CN104549061A

CN104549061A - Heavy oil hydrogenation slurry bed reactor and heavy oil hydrogenation method

Info

Publication number: CN104549061A
Application number: CN201310516552.3A
Authority: CN
Inventors: 唐晓津; 张占柱; 胡立峰; 朱振兴; 侯栓弟; 王子军
Original assignee: Sinopec Research Institute of Petroleum Processing; China Petroleum and Chemical Corp
Current assignee: Sinopec Research Institute of Petroleum Processing; China Petroleum and Chemical Corp
Priority date: 2013-10-28
Filing date: 2013-10-28
Publication date: 2015-04-29

Abstract

The invention relates to a heavy oil hydrogenation slurry bed reactor and a heavy oil hydrogenation method. The heavy oil hydrogenation slurry bed reactor comprises a riser (4), an expansion section (1) at the top of the riser and a downcomer (8), wherein the expansion section (1) is communicated with the upper part of the downcomer (8), the lower part of the riser (4) is communicated with the bottom of the downcomer (8), a slurry phase separator is arranged in the expansion section (1), the slurry phase separator is of a sleeve structure comprising an inner cylinder (3) and an outer cylinder (2), a fluid distributor (7) is arranged at the bottom of the riser (4), a raw material inlet (9) is formed in the bottom of the riser (4), and a material outlet (10) is formed in the top of the expansion section. The slurry bed reactor provided by the invention is suitable for heavy oil hydrogenation process and can realize hydrogenation reaction to separate a light oil product and an unreacted heavy oil product. The slurry bed reactor provided by the invention can also inhibit the generation of coke particles of a heavy oil reaction system and effectively prolong the operation period of the reactor.

Description

A kind of heavy-oil hydrogenation paste state bed reactor and Heavy oil hydrogenation method

Technical field

The present invention relates to a kind of paste state bed reactor and application method thereof, more particularly, relate to and be a kind ofly applicable to the slurry bed circulatory flow reactor of mink cell focus hydrogenation process and a kind of mink cell focus method of hydrotreating.

Background technology

Hydrogenation is a kind of technological line of important inferior raw material process, and by hydrogenation, the impurity such as the metal in heavy oil product, colloid, carbon residue, sulphur, nitrogen all can by effective elimination.The most frequently used in current hydroprocessing processes is down-type fixed-bed reactor, i.e. trickle-bed reactor, but heavy oil product (as residual oil, liquefied coal coil) due to foreign matter content high, easily cause the blocking of hydrogenation catalyst poisoning or catalyzer duct and rapid deactivation, and impurity may block bed to be made pressure drop raise fast to cause reactor operating mode to be deteriorated, even cannot normal running.And the reactor adopting gas and liquid flowing to move upward carries out heavy oil product hydrogenation preferably to select.This type of reactor comprises up-flow reactor, ebullated bed reactor and paste state bed reactor.Also flow at gas-liquid two-phase in the process of flowing, oil product is as external phase, and hydrogen is as disperse phase, both can process the high heavy oil product of foreign matter content, overcomes again fixed bed catalyst bed and holds susceptible to plugging problem.

US4753721 discloses a kind of boiling bed residual oil hydrogenator.Gas and liquid flowing upwards by beds, makes bed create significant expansion.Major part liquid phase is recycled pump again by reactor bottom injecting reactor in reactor head, realizes circulating.Partial Liquid Phase and hydrogen-rich gas are by discharge gate outflow reactor.Because beds expands significantly, be thus less likely to occur the problem of bed blocking.

CN1349554A discloses the up-flow reactor system of a kind of hydrotreating heavy feedstocks band stratiform beds, up-flow reactor contains the catalyst layer of at least two different hydrogenation activities, with selectively removing by the pollutent of whole bed to prevent blocking and to improve catalyst life.Fluid containing heavy feed stock and hydrogen is sent into the bottom of fixed-bed reactor, fluid first with the catalyst exposure in lower horizontal beds, and then with the catalyst exposure in upper level beds, and take out the product after hydrogenation from the top of fixed-bed reactor.For removing most of metal in oil product and solid particle polluter and part sulphur, nitrogen, to extend the work-ing life of hydrogenation catalyst in main reactor.Because gas phase is dispersed into bubble and liquid phase external phase and stream moves upward, makes beds create expansion, bed can be avoided to block.

CN2538416Y discloses a kind of common loop reactor being applicable to heavy-oil slurry hydrocracking.This reactor has two guide shells, the internal diameter of upper guide shell and be highly all greater than lower guide shell.Reactor temperature is evenly distributed, and gas holdup is high, is conducive to the carrying out of reaction process, and without sedimentation of coke, running period is long.

Contrast up-flow reactor and ebullated bed reactor, paste state bed reactor is due to catalyst particle diameter very little (be generally tens microns or less), eliminate the impact of catalyzer internal diffusion, there is very high reaction specific surface and activity, therefore can greatly reduce the consumption of catalyzer.

CN101081357A discloses a kind of slurry bed circulatory flow reactor, comprise upcast and at least one downtake, upcast is connected respectively by pipeline with downtake two ends, described upcast top is the negative area that caliber expands, the top of negative area is provided with venting port, be filtered medium in every root downtake and be divided into filtrate district and slurries district two portions, wherein lower end, filtrate district is communicated with liquid outlet opening, and the two ends in slurries district are connected with the two ends of upcast.This slurry bed circulatory flow reactor is applied to gas-liquid-solid phase reaction system, can realize being continuously separated of gas in slurries, liquid and solid particulate.Because heavy distillate compares thickness, foreign matter content is high, easily blocks, and this slurry bed circulatory flow reactor is not suitable for mink cell focus hydrogenation process.Exploitation is needed a kind ofly to be applicable to the paste state bed reactor of heavy distillate as residual hydrogenation.

Summary of the invention

One of the technical problem to be solved in the present invention is on the basis of existing technology, provides a kind of paste state bed reactor being applicable to heavy-oil hydrogenation.

Two of the technical problem to be solved in the present invention is to provide a kind of Heavy oil hydrogenation method.

A kind of heavy-oil hydrogenation paste state bed reactor, comprise upcast 4, the expanding reach 1 at upcast top and downtake 8, described expanding reach 1 is communicated with the top of downtake 8, described upcast 4 bottom is communicated with bottom downtake 8, arrange slurry phase separator in described expanding reach 1, slurry phase separator is the tube-in-tube structure of inner core 3 and urceolus 2, and described expanding reach top arranges material outlet 10, bottom described upcast 4, fluid distributor 7 is set, bottom described upcast 4, material inlet 9 is set.

The Heavy oil hydrogenation method of confession of the present invention, adopt above-mentioned mink cell focus hydrogenation paste state bed reactor, heavy oil containing hydrocracking catalyst particle and hydrogen are entered the upcast of paste state bed reactor through material inlet by bottom, carry out hydrocracking reaction, reactant flow upwards flows into expanding reach, in expanding reach, slurry flow rate reduces, the material outlet of slurries through expanding reach top being rich in gas draws reactor, all the other slurries flow downward along the annular space between slurry phase separator inner core and urceolus, enter downtake, reenter upcast in the bottom of downtake and continue reaction.

The operation condition of mink cell focus method of hydrotreating provided by the invention is: reaction pressure is 8-30MPa, and temperature of reaction is 350-500 DEG C.

The beneficial effect of mink cell focus hydrogenation paste state bed reactor provided by the invention and mink cell focus method of hydrotreating is:

Compared with being applicable to the reactor of heavy-oil hydrogenation disclosed in prior art, heavy-oil hydrogenation paste state bed reactor structure provided by the invention is simple, the main body circulation that reactant flow is formed in reactor can wash away reactor wall, effectively suppresses deposition and the attachment of solid particulate.The slurry phase separator of reactor head can strengthen being separated of light-end products that hydrogenation reaction obtains and unreacted heavy oil product, and in the light-end products obtained, solid content is low, is convenient to the processing of subsequent process equipment to slurries.Gas phase is discharged by reactor head with slurry is mutually common, and therefore slurry is full of continuously in reactor, without the need to carrying out the Liquid level starching phase, avoiding gas-liquid principal phase interface, liquid level place and easily producing the problem such as system emulsification and solid impurity enrichment.Unreacted heavy oil product mixes with fresh reactant thing bottom reactor upcast, improves the phase solubility of oil product, improves the hydrogenation conversion of heavy oil product, and inhibits coking presoma in oil product to be agglomerated into the possibility of coking particle.Part bubble carried mutually secretly by the slurry flowed in downtake, and during bubble can effectively suppress slurry mutually, coking presoma is agglomerated into coking particle.Adopt slurry bed system heavy oil product hydrogenator provided by the invention can operational cycle of effective extension reactor, suppress the generation of coking particle, can by the discharge gate discharge section slurries of reactor bottom and the solid particulate being deposited on reactor bottom time necessary, with the operational cycle of extension reactor.

Accompanying drawing explanation

Fig. 1 is heavy-oil hydrogenation paste state bed reactor structural representation provided by the invention;

Wherein: 1-expanding reach; 2-starches phase separator urceolus; 3-starches phase separator inner core; 4-upcast; 5-bubble; 6-slurry discharge ports; 7-fluid distributor; 8-downtake; 9-feed(raw material)inlet; 10-material outlet.

Embodiment

Below describe the embodiment of mink cell focus hydrogenation paste state bed reactor provided by the invention and mink cell focus method of hydrotreating in detail, the top mentioned in specification sheets refers to the position of the 90%-100% of container height from the bottom to top; Top refers to the 70%-100% position of container height from the bottom to top, and middle and upper part refers to the 50%-100% position of container height from the bottom to top, and described bottom refers to the 0-30% position of container height from the bottom to top; Described bottom refers to the 0-10% position of container height from the bottom to top.

Paste state bed reactor for mink cell focus hydrogenation provided by the invention is so concrete enforcement:

A kind of heavy-oil hydrogenation slurry bed circulatory flow reactor, comprise upcast 4, the expanding reach 1 at upcast top and downtake 8, described expanding reach 1 is communicated with the top of downtake 8, described upcast 4 bottom is communicated with bottom downtake 8, arrange slurry phase separator in described expanding reach 1, slurry phase separator is the tube-in-tube structure of inner core 3 and urceolus 2, and described expanding reach top arranges material outlet 10, bottom described upcast 4, fluid distributor 7 is set, bottom described upcast 4, material inlet 9 is set.

Preferably, described expanding reach is 1.1 ~ 4 with the diameter ratio of upcast.

Preferably, described upcast diameter is 0.5 ~ 20:1, more preferably 1 ~ 10:1 with downtake diameter ratio.

Preferably, the inner core of described slurry phase separator is 0.01 ~ 0.9:1, more preferably 0.1 ~ 0.7:1 with the diameter ratio of urceolus.

Preferably, the urceolus of described slurry phase separator with the diameter ratio of expanding reach is: 0.4 ~ 0.9:1.

Preferably, the bottom of described upcast arranges slurry discharge ports 6.In use for discharging the catalyzer of inactivation and overweight slurries.

In heavy-oil hydrogenation paste state bed reactor provided by the invention, described material inlet place arranges fluid distributor 4, and fluid distributor is positioned at bottom reactor upcast, the position that the level height of fluid distributor is connected with lower pipe connecting lower than upcast.More preferably, the perforate direction of described fluid distributor down.In use, make bottom upcast, to be subject to stronger fluid flowing and wash away, prevent deposition and the attachment of solid particulate.

In paste state bed reactor provided by the invention, described upcast top is the expanding reach that caliber expands, connected by inverted cone-shaped structure between upcast top and expanding reach, described expanding reach is communicated with downtake top, the inverted conical shape structure place be communicated with bottom the preferred expanding reach in position of described expanding reach and downtake; Described upcast bottom is communicated with downtake bottom, and the position that upcast bottom is communicated with lower pipe connecting is preferably the above 0.5-1.5m place of fluid distributor.In use, described upcast is reaction zone to paste state bed reactor provided by the invention, and described expanding reach and downtake are disengaging zone, and the quantity of wherein said downtake is at least one, can be one or more.

Heavy-oil hydrogenation paste state bed reactor provided by the invention, can be used for residual oil, heavy oil feed that gelatin liquefaction wet goods foreign matter content is high carries out hydrocracking or hydrotreatment.The transformation efficiency of hydrogenation reaction can be improved, suppress mink cell focus reactant to generate coking particle, the operational cycle of effective extension reactor.

Wherein, described mink cell focus hydrogenation paste state bed reactor comprises upcast 4, the expanding reach 1 at upcast top and downtake 8, described expanding reach 1 is communicated with the top of downtake 8, described upcast 4 bottom is communicated with bottom downtake 8, in described expanding reach 1, slurry phase separator is set, slurry phase separator is the tube-in-tube structure of inner core 3 and urceolus 2, described expanding reach top arranges material outlet 10, bottom described upcast 4, fluid distributor 7 is set, bottom described upcast 4, material inlet 9 is set.

In Heavy oil hydrogenation method provided by the invention, the operational condition of described paste state bed reactor is reaction pressure 8-30MPa, preferably 15-25MPa, and temperature of reaction is 350-500 DEG C, is preferably 380-480 DEG C.

In Heavy oil hydrogenation method provided by the invention, described mink cell focus refers to the petroleum hydrocarbon cut of boiling range scope >450 DEG C, is selected from decompressed wax oil, long residuum, vacuum residuum or liquefied coal coil.

In Heavy oil hydrogenation method provided by the invention, described catalyzer is Powdered, the active metal component containing one or more in metal M o, W, V and Ni and heat-resistant inorganic oxide.

Preferably, the grain diameter of described hydrocracking catalyst is 0.5-500 micron.

Heavy oil hydrogenation method provided by the invention, particularly, heavy oil slurries containing catalyzer and hydrogen are as reactant flow after paste state bed reactor mixes outward, and reactant flow, by the material inlet bottom paste state bed reactor upcast, enters in upcast through fluid distributor.Preferably, fluid distributor perforate direction is downward, and reactant flow flowed downward before this and washes away bottom upcast, changes flow direction subsequently and moves upward.Reaction-ure fluid to washing away the deposition that effectively can suppress coking particle bottom upcast, and then suppresses the attachment of coking particle in upcast bottom interior wall.

In paste state bed reactor, the slurries containing granules of catalyst are external phase, hydrogen as disperse phase with the form of bubble and slurry liquid contacts.In upcast, reaction-ure fluid carries out hydrocracking reaction and obtains light-end products in upwards flow process.After reaction-ure fluid reacts in upcast, enter the expanding reach of reactor.Slurry phase separator is provided with in expanding reach.Diameter due to expanding reach is greater than the diameter of reactor upcast, and the movement velocity of slurries in expanding reach declines, and is conducive to the different material of density and carries out settlement separate.Slurry phase separator is provided with inner core and urceolus, should retain certain space (more than 1 millimeter), avoid causing flow dead, cause deposition and the attachment of coking particle between the bottom of inner core and the top of upcast.Inner core tip position and the urceolus tip position of slurry phase separator can adjust according to practical situation, and the top of preferred inner core should lower than the top of urceolus.After reaction-ure fluid enters expanding reach, upwards flow through slurry phase separator inner core.Because the velocity of flow of expanding reach entoplasm phase reduces, continue to move upward by expanding reach top material outlet discharge in inner core top gas and lighter reaction product.And the little slurries of part air content move downward along the annular space between inner core and urceolus.When slurry stream is bottom urceolus, enter downtake, reenter upcast in the bottom of downtake and participate in hydrogenation reaction.

In mink cell focus method of hydrotreating provided by the invention, mink cell focus carries out hydrogenation reaction in reactor upcast, obtains part light-end products.According to the similar principle mixed, the solubleness between light-end products and heavy oil product reduces, and therefore need that the light-end products be obtained by reacting are discharged reactor and carry out following process, and unreacted heavy oil product stays continuation reaction in reactor.In reactor provided by the invention, time the slurries containing a small amount of gas phase flow to bottom urceolus along the annular space between slurry phase separator inner/outer tube, gentle the meeting along the annular space between urceolus and expanding reach inwall of light-end products is upwards flowed.Because the velocity of flow of now slurries is lower, the light-end products be obtained by reacting can be separated more fully with unreacted heavy oil product.And due to settlement action, most of granules of catalyst is present in unreacted heavy oil product.The gentle finally discharge reactor that continues mutually upwards to flow of light-end products containing a small amount of solid particulate carries out subsequent disposal, and the unreacted heavy oil product inflow reactor downtake containing a large amount of solid particulate, finally reenters reactor upcast and react.Because solid content is few in the light-end products of discharge reactor, is easy to processing, reduces the burden of follow-up oil product processing units, extend the operational cycle of device.

In mink cell focus method of hydrotreating provided by the invention, the reactant flow comprising heavy oil, granules of catalyst and hydrogen circulates and forms directed circulation between the upcast and downtake of reactor.Slurries circulation can wash away reactor wall, makes coking particle not easily deposit or be attached on reactor wall, thus extends the operational cycle of reactor.Unreacted heavy oil product through downtake reenter mix with raw feed bottom upcast after continue reaction, according to the similar principle that mixes, intermiscibility between unreacted mink cell focus and the heavy raw oil entering reactor is good, inhibit coking presoma in circulation mink cell focus to reunite and form coking particle, improve the transformation efficiency of heavy-oil hydrogenation, extend the reactor operational cycle.Flow in the slurries of downtake and carried part bubble secretly, this part bubble does not need to carry out further degassed process.Because the coking presoma that can effectively suppress to starch mutually of the hydrogen in bubble is reunited for coking particle, be therefore conducive to the stable operation of paste state bed reactor.

In mink cell focus method of hydrotreating provided by the invention, due to reaction process inevitably generating portion coking particle, and these particles are likely finally deposited on reactor bottom, therefore slurry discharge ports is provided with in the bottom of reactor upcast, can regularly discharge section slurries to reduce the concentration of coking particle in reactor, suppress coking, prolong operation cycle.

Because gas phase and slurries are discharged by reactor head jointly, therefore slurries are being full of whole reactor, without the need to carrying out the Liquid level of slurries, gas-liquid principal phase interface is not had in expanding reach 1, avoid gas-liquid principal phase interface and easily produce the problem such as system emulsification and solid impurity enrichment, be conducive to the operational cycle of extension reactor.

Embodiments of the present invention are illustrated below in conjunction with accompanying drawing, accompanying drawing 1 is the structural representation of heavy-oil hydrogenation paste state bed reactor provided by the invention, as shown in Figure 1, described heavy-oil hydrogenation paste state bed reactor comprises reactor expanding reach 1, upcast 4 and downtake 8, the slurry phase separator comprising slurry phase separator urceolus 2 and slurry phase separator inner core 3 is set in described expanding reach, material inlet 9 is set bottom described upcast, material inlet top arranges fluid distributor 7, and described expanding reach top arranges material outlet 10.Slurry discharge ports 6 is also provided with bottom preferred upcast.Described expanding reach 1 is connected by inverted cone-shaped structure with between upcast 4.

Heavy oil hydrogenation method provided by the invention, hydrogen mixes with the heavy oil slurries containing catalyzer, enters reactor by the material inlet 9 of reactor bottom through fluid distributor 7.Gas slurry reaction mixture first flows downward and washes away the bottom of upcast 4, changes flow direction subsequently and travels up to expanding reach 1 along upcast 4.Diameter due to expanding reach 1 is greater than the diameter of upcast 4, and thus the flow velocity of slurries in expanding reach 1 declines.Space is left, to avoid causing flow dead between the bottom of slurry phase separator inner core 3 and the top of upcast 4.After reactant flow enters expanding reach 1, upwards flow through slurry phase separator inner core 3, the comparatively light sizing liquid containing a large amount of bubble 5 at slurry phase separator inner core 3 top discharges reactor through material outlet 10.The slurries that part air content is low move downward along the annular space between slurry phase separator inner core 3 and urceolus 2, enter downtake 8, reenter upcast 4 participate in hydrogenation reaction in the bottom of downtake 8.Some slurries upwards can flow along the annular space between slurry phase separator urceolus 2 and expanding reach 1 inwall.Due to settlement action, gas and the light-end products be obtained by reacting are in expanding reach top, and gas phase and light-end products are discharged reactor and carried out subsequent disposal.Most of granules of catalyst falls in unreacted heavy oil and flows into downtake 8 simultaneously.

Below the specific embodiment of the present invention is described by reference to the accompanying drawings; but the present invention is not limited to the detail in above-mentioned embodiment; within the scope of technical conceive of the present invention; can carry out multiple simple variant to technical scheme of the present invention, these simple variant all belong to protection scope of the present invention.

Further illustrate implementation method of the present invention by the following examples, but not thereby limiting the invention.

Embodiment 1

Adopt paste state bed reactor as shown in Figure 1, wherein, upcast is 2:1 with the diameter ratio of downtake outer tube, and expanding reach is 2:1 with the diameter ratio of upcast, slurry phase separator urceolus and expanding reach diameter are than being 0.9:1, and slurry phase separator inner core is 0.6:1 with the diameter ratio of the diameter of urceolus.Expanding reach and downtake link position are the inverted cone-shaped structure place of expanding reach bottom, and upcast bottom and decline interface are apart from 2.5m bottom upcast.

Method for preparing catalyst: metallic precursor thing ammonium molybdate ((NH ₄) 6Mo ₇o ₂₄4H ₂o), nickelous nitrate (Ni(NO ₃) ₂6H ₂and vanadium oxide (V O) ₂o ₅) mass ratio be 3.3:4.16:1, be added to the water, stir.Then the vulcanizing agent (sublimed sulphur) through acid-treated gac and 0.34 times adding metal precursor total mass 3.5 times joins in autoclave, 300 DEG C, the first pressing of 7.0Mpa(hydrogen), sulfuration 60min under the condition of high-speed stirring, product after filtration, obtain catalyzer after drying, average particle size is 50 microns, and catalyst property is in table 2.

Heavy oil feed is vacuum residuum, and character is in table 1.Heavy oil containing catalyzer mixes with hydrogen, enters reactor by the material inlet of reactor bottom.In upcast, carry out hydrogenation reaction and upwards flow, because settlement action gas is separated with serum portion in expanding reach, gas and lighter slurries are discharged through material outlet, and the slurries containing a large amount of granules of catalyst enter downtake, continue reaction by returning bottom downtake in upcast.Reaction conditions and products distribution are in table 3.

In the present embodiment, paste state bed reactor form can suppress generation and the deposition of coking particle, and thus the cycle of operation is long, and the hydrogenation conversion of heavy oil product is more than 80%.

Table 1

Analysis project	Residual oil
		Density (20 DEG C)/(g/cm ³）	1.029
W(carbon residue)/%	23.2
		W (element)/%
C	83.87
		H	9.98
S	4.9
		N	0.34
W(metal)/(μ g/g)
		Ni	42
V	96
		Four composition
Saturated point	9.3
		Fragrance point	53.6
Colloid	24.4
		Bituminous matter	12.7
Boiling range/DEG C
		Initial boiling point	470
5%	515
		10%	547
30%	600
		45%	623

Table 2 catalyzer forms

Element	Content/wt%
		Mo	3.2
W	-
		Ni	1.5
V	1.0
		C	84.7
H	0.5
		S	7.6
Amount to	98.5

Table 3

Temperature of reaction/DEG C	420
		Reaction pressure/MPa	10
Reaction times/h	1
		Feed throughput/g	3000
Catalyst charge/%	1
		Product yield/wt%
Gas	7.30
		< 200 DEG C of gasoline	6.50
200 ~ 350 DEG C of diesel oil	32.75
		350 ~ 500 DEG C of wax oils	33.95
> 500 DEG C of residual oil	16.14
		Wherein:
Yield of light oil/%	39.25
		Coke yield/%	3.36

Claims

1. a heavy-oil hydrogenation paste state bed reactor, comprise upcast (4), the expanding reach (1) at upcast top and downtake (8), described expanding reach (1) is communicated with the top of downtake (8), described upcast (4) bottom is communicated with downtake (8) bottom, it is characterized in that, in described expanding reach (1), slurry phase separator is set, slurry phase separator is the tube-in-tube structure of inner core (3) and urceolus (2), described upcast (4) bottom arranges fluid distributor (7), described upcast (4) bottom arranges material inlet (9), described expanding reach top arranges material outlet (10).

2. according to the paste state bed reactor of claim 1, it is characterized in that, described expanding reach is 1.1 ~ 4 with the diameter ratio of upcast.

3. according to the paste state bed reactor of claim 2, it is characterized in that, the perforate direction of described fluid distributor (4) down.

4. according to the paste state bed reactor of claim 1, it is characterized in that, described upcast (1) diameter and downtake (8) diameter ratio are 0.5 ~ 20:1.

5. according to the paste state bed reactor of claim 4, it is characterized in that, described upcast (1) diameter and downtake (8) diameter ratio are 1 ~ 10:1.

6. according to the paste state bed reactor of claim 1, it is characterized in that, the inner core of described slurry phase separator is 0.01 ~ 0.9:1 with the diameter ratio of urceolus.

7. according to the paste state bed reactor of claim 6, it is characterized in that, the inner core of described slurry phase separator is 0.1 ~ 0.7:1 with the diameter ratio of urceolus.

8. according to the paste state bed reactor of claim 1, it is characterized in that, the urceolus of described slurry phase separator with the diameter ratio of expanding reach is: 0.2 ~ 0.95:1.

9. according to the paste state bed reactor of claim 1, it is characterized in that, the bottom of described upcast (1) arranges slurry discharge ports (6).

10. a Heavy oil hydrogenation method, it is characterized in that, adopt the heavy-oil hydrogenation paste state bed reactor in claim 1-9, heavy oil containing hydrocracking catalyst particle and hydrogen are entered the upcast of paste state bed reactor through material inlet by bottom, carry out hydrocracking reaction, reactant flow upwards flows into expanding reach, in expanding reach, slurry flow rate reduces, the material outlet of slurries through expanding reach top being rich in gas discharges reactor, all the other slurries flow downward along the annular space between slurry phase separator inner core and urceolus, enter downtake, and continuation reaction bottom upcast is reentered in the bottom of downtake.

11. according to the method for claim 10, and it is characterized in that, the operational condition of described heavy-oil hydrogenation paste state bed reactor is: reaction pressure 8-30MPa, and temperature of reaction is 350-500 DEG C.

12. according to the method for claim 11, and it is characterized in that, the operational condition of described heavy-oil hydrogenation paste state bed reactor is reaction pressure 15-25MPa, and temperature of reaction is 380-480 DEG C.

13. according to the method for claim 10, and it is characterized in that, described heavy oil is decompressed wax oil, long residuum, vacuum residuum or liquefied coal coil.

14. according to the method for claim 10, and it is characterized in that, described hydrocracking catalyst is the catalyzer of one or more active ingredients in Powdered containing metal Mo, W, V, Ni.

15. according to the method for claim 14, and it is characterized in that, the grain diameter of described hydrocracking catalyst is: 0.5-500 micron.