CN1040612A

CN1040612A - The process for hydrocracking of hydrocarbonaceous of hydrocarbon feed

Info

Publication number: CN1040612A
Application number: CN 89105535
Authority: CN
Inventors: 斯旺·廷格·西
Original assignee: Shell Internationale Research Maatschappij BV
Current assignee: Shell Internationale Research Maatschappij BV
Priority date: 1988-08-11
Filing date: 1989-08-09
Publication date: 1990-03-21
Anticipated expiration: 2004-08-09
Also published as: AU3953489A; IN174056B; DE68920377D1; GB8819121D0; CA1320468C; BR8904006A; CN1021341C; JPH0288694A; DE68920377T2; ES2066836T3; EP0354626B1; AU614865B2; EP0354626A1

Abstract

The hydrocracking that hydrocarbon feed repeatedly reacts ties up in the first step of reaction, and raw material hydrocarbon is contacted with first hydrocracking catalyst.The liquid portion of first effluent that obtains to the major general mixes with second effluent of second step reaction again, the mixture that obtains contacts with same the 3rd hydrocracking catalyst in the presence of the hydrogen in High Temperature High Pressure in three-step reaction, the 3rd effluent that the obtains tripping device of flowing through, the Residual oil fraction is delivered in the reaction of second step again, contacts with same second hydrocracking catalyst in the presence of the hydrogen in High Temperature High Pressure and produces second effluent.

Description

The process for hydrocracking of hydrocarbonaceous of hydrocarbon feed

The method that the present invention relates to adopt repeatedly reaction to carry out hydrocarbon feed hydrocracking.

Hydrocracking is to make heavy hydrocarbon exist the method that contacts with a kind of hydrocracking catalyst under the situation of hydrogen.It has been a kind of very sophisticated method.Because the temperature and pressure of reaction is than higher, so heavy hydrocarbon just is cracked into lower boiling product.Though this method can be finished in a step, but has obtained proof, the method for carrying out polystep reaction can be beneficial to.In the first step of reaction, raw material is earlier through denitrogenation, desulfurization and some hydrocracking, and second step realized just that most hydrocracking reacted.

Existing nitrogen compound in the raw material may throw into question, because in general, therefore unbodied hydrocracking catalyst may be removed activity by nitrogen compound often to the nitrogen sensitivity.Consider that in the past solution to this problem is, in the first step of reaction, adopt the hydrocracking catalyst with hydrodenitrification ability, second step of reaction is then adopted the hydrocracking catalyst to the more insensitive zeolite type of nitrogen.Yet but this class zeolite catalyst brings some shortcomings, and promptly if not adopt high temperature, some macromolecular cracking severities that contain ring texture are not enough.

About this problem, U.S. Patent number 3,702,818 have proposed a kind of solution, promptly adopt the method for two second stage reactors, a reactor charge amorphous catalyst, another reactor charge zeolite catalyst.The macromole of ring texture can be by the amorphous catalyst cracking, and the middle matter hydrocarbon product that still contains some amount in its recycled fluid then can increase the load of catalyzer excessively.

The invention provides a kind of solution to the susceptibility of nitrogen and the method for the not enough problem of the macromolecular structure hydrocracking degree of depth.

Therefore, the process for hydrocracking of hydrocarbonaceous that hydrocarbon feed provided by the invention repeatedly reacts, be included in the first step of reaction, in High Temperature High Pressure and existing under the situation of hydrogen, make raw material hydrocarbon with the contact of first hydrocracking catalyst, produce first effluent, mix with second effluent to the first-class liquid portion that goes out thing of major general again from the reaction of second step, the mixture that obtains contacts with same the 3rd hydrogenation catalyst under the condition that has hydrogen in High Temperature High Pressure in three-step reaction, to produce the 3rd effluent, make the 3rd effluent flow through fractionation plant to obtain at least a top fraction and a kind of Residual oil fraction, residual oil fraction is delivered in the reaction of second step again, contacts with same second hydrocracking catalyst under the condition that exists hydrogen in High Temperature High Pressure and produces second effluent.

If first hydrocracking catalyst has the activity of denitrogenation, the 3rd catalyzer is more insensitive to nitrogen, and second hydrocracking catalyst can the macromolecular words of cracking, just can avoid more above mentioned problems.

The present invention can have some different embodiments, and they are variation patterns of series flow hydrocracking device and two-part hydrocracking device.The schema of these currently known methodss can be with reference to " oil handbook " (The Petrolenm Handbook) sixth version, the 294th～300 page, Elsevier press, nineteen eighty-three, Amsterdam (Amsterdam).

First embodiment is based on series flow hydrocracking device.In general series flow hydrocracking device, the effluent that comes out from the first step reaction flows in the reaction of second step and goes, and the effluent that comes out from the reaction of second step then allows it through a comprehensive process process that comprises fractionation operation.The Residual oil fraction that fractionation operation drew is with first effluent mixing that is about to be sent to the reaction of second step.Three-step reaction of the present invention is then with the second general step reacting phase unanimity.

According to the inventive method, the part of at least the first effluent and second effluent mix and flow to three-step reaction.The 3rd effluent that comes out from three-step reaction passes through the comprehensive process process again, has reclaimed some fractionation products and a kind of Residual oil fraction at this.The Residual oil fraction that comes out from separation column is recycled to the reaction of second step again to draw second effluent.Also can make first effluent through a gas purification step, for example be handled by the solution that utilizes a kind of inorganic aqueous acid or other material.So that remove the ammonia and/or the hydrogen sulfide that in the first step reaction, generate.But, should allow the whole of first effluent be mixed into, the advantage of changing common series flow method is hardly arranged like this with second effluent.Another kind of more excellent scheme is to allow first effluent stand a sepn process, is separated into a liquid phase and vapour phase.Then same the 3rd effluent mixing of vapour phase also stands the comprehensive process process.This method has an advantage, promptly will contain the ammonia of major part in the vapour phase, hydrogen sulfide, and the while is some cracking product also.Therefore do not have the desired product that obtains is cracked into too far and do not wish the C that obtains _1-4The danger of product.The liquid phase that only contains little ammonia in first effluent is with second effluent mixing that is about to send to the 3rd step hydrocracking.Certainly, first effluent also can be separated under various temperature and pressure condition.So just the temperature of first effluent need be cooled to below the temperature of the first step reaction.But, preferably this sepn process is still undertaken by the same temperature and pressure of the first step reaction basically.So just avoid first effluent is heated or the refrigerative benefit.Another kind of more superior embodiment is that this sepn process can realize in the same reaction vessel that carries out the first step reaction.This can form a negative area at reaction container bottom, takes out liquid and vapor capacity by different perforates again and reaches.Should recognize in the first step reaction and some little fluctuations may occur.The carrying out of sepn process preferably carries out reflecting under the uniform temp of oral area position and the pressure with the first step.

Another embodiment of the present invention is to derive out from general secondary hydrogenation cracker.In general hydrocracking device, the effluent that comes the autoreaction the first step is the effluent mixing with the reaction of second step, mixed effluent has then obtained desired various distillage and a kind of Residual oil fraction that is sent to the reaction of second step again through a comprehensive process process that comprises fractionation operation in the fractionation.

According to the present invention, above-described this embodiment, Residual oil fraction after the fractionation operation mixes with the effluent of second step reaction, and then together through three-step reaction, the effluent of three-step reaction is separated into the top fraction of a vapour phase and the end fraction of a liquid phase again.The top fraction that the 3rd effluent separates the back gained preferably mixes with first effluent, and then together through a comprehensive process process, reclaims various products by fractionation operation.Fraction then is sent to the reaction of second step at the bottom of the liquid phase of the 3rd effluent.

According to this way, this programme can be obtained one or more distillation fractions and they are recycled into product by fractionation operation by first effluent, also obtains a kind of Residual oil liquid phase in addition, mixes with second effluent.The top fraction that fractionation operation obtained can be processed respectively.But in this programme, the top fraction that fractionation operation obtained preferably mixes with first effluent that will carry out fractionation operation.

The separation of the 3rd effluent if can be undertaken then can being beneficial to by above-described first flow for separating outflow based on the series flow process for hydrocracking of hydrocarbonaceous.Therefore, though the separation of the 3rd effluent also can be carried out under different temperature and pressure conditions, for example effluent is cooled to below the temperature that is lower than three-step reaction, but had better allows this sepn process carry out according to the uniform temp and the uniform pressure of three-step reaction (on the outlet position) basically.Like this, the 3rd effluent have avoid the heating or the refrigerative benefit.Another kind of more superior embodiment is that this lock out operation can carry out in the same reaction vessel of three-step reaction.This can form a negative area in the bottom of reaction vessel, takes out liquid and vapor capacity by different perforates again and reaches.

Second step also can carry out in different reactors with three-step reaction.But, preferably this two-step reaction still carries out to good in same reactor.In general, the difficulty of doing involved technological transformation like this is very not many, because most general hydrocracking device all includes a plurality of catalyst beds, so as long as the feed pipeline is done this change and each bed is loaded different catalyzer, general hydrocracking device is just applicable to the inventive method.

Above-described first hydrocracking catalyst preferably has a kind of catalyzer of hydrodenitrification and/or hydrogen sweetening power.The suitable catalyst that comprises first hydrocracking catalyst will comprise the metal of VIII family at least a periodic table of elements and/or VI b family on its unbodied carrier.Carrier is preferably from containing silica, alumina, and thorium dioxide, titanium dioxide, magnesium oxide, the classification of zirconium dioxide and their mixing system are chosen.Carrier preferably contains alumina.Can be with reference to the periodic table of elements of stepping on " physics and chemical handbook " (Handbook of Chemistry and Physics), the 55th edition (1975) CHC press, Ohio, USA.

In reaction of second step and three-step reaction, can adopt identical or different hydrocracking catalyst.All can adopt the combination or the mixture of different catalysts in each step reaction: promptly catalyst for reaction combination of per step or mixture can be identical or inequality.But, be used for the second step catalyst for reaction, catalyst combination or mixture preferably will be with being used for three-step reaction person difference.

Second hydrocracking catalyst preferably has the catalyzer of good cracking performance to the macromole that contains some ring texturees.Second hydrocracking catalyst is preferably in and contains the metal that contains a kind of VIII family and/or VI b family on silica-alumina carrier at least.This catalyzer is often very sensitive to nitrogen.But owing to will live through twice hydrocracking process by the cracked hydrocarbon feed on this silica-alumina catalyzer, nitrogen is removed, so can not adopt the shortcoming of nitrogen sensitive catalyst here.It is emphasized that the second step reaction also can adopt other catalyzer, for example with alumina, silica, titanium dioxide, magnesium oxide, zirconium dioxide or their mixture be basic catalyzer etc.It also is possible adopting the catalyzer of zeolite type in the second step reaction, but not so good, though because this catalyst activity is very strong, but they transform macromolecular activity and await to improve.

The 3rd hydrocracking catalyst is zeolite catalyst preferably, also promptly contains the metal of a kind of VIII family and/or VI b family on it contains the carrier of zeolite at least.Be used in the zeolite preferably zeolite of octahedral build, especially Y zeolite on the 3rd hydrocracking catalyst.The silica of this class zeolite/alumina molar ratio can change in 4 to 25, especially changes in 6 to 15.The single pore size of Y zeolite can change in 2.419 to 2.475 nanometers (nm), especially changes in 2.425 to 2.460 nanometers (nm).Except zeolite, the 3rd hydrocracking catalyst must contain a kind of binding agent at least.This binding agent can be from silica, alumina, and silica-alumina, thorium dioxide, titanium dioxide, zirconium dioxide, magnesium oxide and their mixing system are chosen.Especially be more suitable for adopting alumina, also can use together by same silica-vanadine sometimes.

The VIII family that uses in used three kinds of hydrocracking catalysts and/or the catalytically-active metals of VI b family can be from cobalts, nickel, and platinum, palladium is chosen in tungsten and the molybdenum.Preferably adopt non-noble metal mixture, such as nickel-tungsten, nickel-molybdenum, cobalt-molybdenum and cobalt-tungsten.Also can contain phosphorus and/or fluorine in the catalyzer to improve their activity.If hydrocracking catalyst adopts base metal as catalytically-active metals, then its content for the metal of VIII family preferably between 1～16% weight ratio, preferably between 6～24% weight ratios, weight ratio is at total catalyst levels for the metal of VI b family.As adopt precious metal, then its content just should be lower, for example 0.2 to 2% weight ratio.Precious metal is to be used in especially on the 3rd and/or second hydrocracking catalyst.Particularly when catalytically-active metals adopted base metal, they preferably occurred with the form of oxide compound, and perhaps the form with sulfide occurs then for better.The technology of preparing of hydrocracking catalyst is known.

The adoptable hydrocarbon feed of the inventive method comprises gas oil, vacuum gas oil, deasphalted oil, the Residual oil that boils for a long time, vacuum distilling Residual oil, catalytic pyrolysis turning oil, Pintsch process gas oil, and synthetic crude (syncrude).Can be for also having of selecting for use from Tar sands, shale oil, Residual oil are promoted to a higher rank and are processed or biofuel oil raw materials such as (biomassb).In addition, also can adopt the combination of various hydrocarbon feeds.The big portion of general requirement hydrocarbon feed promptly surpasses 50% weight ratio, and the boiling point more than 370 ℃ is arranged.When containing nitrogen in the raw material, the inventive method has superiority especially.Typical nitrogen content scope is below 5000ppmw.Nitrogen content can be from containing 50ppmw.Generally also contain sulphur compound in the raw material.Sulphur content generally is between 0.2 to 6% weight ratio.

Processing condition during reaction, temperature of reaction is preferably between 300 to 450 ℃, especially between 350 ° to 420 ℃, pressure from 50 to 250 crust, especially from 75 to 150 cling to from 0.1 to 10 kilogram/liter/hour of space velocity, especially from 0.2 to 5 kilogram/liter/hour, hydrogen/oil ratio rate from 500 to 5000 standard liter/kilograms, especially from 1000 to 2500 standard liter/kilograms.

Present method will utilize following diagrammatic sketch to be illustrated further.For simplicity, some just do not illustrate the unimportant various kinds of equipment of the present invention.Arbitrary step reaction shown on the figure all has only a catalyst bed, must understand, can utilize a plurality of catalyst beds to replace this catalyst bed.

The embodiment that is based on series flow hydrocracking device shown in Figure 1, wherein second and three-step reaction carry out in single reactor.

The scheme that is based on series flow hydrocracking device shown in Figure 2, wherein reacted first effluent of the first step stands the solution-air lock out operation one time.

The scheme that is based on the two-stage hydrogenation cracker shown in Figure 3, the 3rd effluent wherein are to stand the solution-air lock out operation one time, this lock out operation be carry out second and the same reaction vessel of three-step reaction in carry out.

Can see the reactor 1 that has a catalyst bed 2 at Fig. 1.First hydrocracking catalyst is arranged in the catalyst bed.Also be shown with second reactor that contains the second hydrocracking catalyst catalytic bed 4 and contain the 3rd hydrocracking catalyst catalytic bed 5 among the figure.Show a gas purification part 6 and a separation column 7 in addition.During operation, hydrocarbon feed enters reactor 1 by pipeline 8, enters hydrogen-containing gas by infeeding pipeline 9 simultaneously.Through entering after the catalyst bed, the mixed gas of hydro carbons and hydrogen leaves reactor 1 by pipeline 10.Above mixed gas is added additional hydrogen in addition by pipeline 11 again, and the mixed gas of formation is sent to the position between catalyst bed 4 and 5 in the reactor 3 again.Again with the effluent that comes out from catalyst bed 4, also promptly second effluent mixes this mixed gas then, together by catalyst bed 5, produces the 3rd effluent again, to being drawn by pipeline 12.The effluent of pipeline 12 is to lead to the gas purification part, by this system ammonia in the gas and/or hydrogen sulfide is removed, and is drawn by system by pipeline 13.The operative technique of the part of purifying is on record.Can utilize some gas-liquid separators under differing temps and/or different pressures to come from the product that requires, to isolate hydrogen-containing gas, also can utilize a washing part to remove deammoniation and/or hydrogen sulfide.May contain number of C in the hydrogen-containing gas (recycled hydrogen) _1-2Light hydrocarbons and/or hydrogen sulfide.The hydrogen that reclaims in device 6 is to enter intrasystemly by pipeline 14 recirculation, and the hydrocarbon product pipeline 15 of then flowing through enters separation column 7.They are separated in separation column, produce product stream 16,17 and 18, and a Residual oil fraction of being discharged by separation column 7 through pipeline 19.The Residual oil fraction is to want recirculation to enter reactor 3, also promptly with after mixing from the hydrogen of pipeline 20, enters reactor 3 above catalyst bed 4.The Residual oil fraction is to carry out hydrocracking on catalyst bed 4, produces second effluent.Hydrogen in the pipeline 9,11 and 20 is from a hydrogen supply pipeline 21, and this is to provide by the recycle hydrogen of pipeline 14 with from the hydrogen make-up of pipeline 22.

In Fig. 2, be shown with in order to carry out the reactor that contains a catalyst bed 32 31 of the first step reaction.Also be shown with the reactor that contains catalyst bed 36 35 that carries out the reactor that contains catalyst bed 34 33 that three-step reaction uses and carry out second step reaction usefulness among the figure.Also be shown with 37, one separation columns 38 of a gas purification part and a separator 39 in addition among the figure.During operation, hydrocarbon feed infeeds and with mixing from the hydrogen-containing gas of pipeline 41, enters reactor 31 jointly from pipeline 40, contains therein on the catalyst bed 32 of first hydrocracking catalyst to carry out hydrocracking.First effluent takes out from reactor 31 by pipeline 42, and is sent to separator 39.Separator 39 can be technical known any gas-liquid separation device.Isolating temperature and pressure is preferably identical with reactor 31.Gas phase after the separation is by pipeline 43, and liquid phase is to draw from tripping device 39 by pipeline 44.Liquid phase is to mix with second effluent that comes autoreactor 35 in pipeline 45, and this mixture leads to reactor 33 through pipeline 46 again, and hydrogen is then added reactor by pipeline 47.In reactor 33, on the catalyst bed 34 that contains the 3rd hydrocracking catalyst, carry out hydrocracking from the mixture of pipeline 46, and produce the 3rd effluent that leaves reactor 33 by pipeline 48.The gas phase part that in the 3rd effluent, adds first effluent in the pipeline 43 again, this combined flow is sent in the gas purification device 37 again, produce useless air-flows such as the ammonia of discharging and/or hydrogen sulfide by pipeline 49, by the recycled hydrogen of pipeline 50 discharges and the hydrocarbon product of discharging by pipeline 51.Pipeline 51 is guided separation column 38 into, in separation column with regard to recyclable

relevant product

52,53,54.Distillation procedure in separation column 38 also produces one Residual oil fraction that is sent to reactor 35 by pipeline 55.The Residual oil fraction carries out hydrocracking on the catalytic bed 36 that contains second hydrocracking catalyst under the situation that the hydrogen of being sent here by pipeline 56 exists.Formed second effluent after hydrocracking on the catalyst bed 36 takes out by pipeline 45, and the liquid-phase mixing in the pipeline 44 that coexists.Used hydrogen infeeds by pipeline 57, and it is to be facilitated by the hydrogen make-up of pipeline 58 and the recycled hydrogen from pipeline 50.

Separator 39 also can be introduced in reactor 31 as the negative area, and this also is significant.Can save the expense of separating device like this.It also is possible that

catalyst bed

36 and 34 is placed in the same reactor as catalyst bed shown in Figure 14 and 5.

Shown in Fig. 3 is the reactor 61 that contains the first hydrocracking catalyst catalytic bed 62, gas purification device 63, separation column 64 and contain second reactor 65 of the catalyst bed of using for the catalyst bed 66 of the second step reaction usefulness with for three-step reaction 67.Reactor 65 also contains the separatory negative area 68 of air feed-liquid.During operation, the hydrocarbon feed in pipeline 69 is with mixing from the hydrogen of pipeline 70, together enters reactor 61 and carry out hydrocracking on 62 first hydrocracking catalyst on the catalytic bed.First effluent that forms is drawn reactor 61 through pipeline 71.First effluent mixes with the vapour phase top fraction in the pipeline 72 again, this mixture is sent to purifying plant 63 again, isolated ammonia and/or hydrogen sulfide again by pipeline 74 by discharging in the system, hydrogenous gas is to enter in the system by pipeline 75 recirculation, and the hydrocarbon product pipeline 76 of then flowing through enters separation column and separates.Reclaimed relevant product 77,78 and 79 in separation column 64, the Residual oil fraction then flows out by pipeline 80.Add in the Residual oil fraction from the hydrogen in the pipeline 81, this mixture enters reactor 65 again between catalyst bed 66 and 67 again.Between catalyst bed 66 and 67, mix from the same effluent of the Residual oil fraction of pipeline 80, and then, produce the 3rd effluent together by catalyst bed 67 from catalyst bed 66.The 3rd effluent flows to negative area 68 again, carries out solution-air and separates.The top fraction of gas phase takes out by pipeline 72, and mixes with first effluent, and the Residual oil fraction then leaves reactor 65 by pipeline 82, mixes with the hydrogen from pipeline 83, and recirculation enters reactor 65, but is to introduce on the position that is higher than catalyst bed 66.The Residual oil fraction is to carry out hydrocracking and produce second effluent on second hydrocracking catalyst on the catalyst bed 66.Used hydrogen is to be infeeded by pipeline 84, and it is by from the hydrogen make-up of pipeline 85 with from the recycled hydrogen synthetic of pipeline 75.

Claims

1, the process for hydrocracking of hydrocarbonaceous of hydrocarbon feed through repeatedly reacting, it is included in the first step of reaction, in High Temperature High Pressure and existing under the condition of hydrogen, make raw material with the contact of first hydrocracking catalyst, produce first effluent, the near again small part first effluent liquid mixes with second effluent from the second step reaction, and the mixture of acquisition is in three-step reaction, and the 3rd hydrocracking catalyst contacts to produce the 3rd effluent together under High Temperature High Pressure and the situation that exists hydrogen; Make the 3rd effluent tripping device of flowing through at last, obtain at least a top fraction and a kind of Residual oil fraction thus, the Residual oil fraction is delivered in the reaction of second step again, contacts with same second hydrocracking catalyst under the condition that exists hydrogen in High Temperature High Pressure, produces second effluent.

2, all mix mutually according to first effluent that the process of claim 1 wherein with second effluent.

3, according to the method for claim 1 or 2, first effluent wherein is divided into liquid and gas through lock out operation, and gas phase is mixed with the 3rd effluent, and liquid phase is then mixed with second effluent that will be sent to three-step reaction.

4, according to the method for claim 3, first effluent wherein, with the roughly the same temperature and pressure of the first step reaction under be separated into gas phase and liquid phase.

5, according to arbitrary method of claim 1～4, wherein reclaim as product by separating obtained top fraction.

6, from first effluent, obtain one or more fractions according to the process of claim 1 wherein through fractionation operation, and they are reclaimed as product.Obtained raffinate then mixes with second effluent.

7, according to the method for claim 6, wherein the top fraction by the fractionation operation gained is with first effluent mixing that is about to stand fractionation operation.

8, according to arbitrary method of claim 1～7, first hydrocracking catalyst wherein contains a kind of metallic element in VIII family and/or the VI b family at least in its unbodied carrier.

9, method according to Claim 8, carrier wherein is from silica, alumina, thorium dioxide, titanium dioxide, magnesium oxide is chosen in zirconium dioxide and their mixture.

10, according to the method for claim 9, carrier wherein contains alumina.

11, according to arbitrary method of claim 1～10, second hydrocracking catalyst wherein contains a kind of metallic element in VIII family and/or the VI b family at least in it contains the carrier of silica-alumina.

12, according to arbitrary method of claim 1～11, the 3rd hydrocracking catalyst wherein contains a kind of metallic element in VIII family and/or the VI b family at least in it contains the carrier of zeolite.

13, according to the method for claim 12, zeolite wherein is octahedra zeolite (fauja site type), especially a Y zeolite.

14, according to arbitrary method of claim 1～13, the first, the second, the 3rd hydrocracking catalyst wherein contains a kind of metallic hydrogenation component at least, and this metal is selected from nickel, cobalt, platinum, palladium, tungsten and molybdenum.

15, according to arbitrary method of claim 1～14, a step wherein or the temperature of polystep reaction are 300 to 450 ℃, and pressure is 50 to 250 crust, and space velocity is 0.1 to 10 kilogram/liter/hour, and hydrogen is 500 to 5000 standard liter/kilograms with the ratio of oil.