CN109306272A - Heavy-oil hydrogenation processing system - Google Patents
Heavy-oil hydrogenation processing system Download PDFInfo
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- CN109306272A CN109306272A CN201710627354.2A CN201710627354A CN109306272A CN 109306272 A CN109306272 A CN 109306272A CN 201710627354 A CN201710627354 A CN 201710627354A CN 109306272 A CN109306272 A CN 109306272A
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- processing system
- oil hydrogenation
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- 239000000295 fuel oil Substances 0.000 title claims abstract description 124
- 238000005984 hydrogenation reaction Methods 0.000 title claims abstract description 83
- 239000000463 material Substances 0.000 claims abstract description 132
- 239000001257 hydrogen Substances 0.000 claims abstract description 95
- 229910052739 hydrogen Inorganic materials 0.000 claims abstract description 95
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims abstract description 89
- 238000006243 chemical reaction Methods 0.000 claims abstract description 36
- 238000005336 cracking Methods 0.000 claims abstract description 27
- 150000002431 hydrogen Chemical class 0.000 claims abstract description 8
- 238000002156 mixing Methods 0.000 claims abstract description 6
- 239000007789 gas Substances 0.000 claims description 51
- 239000012528 membrane Substances 0.000 claims description 34
- 230000003014 reinforcing effect Effects 0.000 claims description 25
- 239000002808 molecular sieve Substances 0.000 claims description 16
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 claims description 16
- 239000000919 ceramic Substances 0.000 claims description 10
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims description 10
- 238000005728 strengthening Methods 0.000 claims description 6
- 238000009835 boiling Methods 0.000 claims description 4
- 229910000831 Steel Inorganic materials 0.000 claims description 3
- 239000010959 steel Substances 0.000 claims description 3
- 230000000694 effects Effects 0.000 description 21
- 210000004027 cell Anatomy 0.000 description 15
- 238000000034 method Methods 0.000 description 15
- 210000003934 vacuole Anatomy 0.000 description 10
- 239000012071 phase Substances 0.000 description 8
- 239000010779 crude oil Substances 0.000 description 7
- 238000010586 diagram Methods 0.000 description 6
- 229930195733 hydrocarbon Natural products 0.000 description 6
- 230000009471 action Effects 0.000 description 5
- 239000007791 liquid phase Substances 0.000 description 5
- 238000004519 manufacturing process Methods 0.000 description 5
- 238000004064 recycling Methods 0.000 description 5
- 238000003756 stirring Methods 0.000 description 5
- 229910052799 carbon Inorganic materials 0.000 description 4
- -1 carbon ion Chemical class 0.000 description 4
- 230000008859 change Effects 0.000 description 4
- 238000010276 construction Methods 0.000 description 4
- 150000002430 hydrocarbons Chemical class 0.000 description 4
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical group [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 3
- 239000004215 Carbon black (E152) Substances 0.000 description 3
- 230000008901 benefit Effects 0.000 description 3
- 238000010504 bond cleavage reaction Methods 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- GPRLSGONYQIRFK-UHFFFAOYSA-N hydron Chemical compound [H+] GPRLSGONYQIRFK-UHFFFAOYSA-N 0.000 description 3
- 238000005381 potential energy Methods 0.000 description 3
- 230000008569 process Effects 0.000 description 3
- 230000007017 scission Effects 0.000 description 3
- 230000035939 shock Effects 0.000 description 3
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 2
- MCMNRKCIXSYSNV-UHFFFAOYSA-N Zirconium dioxide Chemical compound O=[Zr]=O MCMNRKCIXSYSNV-UHFFFAOYSA-N 0.000 description 2
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 description 2
- 239000003054 catalyst Substances 0.000 description 2
- 239000008367 deionised water Substances 0.000 description 2
- 229910021641 deionized water Inorganic materials 0.000 description 2
- 230000005684 electric field Effects 0.000 description 2
- 230000002708 enhancing effect Effects 0.000 description 2
- 150000002500 ions Chemical class 0.000 description 2
- 210000000056 organ Anatomy 0.000 description 2
- 238000000926 separation method Methods 0.000 description 2
- 239000007787 solid Substances 0.000 description 2
- 239000012257 stirred material Substances 0.000 description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 2
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- 239000005864 Sulphur Substances 0.000 description 1
- 238000010521 absorption reaction Methods 0.000 description 1
- 230000001133 acceleration Effects 0.000 description 1
- 238000013019 agitation Methods 0.000 description 1
- 150000001336 alkenes Chemical class 0.000 description 1
- 150000004945 aromatic hydrocarbons Chemical class 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 230000000903 blocking effect Effects 0.000 description 1
- 238000003763 carbonization Methods 0.000 description 1
- 230000003197 catalytic effect Effects 0.000 description 1
- 238000004517 catalytic hydrocracking Methods 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 230000006835 compression Effects 0.000 description 1
- 238000007906 compression Methods 0.000 description 1
- 230000009514 concussion Effects 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 229910052593 corundum Inorganic materials 0.000 description 1
- 230000007423 decrease Effects 0.000 description 1
- 238000002224 dissection Methods 0.000 description 1
- 238000004821 distillation Methods 0.000 description 1
- 238000009826 distribution Methods 0.000 description 1
- 230000009977 dual effect Effects 0.000 description 1
- 230000005611 electricity Effects 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 238000007701 flash-distillation Methods 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 230000004907 flux Effects 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 238000001727 in vivo Methods 0.000 description 1
- 238000009413 insulation Methods 0.000 description 1
- 239000002184 metal Substances 0.000 description 1
- 229910044991 metal oxide Inorganic materials 0.000 description 1
- 150000004706 metal oxides Chemical class 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 239000003921 oil Substances 0.000 description 1
- 239000011224 oxide ceramic Substances 0.000 description 1
- 229910052573 porcelain Inorganic materials 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 230000008439 repair process Effects 0.000 description 1
- 229930195734 saturated hydrocarbon Natural products 0.000 description 1
- 239000000377 silicon dioxide Substances 0.000 description 1
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- 239000000126 substance Substances 0.000 description 1
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Classifications
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G47/00—Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen- generating compounds, to obtain lower boiling fractions
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J19/08—Processes employing the direct application of electric or wave energy, or particle radiation; Apparatus therefor
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J19/18—Stationary reactors having moving elements inside
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G67/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only
- C10G67/02—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J2219/08—Processes employing the direct application of electric or wave energy, or particle radiation; Apparatus therefor
- B01J2219/0894—Processes carried out in the presence of a plasma
Abstract
The present invention provides a kind of heavy-oil hydrogenation processing systems, the heavy-oil hydrogenation processing system includes main reactor and at least one sub- reactor, main reactor includes the first cylinder, first cylinder is for holding material, sub- reactor includes: mixed cell, and for mixing material and hydrogen, mixed cell includes the second cylinder, material inlet, hydrogen inlet and first outlet, the outlet of material inlet and the first cylinder are provided on second cylinder；Intensifying device, the entrance of intensifying device are connected to the first outlet of the second cylinder, and the outlet of intensifying device is connected to the accommodating chamber of the first cylinder, and intensifying device is used to provide energy to material so that cracking reaction occurs for material.The technical solution provided through the invention is able to solve heavy-oil hydrogenation processing system operating cost height in the prior art and the high problem of cost of investment.
Description
Technical field
The present invention relates to technical field of petrochemical industry, in particular to a kind of heavy-oil hydrogenation processing system.
Background technique
Heavy oil is crude oil part remaining after extracting distillate.Heavy oil and crude oil ratio, complicated component, density is big,
Viscosity is high, average molecular weight is big, hydrogen-carbon ratio is low, carbon residue is high, and contains the harmful substances such as a large amount of metal, sulphur, nitrogen.From abundant
From the point of view of the energy or protection environment, need to handle heavy oil.
Crude oil is divided into light crude oil and heavy crude, and with the intensification of oil exploitation degree, the component for producing crude oil is more next
Heavier, the phenomenon that crude oil heaviness, in poor quality, is more and more prominent, i.e. the ratio of heavy crude is higher and higher.The processing of heavy oil compared with
For difficulty, after especially being processed to heavy crude, the amount of the heavy oil of generation may account for the half of heavy crude total amount with
On, and the content of the saturated hydrocarbons of heavy oil is lower, and subsequent processing is more difficult.
It mainly include two class technology of carbonization treatment technique and hydroprocessing technique when handling heavy oil.In order to mention
Height can use hydroprocessing technique to the utilization rate of heavy oil.Hydroprocessing technique is that hydrogen is added in heavy oil, certain
Under the action of temperature, pressure and catalyst, hydrogen ion and carbon ion are combined, and make alkene even aromatic hydrocarbons saturation, to reach lighting
Purpose.The existing heavy-oil hydrogenation processing system using hydroprocessing technique need to be run under conditions of high temperature and pressure, and
It is big to the consumption of hydrogen, to keep the operating cost of heavy-oil hydrogenation processing system high.Moreover, because needing in high temperature and pressure
Under the conditions of run, it is high to the performance requirement of system so that structure is complicated for system, to make the investment of heavy-oil hydrogenation processing system
It is at high cost.
Summary of the invention
The present invention provides a kind of heavy-oil hydrogenation processing system, to solve heavy-oil hydrogenation processing system operation in the prior art
The at high cost and high problem of cost of investment.
To solve the above-mentioned problems, the present invention provides a kind of heavy-oil hydrogenation processing system, the heavy-oil hydrogenation processing systems
Including main reactor and at least one sub- reactor, main reactor includes the first cylinder, and sub- reactor includes: mixed cell, is used
It is mixed in by material and hydrogen, mixed cell includes the second cylinder, and material inlet, hydrogen inlet and the are provided on the second cylinder
One outlet, the outlet of material inlet and the first cylinder；Intensifying device, the entrance of intensifying device go out with the first of the second cylinder
Mouth connection, the outlet of intensifying device are connected to the accommodating chamber of the first cylinder, and intensifying device is used to provide energy so that object to material
Cracking reaction occurs for material.
Further, intensifying device includes strengthening unit, and reinforcing unit is plasma unit, cavitation unit, stirring list
One of member and crash unit are a variety of, and for carrying out ionization processing to material, cavitation unit is used for plasma unit
Material is set to generate cavitation, agitating unit is for being stirred material, and crash unit will be for that will enter the appearance of the first cylinder
The material of chamber received is hit.
Further, intensifying device includes multiple reinforcing units, and each reinforcing unit is plasma unit, cavitation list
One of member, agitating unit and crash unit, when it is one of to strengthen unit be crash unit when, the outlet of crash unit with
The accommodating chamber of first cylinder is connected to, and the first outlet of the second cylinder, other reinforcing units are sequentially connected to crash unit.
Further, intensifying device includes multiple reinforcing units, and each reinforcing unit is plasma unit, cavitation unit
One of with agitating unit, the first outlet of the second cylinder multiple strengthens unit and the accommodating chamber of the first cylinder is sequentially connected to.
Further, plasma unit includes: third cylinder, has the first barrel and the second barrel, and the first barrel is set
Set has the first cavity between the inside of the second barrel, the first barrel and the second barrel, has the second cavity in the first barrel,
Material can flow in the first cavity；Dielectric is arranged in the second cavity；Electrode at least partially penetrates in dielectric, electricity
One end of pole connects high voltage power supply.
Further, cavitation unit includes: the 4th cylinder；Cavitation board group is arranged in the 4th cylinder；And/or cavitation
Mouth is arranged in the 4th cylinder.
Further, cavitation unit includes cavitation board group, and cavitation board group includes: the first plate body, is provided on the first plate body
Multiple through-holes；Second plate body is provided with multiple through-holes on the second plate body, has angle between the second plate body and the first plate body.
Further, at least partly the periphery of the first plate body is zigzag, and/or the periphery of at least partly the second plate body is
Zigzag.
Further, cavitation board group is multiple, and multiple cavitation board groups are sequentially arranged along the flow direction of material at the 4th
In vivo.
Further, agitating unit includes: the 5th cylinder；Shaft is rotatably arranged in the 5th cylinder, the axis of shaft
It is arranged to along the flow direction of material；Multiple blades, multiple blades are arranged at intervals in shaft along the circumferencial direction of shaft.
Further, agitating unit further include: multiple arcs baffle, be fixed at the 5th cylinder and multiple blades it
Between, multiple arcs baffle is arranged along the circumferencial direction interval of shaft.
Further, the top of the accommodating chamber of the first cylinder is arranged in crash unit, and crash unit includes: bracket, fixed
On the inner sidewall of the first cylinder；Delivery pipe is fixed on bracket, and the first outlet of the entrance of delivery pipe and the second cylinder connects
It is logical.
Further, the intensifying device of sub- reactor includes crash unit, and the first of crash unit entrance and the second cylinder
The outlet of outlet, crash unit is connected to the accommodating chamber of the first cylinder；Sub- reactor at least two, at least two sons are anti-
The outlet interval of the crash unit of device is answered to be arranged, the material for entering the first cylinder from different crash units is hit.
Further, the cross-sectional area of the inner wall of the second cylinder is greater than the cross-sectional area of the inner wall of first outlet, the
Two cylinders are made of steel pipe.
Further, mixed cell further include: gas distributor is arranged in the second cylinder, gas distributor and hydrogen
Entrance connection, gas distributor is for hydrogen to be evenly distributed in material.
Further, gas distributor includes: ontology, and ontology has entrance and exit, the entrance of ontology and the second cylinder
Hydrogen inlet connection；Inoranic membrane is arranged in the outlet of ontology, and inoranic membrane has multiple through-holes, it is preferable that inoranic membrane is pottery
Porcelain film, it is highly preferred that the diameter of the through-hole of ceramic membrane is between 0.3 μm to 1.0 μm.
Further, gas distributor further include: molecular sieve, molecular sieve are attached on inoranic membrane, it is preferable that molecular sieve is
FAU type molecular sieve, it is highly preferred that the thickness of FAU type molecular sieve is less than 1.0 μm.
Further, sub- reactor further include: the pump housing is arranged between the outlet of the first cylinder and the outlet of intensifying device
Pipeline on, the pump housing is for conveying material.
Further, heavy-oil hydrogenation processing system further include: hydrogen supply device, the hydrogen outlet of hydrogen supply device and the second cylinder
Hydrogen inlet connection, hydrogen supply device provide hydrogen purity be A, wherein A >=20%.
Further, hydrogen supply device prepares hydrogen by methane cracking.
Further, heavy-oil hydrogenation processing system further include: rectifying column, rectifying column are used for the gas-phase product of material by boiling
Point range separation, the gas-phase product outlet of the entrance of rectifying column and the first cylinder；At the top of rectifying column fixed gas outlet with
Fixed gas outlet at the top of the entrance connection of hydrogen supply device or rectifying column is connected to the hydrogen inlet of the second cylinder.
Further, the pressure in heavy-oil hydrogenation processing system is less than 0.1MPa.
Further, in heavy-oil hydrogenation processing system the reaction temperature of material between 350 DEG C to 410 DEG C.
It applies the technical scheme of the present invention, is provided with mixed cell and intensifying device in heavy-oil hydrogenation processing system, by
In intensifying device energy can be provided to heavy oil and the mixed material of hydrogen so that cracking reaction, therefore the heavy oil occur for material
Hydrotreating systems do not need higher pressure and temperature, do not need higher hydrogen consumption yet, so that it may use hydrotreating
Technique is handled to heavy oil, so as to reduce the operating cost of heavy-oil hydrogenation processing system.The heavy-oil hydrogenation processing system
System can be run under normal pressure and lower temperature, be reduced to the performance requirement of system, therefore can simplify the structure of system, thus
It can reduce the cost of investment of heavy-oil hydrogenation processing system.
Detailed description of the invention
The accompanying drawings constituting a part of this application is used to provide further understanding of the present invention, and of the invention shows
Examples and descriptions thereof are used to explain the present invention for meaning property, does not constitute improper limitations of the present invention.In the accompanying drawings:
Fig. 1 shows the structural schematic diagram of heavy-oil hydrogenation processing system provided by the invention；
Fig. 2 shows the top views of the heavy-oil hydrogenation processing system in Fig. 1；
Fig. 3 shows the structural schematic diagram of the mixed cell in heavy-oil hydrogenation processing system；
Fig. 4 shows the structural schematic diagram of the plasma unit in heavy-oil hydrogenation processing system；
Fig. 5 shows the structural schematic diagram of the cavitation unit in heavy-oil hydrogenation processing system；
Fig. 6 shows the structural schematic diagram of the agitating unit in heavy-oil hydrogenation processing system；
Fig. 7 shows the structural schematic diagram of the crash unit in heavy-oil hydrogenation processing system.
Wherein, the above drawings include the following reference numerals:
10, mixed cell；11, the second cylinder；12, gas distributor；20, plasma unit；21, third cylinder；22,
Dielectric；23, electrode；30, cavitation unit；31, cavitation board group；31a, the first plate body；31b, the second plate body；40, agitating unit；
41, shaft；42, blade；43, curved baffle；50, crash unit；51, bracket；52, delivery pipe；60, the pump housing；100, sub- reaction
Device；200, main reactor；210, the first cylinder.
Specific embodiment
Following will be combined with the drawings in the embodiments of the present invention, and technical solution in the embodiment of the present invention carries out clear, complete
Site preparation description.Obviously, described embodiments are only a part of the embodiments of the present invention, instead of all the embodiments.Below
Description only actually at least one exemplary embodiment be it is illustrative, never as to the present invention and its application or make
Any restrictions.Based on the embodiments of the present invention, those of ordinary skill in the art are not making creative work premise
Under every other embodiment obtained, shall fall within the protection scope of the present invention.
As shown in Figures 1 to 7, the embodiment provides a kind of heavy-oil hydrogenation processing system, at the heavy-oil hydrogenation
Reason system includes main reactor 200 and sub- reactor 100.Wherein, main reactor 200 includes the first cylinder 210, and material can add
Enter in the first cylinder 210 or be discharged from the first cylinder 210, material can also react in the first cylinder 210.It is sub anti-
Answering device 100 includes mixed cell 10 and intensifying device.Wherein, mixed cell 10 is used to mix material and hydrogen.Such as Fig. 3 institute
Show, mixed cell 10 includes the second cylinder 11, is provided with material inlet, hydrogen inlet and first outlet, object on the second cylinder 11
Expect the outlet of entrance and the first cylinder 210.The entrance of intensifying device is connected to the first outlet of the second cylinder 11, strengthens dress
The outlet set is connected to the accommodating chamber of the first cylinder 210.
Intensifying device is used to provide energy to material so that cracking reaction occurs for material.The energy that intensifying device provides can make
Hydrocarbon molecules and hydrogen molecule in material obtain enough external energies, and under the effect of the catalyst, hydrocarbon molecules are especially more
The molecular link of cycloaromatics, which is cut off, generates hydro carbons ion, and the hydrogen bond of hydrogen molecule is cut off and generates hydrogen ion.Hydro carbons ion and
Hydrogen ion, which combines, forms new compound, completes cracking reaction.The program can replace original by the effect of intensifying device
The scheme that material can just react at high temperature under high pressure.
It applies the technical scheme of the present invention, since intensifying device can provide energy to heavy oil and the mixed material of hydrogen
So that cracking reaction occurs for material, therefore the heavy-oil hydrogenation processing system does not need higher pressure and temperature, do not need yet compared with
High hydrogen consumption, so that it may be handled using hydroprocessing technique to heavy oil, so as to reduce heavy-oil hydrogenation processing
The operating cost of system.Also, since the heavy-oil hydrogenation processing system can be run under normal pressure and lower temperature, to system
Performance requirement reduces, therefore can simplify the structure of system, so as to reduce the cost of investment of heavy-oil hydrogenation processing system.
Specifically, intensifying device includes strengthening unit, and reinforcing unit is plasma unit 20, cavitation unit 30, stirring
One of unit 40 and crash unit 50 are a variety of.Plasma unit 20 is for carrying out ionization processing, cavitation to material
Unit 30 is for making material generate cavitation, and agitating unit 40 is for being stirred material, and crash unit 50 is for will be into
The material for entering the accommodating chamber of the first cylinder 210 is hit.By setting intensifying device to strengthen unit, and strengthen unit
Type can be selected, suitable intensifying device can be set according to production needs, to provide for mixed material
Enough energy, so that cracking reaction occurs for material.Moreover, selectively setting intensifying device can enhance heavy-oil hydrogenation processing
The scope of application of system.Intensifying device can be set to plasma unit 20, cavitation unit 30, agitating unit 40 and hit single
Member 50 in any one, it is two kinds any, it is any three kinds or all four kinds.A variety of reinforcing units can be used in parallel or series
Mode connects, can also be simultaneously by the way of in parallel or series.When reducing the type of the reinforcing unit in intensifying device, energy
The manufacturing cost for enough reducing device can be improved the reaction effect of system when increasing the type of the reinforcing unit in intensifying device
Rate.In actual production, it should accomplish the balance of cost and efficiency according to different situations.
A kind of reinforcing unit can be only included in intensifying device, in such cases the first outlet of the second cylinder 11, this is strong
Change unit and the first smoothly connection of cylinder 210.For example, intensifying device only includes crash unit 50, the first of the second cylinder 11 goes out
Mouth, crash unit 50 are sequentially connected to the first cylinder 210.Intensifying device may include multiple reinforcing units, and one of them
When reinforcing unit is crash unit 50, the outlet of crash unit 50 is connected to the accommodating chamber of the first cylinder 210, the second cylinder 11
First outlet, other reinforcing units are sequentially connected to crash unit 50.When including crash unit 50 i.e. in group reactor, hit
The rear end in Flow of Goods and Materials direction is arranged in unit 50.After heavy oil and hydrogen mix in the second cylinder 11, sequentially enter multiple strong
Change in unit, energy is successively provided by multiple effects for strengthening unit, so that material be made sufficiently to react.
In this application, intensifying device may include multiple reinforcing units, each reinforcing unit be plasma unit 20,
One of cavitation unit 30 and agitating unit 40.Intensifying device does not include crash unit 50, the second cylinder 11 in such cases
First outlet, multiple accommodating chambers for strengthening unit and the first cylinder 210 are sequentially connected to.Heavy oil and hydrogen are in the second cylinder 11
After mixing, sequentially enter in multiple reinforcing units, energy is successively provided by multiple effects for strengthening unit, so that material be made to fill
Divide reaction.
As shown in figure 4, plasma unit 20 includes third cylinder 21, dielectric 22 and electrode 23.Wherein, third cylinder
21 have the first barrel and the second barrel, and the inside of the second barrel is arranged in the first barrel.And the first barrel and the second barrel
Between there is the first cavity, there is the second cavity, material can flow in the first cavity in the first barrel.The setting of dielectric 22 exists
In second cavity.Electrode 23 at least partially penetrates in dielectric 22, and one end of electrode 23 connects high voltage power supply.So set
It sets, the electrode 23 for inputting high voltage power supply generates high voltage electric field, blocking decentralization electric forming etc. of the high voltage electric field in insulation dielectric 22
Gas ions (DBD Plasma), so that material is dissociated into ion, so that cracking reaction occurs for material.
In the present embodiment, cavitation unit 30 includes the 4th cylinder, and material can flow in the 4th cylinder.Cavitation unit 30
It further include one or both of cavitation board group 31 and cavitation mouth.Cavitation mouth can be set to Venturi tube (Venturi
Tube), one of organ pipe (Organ Tube) and last of the twelve Earthly Branches nurse hertz pipe (Helmholtz Tube) or a variety of.Work as cavitation unit
30 include cavitation board group 31 when, cavitation board group 31 be arranged in the 4th cylinder；When cavitation unit 30 includes cavitation mouth, cavitation mouth
It is also disposed in the 4th cylinder.In cavitation unit 30, the material of flowing under cavitation board group 31 or the dissection of cavitation mouth,
Cavitation effect can occur.Cavitation effect can provide energy for material, to make the molecular scission of material, it is anti-that cracking occurs
It answers.
Vacuole can be generated in the region that cavitation effect occurs, vacuole can undergo the process of formation and collapse.The collapse of vacuole
The temperature of gas phase zone can be made to reach 5200K or so, the temperature of liquid phase region can be made to reach 1900K or so, and local pressure can
Reach 50.5MPa, rate of temperature change can reach 109K/s.Also with strong shock wave and speed while vacuole collapse
The microjet of 110m/s can be reached.By cavitation effect in the high energy locally generated, it is sufficient to include condensed ring virtue in cracking material
Molecular link including hydrocarbon, to make material that adequately reaction occur.
As shown in figure 5, cavitation board group 31 includes the first plate body 31a and the second plate body 31b, the first plate body 31a and the second plate
Body 31b is fixed in the 4th cylinder.Wherein, multiple through-holes are provided on the first plate body 31a, on the second plate body 31b
Multiple through-holes are provided with, there is angle between the second plate body 31b and the first plate body 31a.Such setting is capable of increasing cavitation board group
31 with flow through the contact area of the 4th intracorporal material, and being capable of strength imparting material and the first plate body 31a and the second plate body 31b
Impact, so as to generate stronger cavitation effect.Cavitation effect enhancing can provide higher energy for material, thus plus
The cracking reaction efficiency of fast material.
Further, in the present embodiment, zigzag can be set by the periphery of at least partly the first plate body 31a,
Zigzag can be set by the periphery of at least partly the second plate body 31b, it can also be by at least partly periphery of the first plate body 31a
The periphery of at least partly the second plate body 31b is disposed as zigzag.So set, can be by the effect of zigzag structure
One step increases the contact area of material and cavitation board group 31, and further strengthens the impact of material Yu cavitation board group 31, thus
Generate stronger cavitation effect.Cavitation effect enhancing can provide higher energy for material, so that the cracking for accelerating material is anti-
Answer efficiency.
In the present embodiment, it can also set multiple for cavitation board group 31, flowing of multiple cavitation board groups 31 along material
Direction is sequentially arranged in the 4th cylinder.The complete material of unreacted can pass through next in this way after a cavitation board group 31
Cavitation board group 31 continues to generate cavitation effect and react.Therefore, multiple cavitation board groups 31 can promote the cracking of material anti-
It answers.
As shown in fig. 6, agitating unit 40 includes the 5th cylinder, shaft 41 and multiple blades 42.Wherein, material can be
The flowing of five cylinders.Shaft 41 is rotatably arranged in the 5th cylinder, and the flow direction axially along material of shaft 41 is set
It sets.Multiple blades 42 are arranged at intervals in shaft 41 along the circumferencial direction of shaft 41.Material is when flowing through five cylinders, multiple paddles
Leaf 42 rotates in the 5th cylinder, and blade 42 not only can make the material of heterogeneity or different shape abundant the agitation of material
Mixing, additionally it is possible to energy is provided for material, to make material that cracking reaction occur.
Specifically, by the stirring action of blade 42, gas-liquid-solid three-phase material is enabled to be sufficiently mixed and contact, and
Hydrogen and heavy oil can be made to be sufficiently mixed and contact, to enhance the transmitting of material.Moreover, pass through the stirring action of blade 42,
Cavitation effect can occur for material.Specifically, when blade 42 rotates, the material at 42 rear portion of blade tails off, 42 rear portion of blade pressure
Power is lower, and small lighter hydrocarbons bubble or bubble hydrogen can become larger in low-pressure state in material, forms cavity flow (Cavitating
Flow) region.When next blade 42 moves to the moment in cavity flow region, blade 42 generates compression to vacuole, keeps vacuole broken
It splits.High temperature and pressure can be generated when cavity collapse, high temperature and pressure makes material that cracking reaction occur.
Further, agitating unit 40 further includes multiple arcs baffle 43, and multiple arcs baffle 43 is fixed at the 5th
Between cylinder and multiple blades 42, and multiple arcs baffle 43 is arranged along the circumferencial direction interval of shaft 41.Multiple blades 42
It is mobile from shaft 41 to the direction of the 5th cylinder inboard wall to will drive material when stirring to material, due to the resistance of curved baffle 43
Gear effect, between material can be concentrated through between the gap between blade 42 and curved baffle 43 and adjacent curved baffle 43
Gap.When passing through gap, blade 42 or curved baffle 43 can generate shear action to material, and shear action facilitates in heavy oil
The cracking of macromolecular, open loop are simultaneously reacted.Therefore, the reaction efficiency of material can be enhanced by the way that curved baffle 43 is arranged.
As shown in Figure 1 and Figure 7, the top of the accommodating chamber of the first cylinder 210 is arranged in crash unit 50.Crash unit 50 is wrapped
Include bracket 51 and delivery pipe 52.Wherein, bracket 51 is fixed on the inner sidewall of the first cylinder 210；Delivery pipe 52 is fixed on bracket
On 51, bracket 51 can play a supportive role to delivery pipe 52.And the first outlet of the entrance of delivery pipe 52 and the second cylinder 11
The object of unit is strengthened in connection from the material directly exported in the second cylinder 11 or after exporting in the second cylinder 11 using other
Material enters the accommodating chamber of the first cylinder 210 by delivery pipe 52.Material enters accommodating chamber from delivery pipe 52 with certain speed,
When entering accommodating chamber, between material and material or the inner sidewall of material and the first cylinder 210 is hit.In the moment of shock
The kinetic energy of material is converted to the potential energy and thermal energy of fluid molecule level, to make material acquisition can be by the high energy of molecular scission
It measures, further occurrence cracking reaction after the molecular scission of material.Therefore the effect for passing through crash unit 50, can promote material
Reaction, to reinforce processing and recycling to heavy oil.
Moreover, the top of the heavy oil in the accommodating chamber of the first cylinder 210 is arranged in crash unit 50, occur in this way in material
During shock, additionally it is possible to accelerate the flash distillation of material, it is product evaporated after material reaction so as to make, be conducive in this way pair
The separation and recycling of product, to improve the treatment effect to heavy oil.
In the present embodiment, the intensifying device of sub- reactor 100 includes crash unit 50,50 entrance of crash unit and second
The first outlet of cylinder 11 is connected to, and the outlet of crash unit 50 is connected to the accommodating chamber of the first cylinder 210.Sub- reactor 100 to
It is less two, the outlet interval of the crash unit 50 of at least two sub- reactors 100 is arranged.So set, can make never same
The material that crash unit 50 enters the first cylinder 210 is mutually hit.Material in different crash units 50 all has certain speed
Degree, they, which mutually hit, can strengthen knockout process, to make the kinetic energy of material more be converted to potential energy and thermal energy, to promote
The reaction of material.
Specifically, as shown in fig. 7, material in crash unit 50 is conveyed by delivery pipe 52, two delivery pipes 52 go out
Mouth face is arranged, and the Flow of Goods and Materials in two such delivery pipe 52 is contrary, and material occurs just over the ground after outlet outflow
It hits, so that the kinetic energy of material is more converted to potential energy and thermal energy, further to promote the reaction of material.Optionally, difference is hit
The bracket 51 hit in unit 50 can be connected with each other, and to increase the structural strength of device, improve the service life of crash unit 50.
In order to guarantee impact effects, in the present embodiment, flow velocity of the material in delivery pipe 52 can be set to 20-50m/s.
As shown in figure 3, the cross-sectional area of the inner wall of the second cylinder 11 is greater than the cross-sectional area of the inner wall of first outlet,
Higher pressure can be kept when being passed through heavy oil and hydrogen in the accommodating chamber of such second cylinder 11, in favor of heavy oil and hydrogen
Mixing, and the reaction of heavy oil and hydrogen can be promoted.Due to being provided with intensifying device, system in the heavy-oil hydrogenation processing system
It can run, the performance requirement of the second cylinder 11 be reduced, therefore can simplify the second cylinder 11 under lower pressure and temperature
Structure, to reduce the cost of investment of heavy-oil hydrogenation processing system.Specifically, the second cylinder 11 can be made of steel pipe, this
Compared with using special pressure vessel, the cost of investment of heavy-oil hydrogenation processing system can be reduced significantly.
In the present embodiment, mixed cell 10 further includes gas distributor 12, and gas distributor 12 is arranged in the second cylinder
In 11, gas distributor 12 is connected to hydrogen inlet, and gas distributor 12 is for hydrogen to be evenly distributed in heavy oil.By setting
Gas distributor 12 is set, the hydrogen entered in the second cylinder 11 can will be concentrated to be distributed to the different location in the second cylinder 11,
To increase the contact area of hydrogen and heavy oil, so that hydrogen be made uniformly to mix with heavy oil, be conducive to subsequent reactions in this way.
In order to reach preferable gas distributed effect, permeable membrane can be set in gas distributor 12.Meanwhile in order to suitable
The working environment of high temperature and liquid phase large disturbances is answered, inoranic membrane can be set by permeable membrane.Since inoranic membrane has intensity high, hot
The advantages that stability is good, corrosion-resistant, easy cleaning, so that inoranic membrane can satisfy requirement.
Specifically, gas distributor 12 includes ontology and inoranic membrane.Wherein, ontology has interconnected entrance and goes out
Mouthful, the entrance of ontology is connected to the hydrogen inlet of the second cylinder 11.Inoranic membrane is arranged in the outlet of ontology, and inoranic membrane has more
A through-hole.So set, hydrogen is dispersed into second from different location by multiple through-holes on inoranic membrane after entering ontology
In cylinder 11, to uniformly be mixed with the heavy oil of different location.
In the heavy-oil hydrogenation processing system, do not need that cracking reaction can occur with the higher hydrogen of purity, therefore
It can be using the few gas of hydrogeneous tolerance as hydrogen source, to reduce the operating cost of system.For example, can will be after methane cracking
Gas as hydrogen source, the hydrogen-containing gas that can also be obtained using other approach.Other can be contained in the few gas of hydrogen
Gas, such as CO, CO2、CH4Or liquefied gas or the vapor such as carbon 2, carbon 3.The size of some of gas molecules is larger, therefore
When selecting inoranic membrane, the inoranic membrane of the biggish no filterability of clear size of opening should be used, so that gas passes through.
In the present embodiment, ceramic membrane can be set by inoranic membrane.Ceramic membrane should have intensity height, thermal stability
The feature good, pore-size distribution is single, flux decline is small.For example, can choose with metal oxide ceramic Al2O3Or ZrO2
For the ceramic membrane of skeleton.Preferably, the diameter of the through-hole of the ceramic membrane in the present embodiment is arranged between 0.3 μm to 1.0 μm, this
Sample can make the biggish deionized water of molecular dimension pass through through-hole.Can be by the ceramic membrane of deionized water, it can also be without selection
Ground allows gas to pass through and present small vapour lock state, so that gas is smoothly through ceramic membrane and mixes with heavy oil.
Optionally, gas distributor 12 further includes molecular sieve, and molecular sieve is attached on inoranic membrane.By the way that molecular sieve is arranged,
Can suitably constrain the aperture of inoranic membrane, this aspect helps to stablize the air pressure for entering liquid phase, on the other hand make hydrogen and its
Its gas rapidly enters liquid phase with certain acceleration and more small bubble.Preferably, thickness can be adhered on ceramic membrane
Spend the FAU type molecular sieve less than 1.0 μm.
Gas distributor 12 has dual function: on the one hand hydrogen can be allowed with pole by setting inoranic membrane and molecular sieve
Small bubble enters in heavy oil, and the vacuole generated in longitudinal wave concussion with heavy oil is arranged side by side or merges, and makes in vacuole or vacuole is attached
It is closely full of hydrogen, completes hydrocracking process in the moment of vacuole collapse；On the other hand inoranic membrane surface layer and heavy oil can be adjusted
The silica alumina ratio of the molecular sieve of contact enables gas distributor 12 to play catalytic action to cracking reaction.It is arranged such both advantageous
It is mixed in hydrogen with the uniform of heavy oil, and is conducive to the cracking reaction of hydrogen and heavy oil.
In the present embodiment, sub- reactor 100 further includes the pump housing 60, the pump housing 60 be arranged in the outlet of the first cylinder 210 with
On pipeline between the outlet of intensifying device, the pump housing 60 is for conveying material.Material can be guaranteed in son by the way that the pump housing 60 is arranged
The flowing between flowing and sub- reactor 100 and main reactor 200 inside reactor 100.As shown in Figure 1, can will pump
Body 60 is arranged between the first cylinder 210 and mixed cell 10, the pump housing 60 can also be arranged in mixed cell 10 and strengthen dress
Between setting, the pump housing 60 can also be arranged in the inside of intensifying device.According to production needs, it can set more for the pump housing 60
It is a.
By the way that the pump housing 60 is arranged, the Matter Transfer in sub- reactor 100 and main reactor 200 can be made to flow, so as to be
Material in system sufficiently reacts.Material, can be in the first cylinder 210 by the product after reaction after through sub- reactor 100
It separates, unreacted material flows into the bottom of the first cylinder 210, and then the pump housing 60 can be by 210 bottom of the first cylinder
Material is again fed in sub- reactor 100 that the reaction was continued.Heavy oil can be made sufficiently to react in this way, to improve the place to heavy oil
Manage efficiency and utilization rate.In the present embodiment, residence time of the material heavy oil in heavy-oil hydrogenation processing system was at 30 minutes
To between 90 minutes, average out to 60 minutes, to reach the balance for the treatment of effeciency and utilization rate, to make maximization of economic benefit.
It is of course also possible to need to set other numerical value for the residence time of material according to technique.
Under conditions of technique is constant, the height of conversion rate of products and the quality of heavy oil are closely related.For example, for heavy
The heavy oil of crude oil, using the technical solution of the present embodiment, the utilization rate that the end point of distillation is 500 DEG C has preferable in 70-90%
Economic indicator.
Further, heavy-oil hydrogenation processing system further includes hydrogen supply device, the hydrogen outlet of hydrogen supply device and the second cylinder
11 hydrogen inlet connection, hydrogen supply device are used to provide hydrogen for mixed cell 10.In the heavy-oil hydrogenation processing system, it is not required to
Can occur cracking reaction with the higher hydrogen of purity, thus can using the few gas of hydrogeneous tolerance as hydrogen source,
To reduce the operating cost of system.The purity for the hydrogen that hydrogen supply device provides, which is greater than or equal to 20%, just can satisfy the anti-of heavy oil
Answer demand.The gas for using hydrogeneous tolerance few can reduce the cost of the raw material of production hydrogen as hydrogen source, therefore can show
Write the operating cost of reduction system.
The hydrogen-consuming volume of existing heavy-oil hydrogenation processing system is in 150NM3/M3To 300NM3/M3Between can run, and
The hydrogen-consuming volume of the heavy-oil hydrogenation processing system of the present embodiment is less than or equal to 50NM3/M3It can run, therefore at the heavy-oil hydrogenation
Reason system can significantly reduce hydrogen-consuming volume, to reduce the operating cost of system.
Specifically, hydrogen supply device can be prepared hydrogen by methane cracking, can either meet system in this way to the purity of hydrogen
It is required that and can reduce cost of material.Include other gases in the gas generated after methane cracking system, is not had to using the system
These gases are separated, can be transported to together in mixed cell 10.
In the present embodiment, heavy-oil hydrogenation processing system further includes rectifying column, and rectifying column is used for the gas-phase product of material
It is separated by boiling spread.The gas-phase product outlet of the entrance of rectifying column and the first cylinder 210, the fixed gas at the top of rectifying column
Outlet is connected to the entrance of hydrogen supply device.Or rectifying column entrance and the first cylinder 210 gas-phase product outlet, rectifying column
The fixed gas outlet at top is connected to the hydrogen inlet of the second cylinder 11.The gas phase of material can be produced with rectifying column by being arranged such
Object is separated by boiling spread, to convert heavy oils into as available product.
In order to improve the utilization rate to hydrogen, the complete hydrogen of unreacted can be recycled.Existing heavy-oil hydrogenation processing system
In system, the hydrogen of recycling is needed through solvent or eluted through lye impurity, or can just be reused by solid absorption.This implementation
Due to being run under the lower environment of pressure and temperature, hydrogen is more easily escaped from liquid phase system in example.
Moreover, because this system is lower to the purity requirement of hydrogen, the hydrogen of recycling, which does not need processing, to be reused.Therefore originally
The technical solution of embodiment can reduce the cost recovery of hydrogen.
It, can be with low by above-mentioned setting due to containing a large amount of unreacted hydrogen in the fixed gas at the top of rectifying column
The mode of cost is by the fixed gas recycling and reusing containing hydrogen.Specifically, fixed gas can be transported in hydrogen supply device, no
The hydrogen generated in solidifying gas and hydrogen supply device is transported in mixed cell 10 again after mixing.Or fixed gas is delivered directly to mixed
It closes and is recycled in unit 10.
Pressure when existing heavy-oil hydrogenation processing system is run is in 5.0MPa between 24.13MPa.And in the present embodiment
In, the pressure in heavy-oil hydrogenation processing system, which is less than 0.1MPa, to be run, i.e., this system can be run under normal pressure.This with
Existing heavy-oil hydrogenation processing system is compared, and the operating pressure of this system substantially reduces, therefore on the one hand can reduce to system
Performance requirement on the other hand can reduce so as to reduce the cost of investment of system to the requirement of the operating parameter of system, from
And it can reduce the operating cost of system.
Reaction temperature when existing heavy-oil hydrogenation processing system is run is between 370 DEG C to 460 DEG C.And in the application
In, the reaction temperature of material is between 350 DEG C to 410 DEG C in heavy-oil hydrogenation processing system.This is handled with existing heavy-oil hydrogenation
The reaction temperature of system is compared and is substantially reduced, therefore can reduce the energy consumption of system, to reduce the operating cost of system.
It can be seen from the above, compared with prior art, heavy-oil hydrogenation processing system provided by the invention can be in normal pressure and temperature
It spends under lower environment and runs, and is low to the purity requirement of hydrogen, low to the consumption of hydrogen.It is above due to having the characteristics that,
Therefore technical solution of the present invention can reduce the investment cost and operating cost of heavy-oil hydrogenation processing system.It is obtained through calculating,
The cost of investment of heavy-oil hydrogenation processing system provided by the invention is only the 1/10 to 1/20 of the cost of investment of existing system, fortune
Row cost is only the 1/2 to 1/3 of the operating cost of existing system, therefore can be obtained according to the technical solution of the present invention significant
Economic benefit.
The foregoing is only a preferred embodiment of the present invention, is not intended to restrict the invention, for the skill of this field
For art personnel, the invention may be variously modified and varied.All within the spirits and principles of the present invention, made any to repair
Change, equivalent replacement, improvement etc., should all be included in the protection scope of the present invention.
It should be noted that term used herein above is merely to describe specific embodiment, and be not intended to restricted root
According to the illustrative embodiments of the application.As used herein, unless the context clearly indicates otherwise, otherwise singular
Also it is intended to include plural form, additionally, it should be understood that, when in the present specification using term "comprising" and/or " packet
Include " when, indicate existing characteristics, step, operation, device, component and/or their combination.
Unless specifically stated otherwise, positioned opposite, the digital table of the component and step that otherwise illustrate in these embodiments
It is not limited the scope of the invention up to formula and numerical value.Simultaneously, it should be appreciated that for ease of description, each portion shown in attached drawing
The size divided not is to draw according to actual proportionate relationship.For technology, side known to person of ordinary skill in the relevant
Method and equipment may be not discussed in detail, but in the appropriate case, and the technology, method and apparatus should be considered as authorizing explanation
A part of book.In shown here and discussion all examples, any occurrence should be construed as merely illustratively, and
Not by way of limitation.Therefore, the other examples of exemplary embodiment can have different values.It should also be noted that similar label
Similar terms are indicated in following attached drawing with letter, therefore, once it is defined in a certain Xiang Yi attached drawing, then subsequent attached
It does not need that it is further discussed in figure.
In the description of the present invention, it is to be understood that, the noun of locality such as " front, rear, top, and bottom, left and right ", " it is laterally, vertical,
Vertically, orientation or positional relationship indicated by level " and " top, bottom " etc. is normally based on orientation or position shown in the drawings and closes
System, is merely for convenience of description of the present invention and simplification of the description, in the absence of explanation to the contrary, these nouns of locality do not indicate that
It must have a particular orientation or be constructed and operated in a specific orientation with the device or element for implying signified, therefore cannot manage
Solution is limiting the scope of the invention；The noun of locality " inside and outside " refers to inside and outside the profile relative to each component itself.
For ease of description, spatially relative term can be used herein, as " ... on ", " ... top ",
" ... upper surface ", " above " etc., for describing such as a device shown in the figure or feature and other devices or spy
The spatial relation of sign.It should be understood that spatially relative term is intended to comprising the orientation in addition to device described in figure
Except different direction in use or operation.For example, being described as if the device in attached drawing is squeezed " in other devices
It will be positioned as " under other devices or construction after part or construction top " or the device of " on other devices or construction "
Side " or " under other devices or construction ".Thus, exemplary term " ... top " may include " ... top " and
" in ... lower section " two kinds of orientation.The device can also be positioned with other different modes and (is rotated by 90 ° or in other orientation), and
And respective explanations are made to the opposite description in space used herein above.
In addition, it should be noted that, limiting components using the words such as " first ", " second ", it is only for be convenient for
Corresponding components are distinguished, do not have Stated otherwise such as, there is no particular meanings for above-mentioned word, therefore should not be understood as to this
The limitation of invention protection scope.
Claims (23)
1. a kind of heavy-oil hydrogenation processing system, which is characterized in that including main reactor (200) and at least one sub- reactor
(100), the main reactor (200) includes the first cylinder (210), and the sub- reactor (100) includes:
Mixed cell (10), for mixing material and hydrogen, the mixed cell (10) includes the second cylinder (11), and described the
Material inlet, hydrogen inlet and first outlet, the material inlet and first cylinder (210) are provided on two cylinders (11)
Outlet；
Intensifying device, the entrance of the intensifying device are connected to the first outlet of second cylinder (11), the intensifying device
Outlet be connected to the accommodating chamber of first cylinder (210), the intensifying device be used for material provide energy so that material
Cracking reaction occurs.
2. heavy-oil hydrogenation processing system according to claim 1, which is characterized in that the intensifying device includes strengthening list
Member, the reinforcing unit is plasma unit (20), cavitation unit (30), in agitating unit (40) and crash unit (50)
One or more, for carrying out ionization processing to material, the cavitation unit (30) is used for the plasma unit (20)
Material is set to generate cavitation, for the agitating unit (40) for being stirred to material, the crash unit (50) is used for will
Material into the accommodating chamber of first cylinder (210) is hit.
3. heavy-oil hydrogenation processing system according to claim 2, which is characterized in that the intensifying device includes multiple reinforcings
Unit, each reinforcing unit are plasma unit (20), cavitation unit (30), agitating unit (40) and crash unit
One of (50), when one of them described reinforcing unit is crash unit (50), the outlet of the crash unit (50) with
The accommodating chamber of first cylinder (210) is connected to, the first outlet of second cylinder (11), other described reinforcing units and institute
Crash unit (50) is stated sequentially to be connected to.
4. heavy-oil hydrogenation processing system according to claim 2, which is characterized in that the intensifying device includes multiple reinforcings
Unit, each reinforcing unit are one of plasma unit (20), cavitation unit (30) and agitating unit (40), institute
State the first outlet of the second cylinder (11), multiple reinforcing units are sequentially connected to the accommodating chamber of first cylinder (210).
5. heavy-oil hydrogenation processing system according to claim 2, which is characterized in that plasma unit (20) packet
It includes:
Third cylinder (21) has the first barrel and the second barrel, and the inside of second barrel is arranged in first barrel,
There is the first cavity between first barrel and second barrel, there is the second cavity in first barrel, material can
It is flowed in first cavity；
Dielectric (22) is arranged in second cavity；
Electrode (23) at least partially penetrates in the dielectric (22), and one end of the electrode (23) connects high voltage power supply.
6. heavy-oil hydrogenation processing system according to claim 2, which is characterized in that the cavitation unit (30) includes:
4th cylinder；
Cavitation board group (31) is arranged in the 4th cylinder；And/or
Cavitation mouth is arranged in the 4th cylinder.
7. heavy-oil hydrogenation processing system according to claim 6, which is characterized in that the cavitation unit (30) includes cavitation
Board group (31), the cavitation board group (31) include:
First plate body (31a) is provided with multiple through-holes on first plate body (31a)；
Second plate body (31b), is provided with multiple through-holes on second plate body (31b), second plate body (31b) and described the
There is angle between one plate body (31a).
8. heavy-oil hydrogenation processing system according to claim 7, which is characterized in that at least partly described first plate body
The periphery of (31a) is zigzag, and/or the periphery of at least partly described second plate body (31b) is zigzag.
9. heavy-oil hydrogenation processing system according to claim 6, which is characterized in that the cavitation board group (31) be it is multiple,
Multiple cavitation board groups (31) are sequentially arranged in the 4th cylinder along the flow direction of material.
10. heavy-oil hydrogenation processing system according to claim 2, which is characterized in that the agitating unit (40) includes:
5th cylinder；
Shaft (41) is rotatably arranged in the 5th cylinder, the flow direction axially along material of the shaft (41)
Setting；
Multiple blades (42), multiple blades (42) are arranged at intervals on the shaft along the circumferencial direction of the shaft (41)
(41) on.
11. heavy-oil hydrogenation processing system according to claim 10, which is characterized in that the agitating unit (40) is also wrapped
It includes:
Multiple arcs baffle (43) is fixed between the 5th cylinder and multiple blades (42), multiple arcs
Shape baffle (43) is arranged along the circumferencial direction interval of the shaft (41).
12. heavy-oil hydrogenation processing system according to claim 2, which is characterized in that crash unit (50) setting exists
The top of the accommodating chamber of first cylinder (210), the crash unit (50) include:
Bracket (51) is fixed on the inner sidewall of first cylinder (210)；
Delivery pipe (52) is fixed on the bracket (51), the entrance of the delivery pipe (52) and second cylinder (11)
First outlet connection.
13. heavy-oil hydrogenation processing system according to claim 2, which is characterized in that
The intensifying device of the sub- reactor (100) includes the crash unit (50), crash unit (50) entrance and institute
State the first outlet connection of the second cylinder (11), the receiving of the outlet of the crash unit (50) and first cylinder (210)
Chamber connection；
The sub- reactor (100) at least two, the outlet of the crash unit (50) of at least two sub- reactors (100)
Interval setting, the material for entering first cylinder (210) from the different crash units (50) are hit.
14. heavy-oil hydrogenation processing system according to claim 1, which is characterized in that the inner wall of second cylinder (11)
Cross-sectional area be greater than the first outlet inner wall cross-sectional area, second cylinder (11) is made of steel pipe.
15. heavy-oil hydrogenation processing system according to claim 1, which is characterized in that the mixed cell (10) further include:
Gas distributor (12), setting is in second cylinder (11), the gas distributor (12) and the hydrogen inlet
Connection, the gas distributor (12) is for hydrogen to be evenly distributed in material.
16. heavy-oil hydrogenation processing system according to claim 15, which is characterized in that gas distributor (12) packet
It includes:
Ontology, the ontology have entrance and exit, the hydrogen inlet company of the entrance of the ontology and second cylinder (11)
It is logical；
Inoranic membrane is arranged in the outlet of the ontology, and the inoranic membrane has multiple through-holes, it is preferable that the inoranic membrane is
Ceramic membrane, it is highly preferred that the diameter of the through-hole of the ceramic membrane is between 0.3 μm to 1.0 μm.
17. heavy-oil hydrogenation processing system according to claim 16, which is characterized in that the gas distributor (12) is also wrapped
It includes:
Molecular sieve, the molecular sieve are attached on the inoranic membrane, it is preferable that the molecular sieve is FAU type molecular sieve, more preferably
Ground, the thickness of the FAU type molecular sieve is less than 1.0 μm.
18. heavy-oil hydrogenation processing system according to claim 1, which is characterized in that the sub- reactor (100) is also wrapped
It includes:
The pump housing (60) is arranged on the pipeline between the outlet and the outlet of the intensifying device of first cylinder (210), institute
The pump housing (60) are stated for conveying material.
19. heavy-oil hydrogenation processing system according to claim 1, which is characterized in that the heavy-oil hydrogenation processing system is also
Include:
Hydrogen supply device, the hydrogen outlet of the hydrogen supply device are connected to the hydrogen inlet of second cylinder (11), the hydrogen supply
The purity for the hydrogen that device provides is A, wherein A >=20%.
20. heavy-oil hydrogenation processing system according to claim 19, which is characterized in that the hydrogen supply device is by methane cracking
Prepare hydrogen.
21. heavy-oil hydrogenation processing system according to claim 19, which is characterized in that the heavy-oil hydrogenation processing system is also
Include:
Rectifying column, the rectifying column are used to separate the gas-phase product of material by boiling spread, the entrance of the rectifying column and institute
State the gas-phase product outlet of the first cylinder (210)；
At the top of the rectifying column fixed gas outlet be connected to the entrance of the hydrogen supply device or the rectifying column at the top of do not coagulate
Gas outlet is connected to the hydrogen inlet of second cylinder (11).
22. heavy-oil hydrogenation processing system according to claim 1, which is characterized in that in the heavy-oil hydrogenation processing system
Pressure be less than 0.1MPa.
23. heavy-oil hydrogenation processing system according to claim 1, which is characterized in that in the heavy-oil hydrogenation processing system
The reaction temperature of material is between 350 DEG C to 410 DEG C.
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| CN201710627354.2A CN109306272B (en) | 2017-07-27 | 2017-07-27 | Heavy oil hydrotreating system |
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110152588A (en) * | 2019-04-19 | 2019-08-23 | 张其凯 | Liquid non-submersion formula impinging stream reaction device and reaction method |
| CN110591758A (en) * | 2019-09-29 | 2019-12-20 | 中国石油化工股份有限公司 | Pretreatment method of residual oil hydrogenation raw material and residual oil hydrogenation method |
| WO2021078186A1 (en) | 2019-10-25 | 2021-04-29 | 中国石油化工股份有限公司 | Liquid phase reactor and application thereof |
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