of the weight of catalyst, molecule
The content of sieve is 5-70wt%, and in terms of the weight of oxide, group vib tenor is 2-10wt%, VIII
Race's tenor is 1-5wt%.
Passivation start-up method containing molecular sieve gasoline hydrogenation modifying catalyst the most according to claim 1,
It is characterized in that, described containing molecular sieve gasoline hydrogenation modifying catalyst, its molecular sieve be ZSM-5 and/
Or SAPO-11, on the basis of catalyst weight, molecular sieve content is 30-65wt%.
Passivation start-up method containing molecular sieve gasoline hydrogenation modifying catalyst the most according to claim 1,
It is characterized in that, described containing in molecular sieve gasoline hydrogenation modifying catalyst, in terms of oxide, tungsten and/or
Molybdenum content be 2-10wt%, preferably 2-5wt%, nickel and/or cobalt content be 1-5wt%, preferably 1-3wt%.
The passivation side of going into operation containing molecular sieve gasoline hydrogenation modifying catalyst the most according to claim 1
Method, it is characterised in that in hydro-upgrading reactor, the operating procedure condition of hydro-upgrading process is: reaction pressure
Power 1.5-2.2MPa, reaction temperature 220-450 DEG C, volume space velocity 1.5-3.0h-1, hydrogen to oil volume ratio
150-500:1, preferred processing condition is: reaction pressure 1.6-2.0MPa, reaction temperature 220-400 DEG C, body
Long-pending air speed 1.7-2.2h-1, hydrogen to oil volume ratio 300-400:1.
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Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5688736A (en) * | 1991-07-30 | 1997-11-18 | Cri International, Inc. | Method of presulfurizing a hydrotreating, hydrocracking or tail gas treating catalyst |
| CN101822985A (en) * | 2009-03-04 | 2010-09-08 | 中国石油天然气股份有限公司 | Pre-treatment method of nickel hydrogenation catalyst |
| CN103785482A (en) * | 2012-10-26 | 2014-05-14 | 中国石油化工股份有限公司 | Olefin isomerization catalyst passivation treatment method |
-
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Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5688736A (en) * | 1991-07-30 | 1997-11-18 | Cri International, Inc. | Method of presulfurizing a hydrotreating, hydrocracking or tail gas treating catalyst |
| CN101822985A (en) * | 2009-03-04 | 2010-09-08 | 中国石油天然气股份有限公司 | Pre-treatment method of nickel hydrogenation catalyst |
| CN103785482A (en) * | 2012-10-26 | 2014-05-14 | 中国石油化工股份有限公司 | Olefin isomerization catalyst passivation treatment method |
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