CN105733674B - A kind of method that inverted sequence is hydrocracked - Google Patents
A kind of method that inverted sequence is hydrocracked Download PDFInfo
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- CN105733674B CN105733674B CN201410733251.0A CN201410733251A CN105733674B CN 105733674 B CN105733674 B CN 105733674B CN 201410733251 A CN201410733251 A CN 201410733251A CN 105733674 B CN105733674 B CN 105733674B
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Abstract
The invention discloses a kind of method that inverted sequence is hydrocracked.Raw material, hydrogen and be hydrocracked generation oil mixing after, reacted into hydrofining reactor；Hydrofinishing effluent enters separator and fractionating system, obtains product and recycle oil；Recycle oil enters hydrocracking reactor after being mixed with hydrogen, and cracking reaction is carried out in the presence of hydrocracking catalyst；At least two beds are set in hydrocracking reactor, set gas phase to draw pipeline in two adjacent catalyst bed interlayers；Gaseous stream leads to high-pressure separator via the vapor delivery line, liquid phase by the beds of lower section and with the hydrogen counter current contacting that enters from reactor bottom, carry out hydrocracking reaction.The inventive method technique is simple, it is easy to operate；High-pressure separator is directly entered because the gas phase light component of cracking is extracted, the secondary or multiple cracking reaction of the part light component is reduced, thus the liquid product yield being hydrocracked can be effectively improved.
Description
Technical field
The present invention relates to a kind of method that inverted sequence is hydrocracked, belong to petroleum refining field.
Background technology
It is one of main technique of heavy distillate deep processing to be hydrocracked, and it is not only petroleum refining industry's production light oil
The important means of product, and turned into the key technology of petrochemical enterprise, play the not replaceable effect of other techniques.
C in hydrocracked product1~C4The economic value of product is relatively low, and consumption amounts of hydrogen is big, so technologist can protect
On the premise of demonstrate,proving smooth operation and product quality, gas yield is reduced as far as possible, increases liquid yield.
Hydrocracking process gas yield is usually 4%~6%（Based on raw material oil quality）.According to feedstock property, need
Purpose product is different with process conditions, and gas yield also can be different.Generally, gas yield is with the improve of conversion ratio
Increase.
Hydrofinishing and to be hydrocracked for overall process be exothermic process, under the conditions of industrial operation, hydrogenation reaction
Device is adiabatic reactor, so each bed can produce temperature rise in reactor.Simultaneously along the direction of reaction stream, refine and cracking
Reaction is constantly deepened, and the molecular weight of intermediate product is tapered into, and relative volatility increases, and causes the rate of gasification of logistics and increases.Essence
Temperature rise is the main cause for causing rate of gasification gradually to increase in reactor processed, imports and exports rate of change smaller.It is big in cracker
It is to cause to export the main cause that rate of gasification is significantly increased to measure volatile pyrolysis product.
Under different condition, the rate of gasification in hydrocracking process reactor is different.Using one-stage serial hydrocracking technique as
Example, when feedstock property is identical, production heavy naphtha is compared with producing intermediate oil scheme, finishing reactor entrance, outlet
Rate of gasification change it is essentially identical, be 10% or so.The rate of gasification change difference of cracker very greatly, produces heavy naphtha side
The cracker outlet rate of gasification of case can reach 100%, show that the reactor lower part bed, without liquid phase, occurs
Be typical gas-solid reaction.The cracker rate of gasification of production intermediate oil scheme is increased to by 10% or so of entrance
60% or so of outlet.Using once by being compared with circulate operation mode, the former cracking severity is relatively low, corresponding cracking reaction
The rate of gasification of device is more slightly lower.
Rate of gasification in hydrocracking reactor is higher, particularly in cracker lower catalyst bed layer, a lot
The light component of cracking can not export reactor in time, carry out secondary or multiple cracking generation C1~C4Product, reduces hydrogenation
Cracking liquid is received.And increase catalyst in the increase with multiple cracking reaction, hydrocracking reactor with gas phase light component
From top to bottom carbon deposit also gradually increases bed.
Chinese patent 200710011928.X discloses a kind of hydrogenating conversion process, this method include long distillate feedstock oil with
Enter the first hydroconversion reaction zone after the generation logistics mixing of second hydroconversion reaction zone, the hydrogenated reacted product of processing is flowed through point
From hydrogen-rich gas and liquid is obtained, hydrogen-rich gas is recycled, and liquid enters fractionating column fractionation and obtains light-end products and tail oil, tail
Oil is mixed into the second hydroconversion reaction zone with hydrogen, and the second hydroconversion reaction zone product stream enters the first hydroconversion reaction zone.The party
Method realizes that long distillate raw material directly produces cleaning automotive fuel and high-quality industrial chemicals in a set of hydrogenation system, but not
Consider how to avoid cracking reaction part light component deep pyrolytic.
The content of the invention
In view of the shortcomings of the prior art, the present invention provides a kind of method that inverted sequence is hydrocracked, and will particularly be hydrocracked
Gas phase in reactor is introduced directly into high-pressure separator, reduces the excessive cracking of light component, the method for being hydrocracked liquid receipts.
The method that a kind of inverted sequence of the present invention is hydrocracked, including following content：
A) after hydrogen needed for raw material, reaction and hydrocracking reactor outflow material are mixed, into hydrofining reactor,
Deposited in Hydrobon catalyst and hydrofining reaction is carried out under Hydrofinishing conditions；
B) material after step a) hydrofinishings enters high-pressure separator and fractionating system, and the recycle stock isolated is with following
Enter hydrocracking reactor after the mixing of ring hydrogen, exist in hydrocracking catalyst and be hydrocracked under hydrocracking condition
Reaction；At least two beds are wherein set in hydrocracking reactor, set gas phase to draw in two catalyst bed interlayers
Go out pipeline；The pipeline that gaseous stream is set via catalyst bed interlayer leads to high-pressure separator, and liquid phase passes through following catalyst
Bed and the hydrogen counter current contacting entered from reactor bottom, carry out hydrocracking reaction；
C) hydrocracking reactor outflow material is directly entered hydrofining reactor, and unreacted hydrogen is used as recycle hydrogen
It is recycled back to hydrofining reactor and/or hydrocracking reactor.
Described raw material can be straight-run oil, coking distillate, catalytic fraction oil, shale oil, coal tar in step a)
Deng one or more, boiling range scope is general in the range of 150 DEG C~600 DEG C, preferably in the range of 200 DEG C~540 DEG C.
Described hydrocracking reactor is one in conventional hydrocracking reactor, hydrocracking reactor in step b)
As set 2~8 beds, according to current unit scale, typically set 4 beds.Generally, exist
Rate of gasification after raw material reaction under reaction condition（Rate of gasification refers at reaction conditions, and the raw material for being converted into gas phase accounts for raw material gross mass
Ratio, not hydrogen）More than 30%（Quality）Catalyst bed interlayer set gas phase draw pipeline.Described gas phase fairlead
Line is generally arranged at two adjacent catalyst bed interlayers.
Described gas phase draws pipeline and is preferably provided at catalyst bed interlayer gas-liquid partition tray or cold hydrogen box in step b)
Lower section.
The operating condition of above-mentioned steps hydrofining reactor is：300 ~ 450 DEG C of reaction temperature, preferably 330 ~ 400 DEG C；Instead
Answer 6.0 ~ 18.0MPa of pressure, preferably 10.0 ~ 16.0MPa；0.2 ~ 4.0h of volume space velocity-1, preferably 0.6 ~ 2.0h-1；Hydrogen oil volume
Than 500:1~1500:1, preferably 600:1~1200:1.
The operating condition of hydrocracking reactor is：300 ~ 450 DEG C of reaction temperature, preferably 330 ~ 400 DEG C；Reaction pressure
6.0 ~ 18.0MPa, preferably 10.0 ~ 16.0MPa；0.2 ~ 4.0h of volume space velocity-1, preferably 0.6 ~ 2.0h-1；Gas phase is drawn on pipeline
Surface catalysis agent bed hydrogen to oil volume ratio 500:1~1500:1, preferably 600:1~1200:1；Gas phase draws catalyst bed below pipeline
Layer hydrogen to oil volume ratio 220:1~1000:1, preferably 300:1~800:1.It is preferred that the hydrogen-oil ratio of hydrocracking reactor is higher than hydrogenation essence
The hydrogen-oil ratio 200~800 of reactor processed, most preferably 300~600.
Catalyst used in above-mentioned steps is this area conventional catalyst.The active metal component of Hydrobon catalyst
Can be the one or more such as nickel, cobalt, molybdenum or tungsten, catalyst is carrying out vulcanizing treatment using preceding, active metal component is converted
For sulphided state.Hydrobon catalyst composition can include by weight percentage：Nickel or cobalt are 0.5% ~ 10%（By its oxide
To calculate）, molybdenum or tungsten are 1% ~ 25%（Calculated by its oxide）, carrier can be aluminum oxide, silica, alumina-silica
One or more in silicon, titanium oxide.Catalyst is extrudate or spherical.The heap density of catalyst is 0.5 ~ 1.1g/cm3, urge
Catalyst particles diameter（Spherical diameter or bar shaped diameter）For 0.4 ~ 3.0mm, specific surface area is 80 ~ 350m2/g.Hydrofinishing is catalyzed
The active metal component of agent can be the one or more in nickel, cobalt, molybdenum or tungsten, and catalyst is carrying out vulcanizing treatment using preceding,
Active metal component is converted into sulphided state.Hydrocracking catalyst composition can include by weight percentage：Nickel or cobalt are
0.5%~10%（Calculated by its oxide）, molybdenum or tungsten are 1% ~ 25%（Calculated by its oxide）, carrier includes molecular sieve
And/or the Cracking Component such as amorphous silica-alumina, while can be aluminum oxide, silica, aluminium oxide-silicon oxide, the one kind such as titanium oxide
Or it is several.Catalyst is extrudate or spherical.The heap density of catalyst is 0.5 ~ 1.1g/cm3, catalyst particle diameter（It is spherical
Diameter or bar shaped diameter）For 0.4 ~ 3.0mm, specific surface area is 150 ~ 400m2/g。
Compared with prior art, this have the advantage that：
1st, present invention process is simple, it is easy to operate, and simple transformation can be carried out in hydrocracking unit and be can be achieved.
2nd, in the material after hydrocracking reactor upper catalyst bed layer, cracked gas phase light component has portion
Divide to be extracted and be directly entered high-pressure separator, reduce the secondary or multiple cracking reaction of the part light component, can be effectively
Improve the liquid product yield being hydrocracked.
3rd, in hydrocracking reactor lower catalyst bed layer the secondary or multiple cracking reaction of light component reduction, can be with
Reduce the carbon deposit of beds, the service cycle of extension fixture.
4th, the beds that gas phase is drawn below pipeline are operated using gas-liquid counter current, can improve gas-liquid mass transfer efficiency,
Promote hydrocracking reaction, improve the conversion level of heavier liquid phase；The part that cracking is produced in lower catalyst bed layer simultaneously is light
Component can also leave reactor, further increase the liquid product yield being hydrocracked.
Brief description of the drawings
Fig. 1 is the method schematic diagram that a kind of inverted sequence of the invention is hydrocracked.
Wherein：1- hydrofining reactors, 2- hydrocracking reactors, 3- hydrocracking reactor upper catalyst beds
Layer, 4- hydrocracking reactors lower catalyst bed layer, 5- feedstock oils, 6- high-pressure separators, the discharging of 7- hydrocracking reactors,
8- circulating hydrogens, 9- recycle oils（Unconverted oil）, 10- fractionating systems, 11- gases, 12- naphtha cuts, 13- midbarrels
Oil.
Embodiment
In the inventive method, hydrocracking reactor is set sets gas phase to draw in the middle of 2 beds, beds
Go out pipeline, gaseous stream leads to high-pressure separator by catalyst bed interlayer pipeline, liquid phase by following beds with from
The hydrogen counter current contacting that reactor bottom enters, carries out hydrocracking reaction, reduces light group of upper catalyst bed slabbing
Divide and carry out secondary or multiple cracking reaction in lower catalyst bed layer, can increase and be hydrocracked liquid receipts, reduction hydrogen is consumed, and extension is urged
Agent service life.
The method that a kind of inverted sequence of the invention is hydrocracked is further described below.
As shown in Figure 1：After hydrogen 8 needed for raw material 5, reaction and hydrocracking reactor outflow material 7 are mixed, into hydrogenation
Finishing reactor 1, deposits in Hydrobon catalyst and hydrofining reaction is carried out under Hydrofinishing conditions；Thing after hydrofinishing
Material enters high-pressure separator 6 and fractionating system 10, and the gas 11 isolated, naphtha cut 12 and midbarrel 13 go out device,
The recycle stock 9 isolated（I.e. unconverted tail oil）Enter hydrocracking reactor 2 after being mixed with recycle hydrogen 8, be hydrocracked
Catalyst exists and carries out hydrocracking reaction under hydrocracking condition；At least two catalyst are set in hydrocracking reactor
Bed（It is 2 in Fig. 1）, catalyst bed interlayer setting gas phase extraction pipeline；Gaseous stream is drawn by catalyst bed interlayer pipeline
To high-pressure separator 6, liquid phase is added by following beds and the counter current contacting of hydrogen 8 entered from reactor bottom
Hydrogen cracking reaction, reduces the light component of upper catalyst bed 3 cracking of layer in the secondary or multiple of the progress of lower catalyst bed layer 4
Cracking reaction.
To further illustrate the solution of the present invention, following examples are enumerated.
Embodiment 1
Hydrocracking reactor sets 2 beds, and 2 catalyst bed interlayers set gas phase to draw pipeline and high pressure
Separator is connected.Feedstock property is shown in Table 1, catalyst, process conditions and the results are shown in Table 2.Catalyst FF-26 is Fushun petrochemical industry
The commodity Hydrobon catalyst of research institute's development and production, FC-24 adds for the commodity of Fushun Petrochemical Research Institute's development and production
Hydrogen Cracking catalyst.
Comparative example 1
Technological process, catalyst and the raw material that comparative example is used are identical with embodiment, simply eliminate gas phase and draw pipeline.
Feedstock property is shown in Table 1, catalyst, process conditions and the results are shown in Table 2.
The feedstock property of table 1.
The process conditions of table 2 and result.
* upper catalyst bed layer refers to that gas phase extracts the hydrocracking catalyst bed above pipeline, and lower catalytic agent out
Bed refers to that gas phase extracts the hydrocracking catalyst bed below pipeline out.
Result above can be seen that in process conditions under the same conditions, using the inventive method, in feed stock conversion phase
With under conditions of, C in hydrocracked product5 +Liquid receives 2.8 percentage points of increase, and economic benefit is obvious.Simultaneous reactions temperature can be with
Further reduction, under identical operating conditions, can also improve the treating capacity of device.
Claims (15)
1. a kind of method that inverted sequence is hydrocracked, including following content：
A) after hydrogen needed for raw material, reaction and hydrocracking reactor outflow material mixing, into hydrofining reactor,
Hydrobon catalyst is deposited and hydrofining reaction is carried out under Hydrofinishing conditions；
B) material after step a) hydrofinishings enters high-pressure separator and fractionating system, the recycle stock isolated and circulation
Enter hydrocracking reactor after hydrogen mixing, it is anti-in the presence of being hydrocracked with progress under hydrocracking condition in hydrocracking catalyst
Should；At least two beds are wherein set in hydrocracking reactor, set gas phase to draw in two catalyst bed interlayers
Pipeline；The pipeline that gaseous stream is set via catalyst bed interlayer leads to high-pressure separator, and liquid phase passes through following catalyst bed
Layer and the hydrogen counter current contacting entered from reactor bottom, carry out hydrocracking reaction；
C) hydrocracking reactor outflow material is directly entered hydrofining reactor, and unreacted hydrogen is followed as recycle hydrogen
Loopback hydrofining reactor and/or hydrocracking reactor.
2. in accordance with the method for claim 1, it is characterised in that described raw material is that straight-run oil, coking evaporate in step a)
The one or more divided in oil, catalytic fraction oil, shale oil and coal tar.
3. in accordance with the method for claim 2, it is characterised in that the boiling range scope of the raw material is at 150 DEG C~600 DEG C.
4. in accordance with the method for claim 1, it is characterised in that set 2 in step b) in described hydrocracking reactor
~8 beds.
5. in accordance with the method for claim 4, it is characterised in that rate of gasification is more than 30 matter after raw material reacts at reaction conditions
The catalyst bed interlayer for measuring % sets gas phase to draw pipeline.
6. according to the method described in claim 1 or 5, it is characterised in that described gas phase is drawn pipeline and is arranged in step b)
The lower section of catalyst bed interlayer gas-liquid partition tray or cold hydrogen box.
7. in accordance with the method for claim 1, it is characterised in that the operating condition of hydrofining reactor is：Reaction temperature
300 ~ 450 DEG C, 6.0 ~ 18.0MPa of reaction pressure, 0.2 ~ 4.0h of volume space velocity-1, hydrogen to oil volume ratio 500:1~1500:1.
8. in accordance with the method for claim 1, it is characterised in that the operating condition of hydrocracking reactor is：Reaction temperature
300 ~ 450 DEG C, 6.0 ~ 18.0MPa of reaction pressure, 0.2 ~ 4.0h of volume space velocity-1；Gas phase draws pipeline uppermost catalyst bed hydrogen
Oil volume compares 500:1~1500:1, gas phase draws beds hydrogen to oil volume ratio 220 below pipeline:1~1000:1.
9. in accordance with the method for claim 1, it is characterised in that the hydrogen-oil ratio of hydrocracking reactor is anti-higher than hydrofinishing
Answer the hydrogen-oil ratio 200~800 of device.
10. in accordance with the method for claim 1, it is characterised in that the active metal component of described Hydrobon catalyst
For the one or more in nickel, cobalt, molybdenum or tungsten, Hydrobon catalyst composition includes by weight percentage：Nickel or cobalt press oxygen
Compound is calculated as 0.5% ~ 10%, and molybdenum or tungsten are calculated as 1% ~ 25% by oxide, carrier be aluminum oxide, silica, aluminium oxide-silicon oxide,
One or more in titanium oxide.
11. in accordance with the method for claim 1, it is characterised in that the composition of the hydrocracking catalyst is with weight percent
Include than meter：Nickel or cobalt are calculated as 0.5% ~ 10% by oxide, and molybdenum or tungsten are calculated as 1% ~ 25% by oxide；Carrier includes molecular sieve
And/or amorphous silica-alumina, while including aluminum oxide, silica, the one or more in aluminium oxide-silicon oxide, titanium oxide.
12. in accordance with the method for claim 3, it is characterised in that the boiling range scope of the raw material is at 200 DEG C~540 DEG C.
13. in accordance with the method for claim 7, it is characterised in that the operating condition of hydrofining reactor is：Reaction temperature
330 ~ 400 DEG C, 10.0 ~ 16.0MPa of reaction pressure, 0.6 ~ 2.0h of volume space velocity-1, hydrogen to oil volume ratio 600:1~1200:1.
14. in accordance with the method for claim 8, it is characterised in that the operating condition of hydrocracking reactor is：Reaction temperature
330 ~ 400 DEG C, 10.0 ~ 16.0MPa of reaction pressure, 0.6 ~ 2.0h of volume space velocity-1；Gas phase draws pipeline uppermost catalyst bed hydrogen
Oil volume compares 600:1~1200:1；Gas phase draws beds hydrogen to oil volume ratio 300 below pipeline:1~800:1.
15. in accordance with the method for claim 9, it is characterised in that the hydrogen-oil ratio of hydrocracking reactor is higher than hydrofinishing
The hydrogen-oil ratio 300~600 of reactor.
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Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1552819A (en) * | 2003-05-31 | 2004-12-08 | 中国石油化工股份有限公司 | Light hydrocarbon hydrogenation method |
| CN102465031A (en) * | 2010-11-04 | 2012-05-23 | 中国石油化工股份有限公司 | Hydrotreating method for heavy hydrocarbon raw materials |
| CN103773450A (en) * | 2012-10-24 | 2014-05-07 | 中国石油化工股份有限公司 | Hydrocracking method for processing inferior raw material |
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Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1552819A (en) * | 2003-05-31 | 2004-12-08 | 中国石油化工股份有限公司 | Light hydrocarbon hydrogenation method |
| CN102465031A (en) * | 2010-11-04 | 2012-05-23 | 中国石油化工股份有限公司 | Hydrotreating method for heavy hydrocarbon raw materials |
| CN103773450A (en) * | 2012-10-24 | 2014-05-07 | 中国石油化工股份有限公司 | Hydrocracking method for processing inferior raw material |
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