CN106753557A - A kind of high-efficiency heavy oil conversion process - Google Patents
A kind of high-efficiency heavy oil conversion process Download PDFInfo
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- CN106753557A CN106753557A CN201611128469.9A CN201611128469A CN106753557A CN 106753557 A CN106753557 A CN 106753557A CN 201611128469 A CN201611128469 A CN 201611128469A CN 106753557 A CN106753557 A CN 106753557A
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- 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
- C10G69/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process
- C10G69/02—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process plural serial stages only
- C10G69/06—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process plural serial stages only including at least one step of thermal cracking in the absence of hydrogen
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
-
- 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
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/70—Catalyst aspects
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0913—Carbonaceous raw material
- C10J2300/0943—Coke
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0953—Gasifying agents
- C10J2300/0959—Oxygen
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0953—Gasifying agents
- C10J2300/0973—Water
- C10J2300/0976—Water as steam
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/52—Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts
Abstract
The present invention relates to a kind of high-efficiency heavy oil conversion process, feedstock oil imports mixed phase generator, gas-liquid mixed phase is mixed to form with catalyst and hydrogen, flow-guiding type slurry bubble bed hydrogenation reactor is sprayed into by gas-liquid mixed phase nozzle hydrocracking reaction occurs, difficult cracking heavy distillat containing solid particle enters pyrolysis apparatus and heat scission reaction occurs with gasifier next high-temperature coke powder particles, the coke of generation flows into gasifier and generation gasification reaction is contacted with gasifying agent with the circulation of coke powder particle, the synthesis gas of generation leaves gasifier from top, and remaining high-temperature coke powder particles are recycled into pyrolysis apparatus.Compared with prior art, the present invention have catalyst expend it is low, dispersion effect is good, without outside tailings row and it is pollution-free the advantages of.
Description
Technical field
The present invention relates to a kind of heavy hydrocarbon Treatment technique for processing, more particularly, to a kind of high-efficiency heavy oil conversion process.
Background technology
With the development of crude oil in poor quality trend, each state all is making great efforts to improve heavy oil utilization rate.Heavy oil utilization rate is depended on
The process technology of heavy oil.The heavy oil decarburization process technology such as traditional delayed coking showed in terms of light oil yield and product quality compared with
The heavy Oil Hydrotreating Processes such as difference, fixed bed hydrogenation are again unsatisfactory in terms of adaptability to raw material, especially processing bad
During reduced fuel oil, what the shortcoming of above-mentioned Heavy Oil Processing Technology embodied more protrudes.
Start the fifties in last century to occur in that slurry bed system heavy-oil hydrogenation technology.Slurry bed system heavy-oil hydrogenation is the presence in hydrogen
Under, the heavy oil that will be mixed with catalyst passes through empty cartridge type or has the reactor of simple inner member, hydrogenation heat cracking reaction is carried out, weight
Oil is converted into the lightweight oils such as naphtha cut, diesel oil distillate, wax oil cut.Its technological process is simple, and green coke is few, and raw material is fitted
Ying Xingqiang, light oil yield is high, good product quality, for the working process of inferior heavy oil provides an effective way.
German VEBA companies develop VCC slurry bed system heavy oil hydrogenation process at the beginning of the fifties, are supported using lignite or coke powder
Ferrous sulfate makees catalyst, and addition is less than 5%.After feedstock oil mixes with catalyst, hydrogen is added, reaction is entered after preheating
Device, reacts under conditions of 440~485 DEG C and 25MPa, and product obtains product after separating, and bed drain purge is about feedstock oil
6%, conversion ratio is more than 90%.
Canadian Alberta Research develop (HC) 3TMSlurry bed system heavy oil hydrogenation process, using carbonyls knot
Colloid/the molecular catalyst of structure.Catalyst can associate with asphalitine, promote the hydro-conversion of asphalitine, and suppress green coke.This
Technical process is as follows：Feedstock oil is diluted with 200-455 DEG C of distillate, and the ratio of diluent/feedstock oil is 1:1-10, is subsequently adding
Carbonyl cobalt, or molybdenum, nickel, iron etc. carbonyls, press 7-15MPa, 420-480 DEG C of temperature, liquid air speed 0.2-2h in hydrogen-1's
Under the conditions of reacted.When reaction temperature is 525 DEG C, the Liaohe River subtracts slag and isolated island subtracts the conversion ratio of slag and reaches 80%-90%.
Hydrogenation catalyst suspended dispersed in slurry bubble bed reaction system is slurry bubble bed process distinction in other heavy-oil hydrogenation works
The principal character of skill.The dispersion effect of hydrogenation catalyst largely influences slurry bubble bed hydrogenation reaction efficiency.Currently, slurries
Bed hydrogenation catalyst has heterogeneous catalysis and homogeneous catalyst, and homogeneous disperse type catalyzer is divided into water-soluble catalyst and oil again
Soluble catalytic agent.Heterogeneous catalysis low cost, but have the shortcomings that decentralization is relatively low, addition is big.Homogeneous decentralized catalysis
Agent decentralization is higher, and specific surface area is big, and addition is few, but high cost, and economic benefit is relatively low.
On the other hand, although existing slurry bed system heavy-oil hydrogenation technology can also be generated substantial amounts of with conversion ratio higher
Tailings, tailings amount is up to 10% or so.The hydrocarbon component of slurry bed system heavy-oil hydrogenation tailings is stable in properties, it is difficult to convert；Solid contains
Amount is big, and viscosity is big, poor fluidity, is worth low, not readily transportable, its high processing cost, hinders slurry bed system heavy-oil hydrogenation
The development of technology.
The content of the invention
The purpose of the present invention is exactly to provide a kind of catalyst for the defect for overcoming above-mentioned prior art to exist to expend low,
Dispersion effect is good, without row and a kind of free of contamination high-efficiency heavy oil conversion process outside tailings.
The purpose of the present invention can be achieved through the following technical solutions：
A kind of high-efficiency heavy oil conversion process, iron-based or coke load iron, cobalt, catalyst with base of molybdenum are loaded using coke, are carried out
Heavy oil slurry bubble bed hydrogenation reaction, produces light-end products, specifically using following steps：
(1) feedstock oil is imported into mixed phase generator, mixed phase generator is provided with mixing inner member, hydrogen, feedstock oil and catalysis
Agent forms gas-liquid mixed phase in the presence of inner member is mixed；
(2) gas-liquid mixed phase sprays into flow-guiding type slurry bubble bed hydrogenation reactor by gas-liquid mixed phase nozzle, dynamic in deflector and fluid
In the presence of energy, circulation disturbance forms full back-mixing reaction system and hydrocracking reaction occurs；
(3) hydrocracking gas of reaction generation leave flow-guiding type slurry bubble bed hydrogenation reactor and go subsequent treatment to walk from top
Suddenly, the difficult cracking heavy distillat containing solid particle is extracted out from flow-guiding type slurry bubble bed hydrogenation reactor bottom, into pyrolysis apparatus；
(4) the high-temperature coke powder particles mixing that difficult cracking heavy distillat comes in pyrolysis apparatus with gasifier is contacted, and is absorbed heat and is occurred
Heat scission reaction, the pyrolysis gas of generation leave pyrolysis apparatus and remove subsequent step from top, and pyrogenous origin coke is with coke powder particle one
Play circulation and flow into gasifier, while part coke powder particle is extracted for preparing coke load iron, cobalt, catalyst with base of molybdenum；
(5) coke contacts generation gasification reaction in gasifier with gasifying agent, and the synthesis gas of generation leaves gasification from top
Device, remaining high-temperature coke powder particles are recycled into pyrolysis apparatus.
Described catalyst is coke load iron, cobalt, catalyst with base of molybdenum, and described iron, cobalt, the mass ratio of molybdenum element are 30
~100:0~70:0~70.
Described catalyst can also mix before mixed phase generator is entered with feedstock oil,
Described hydrogen can also mix before mixed phase generator is entered with feedstock oil.
The addition of described catalyst is 0.1%~10wt% of feedstock oil, and hydrogen is 10 with the volume ratio of feedstock oil:
1~2000:1.
In the described built-in wire packing of mixed phase generator, spiral deflector, Venturi nozzles, deflection plate or sieve tray
The combination of one or more.
Before or after mixed phase generator can be arranged on heating furnace.
Described gas-liquid mixed phase nozzle is the part that pressure energy is converted into fluid dynamic energy, including undergauge center pipe or is opened
Hole pipe.
Described flow-guiding type slurry bubble bed hydrogenation reactor is the barrel type reactor of built-in deflector, and described deflector is
One monoblock is divided into several pieces of flat board and arc, axial arranged along reactor, is set on flow-guiding type slurry bubble bed hydrogenation reactor
Multiple spot hydrogen injection point is put, for inside reactor Liquid Flow provides kinetic energy.
Before pyrolysis gas and synthesis gas can be passed through flow-guiding type slurry bubble bed hydrogenation reactor or reactor, as slurry bubble bed plus
The thermal source of hydrogen reaction.
The addition of catalyst and hydrogen is relevant with feedstock property, and general catalyst charge is 0.1 (w) % of feedstock oil
~10 (w) %, hydrogen to oil volume ratio is 10:1~2000:1.
Reaction mass is by the reaction condition of flow-guiding type slurry bubble bed hydrogenation reactor with feedstock property, the change for the treatment of target
And change, General reactions temperature is 360 DEG C~470 DEG C, and reaction pressure is 10~22MPa, and volume space velocity is 1~10h-1。
The reaction condition of pyrolysis apparatus with feedstock property, treatment target change change, General reactions temperature be 450 DEG C~
650 DEG C, reaction pressure is 0.1~22MPa, and volume space velocity is 0.1~20h-1。
The oxygen of gasifier, the addition of vapor change with the change of properties of feedstock oil, and general oxygen oil quality ratio is
0.1:1~10:1, water oil quality ratio is 0.1:1~10:1.
Gasification reaction conditions change with the property of feedstock oil, the change of gasifier form, and general gasification reaction pressure is 4
~22MPa, gasification reaction temperature is 500 DEG C~2000 DEG C, and volume space velocity is 0.1~100h-1。
Compared with prior art, the coke that the present invention is used is homologous with heavy oil, and compatibility is good, and particle diameter very little, in original
Dispersive property in material oil is good, and efficiency high, consumption is few.Iron, cobalt, molybdenum are metallic element common in crude oil, pyrogenous origin Jiao
Charcoal inherently contains iron, cobalt, molybdenum, can be originated as catalyst metal components, reduces catalyst consumption amount.Using built-in water conservancy diversion
The slurry bubble bed hydrogenation reactor of plate, in the presence of deflector, reactor temperature is distributed, reaction effect homogeneous with concentration distribution
It is good.The component that the pyrolysis apparatus and gasifier of use are difficult to be hydrocracked is further converted into pyrolysis gas and synthesis gas, realizes
Heavy oil 100% is converted, without low value by-product output, device high efficiency.Gasifier gasification reaction production synthesis gas, can be further
Hydrogen can be produced, the hydrogen that hydrogenation reaction is consumed is made up, without extra hydrogen supply.
Brief description of the drawings
Fig. 1 is process flow diagram of the invention.
In figure, 1- mixed phases generator, 2- flow-guiding type slurry bubble beds hydrogenation reactor, 3- pyrolysis apparatus, 4- gasifiers.
Specific embodiment
The present invention is described in detail with specific embodiment below in conjunction with the accompanying drawings.Following examples will be helpful to this area
Technical staff further understand the present invention, but the invention is not limited in any way.It should be pointed out that to the general of this area
For logical technical staff, without departing from the inventive concept of the premise, various modifications and improvements can be made.These are belonged to
Protection scope of the present invention.
Embodiment 1
A kind of high-efficiency heavy oil conversion process, ferrum-based catalyst is loaded using coke, carries out heavy oil slurry bubble bed hydrogenation reaction, raw
Produce light-end products.Its technique is as shown in Figure 1.The equipment of production include mixed phase generator 1, flow-guiding type slurry bubble bed hydrogenation reactor 2,
Pyrolysis apparatus 3 and gasifier 4.Raw material initially enters mixed phase generator 1, mixes with catalyst and hydrogen.Mixed phase generator 1 is provided with mixed
Inner member is closed, hydrogen, feedstock oil and catalyst form gas-liquid mixed phase in the presence of inner member is mixed.Gas-liquid mixed phase is by gas-liquid
Mixed phase nozzle sprays into flow-guiding type slurry bubble bed hydrogenation reactor 2, and in the presence of deflector and fluid dynamic energy, circulation disturbance is formed
Full back-mixing reaction system, and there is hydrocracking reaction.The hydrocracking gas for reacting generation leave flow-guiding type slurry bubble bed from top
Hydrogenation reactor 2, goes subsequent processing steps.Hardly possible containing solid particle cracks heavy distillat from flow-guiding type slurry bubble bed hydrogenation reactor
2 bottom is extracted out, into pyrolysis apparatus 3.Pyrolysis apparatus 3 uses fluidized-bed reactor, fluid coke powder particles to constitute reaction bed, and difficulty is split
Solution heavy distillat is contacted with the high-temperature coke powder particles mixing of gasifier 4 herein, absorb heat concurrent heat cracking reaction, the pyrolysis of generation
Gas leaves pyrolysis apparatus 3 from top, removes subsequent step.Pyrogenous origin coke circulates inflow gasifier 4 with coke powder particle, with
There is gasification reaction in gasifying agent contact, the synthesis gas of generation leaves gasifier 4 from top, and remaining high-temperature coke powder particles are recycled into
Pyrolysis apparatus.A coke powder particle part in pyrolysis apparatus be used to prepare coke load ferrum-based catalyst.
According to aforesaid operations flow, ferrum-based catalyst is loaded using coke, be raw material, the result of gained with 380 fuel oil
It is as follows：
The property of the feedstock oil of table 1
| Project | Measurement result |
| General physical property | |
| Density (20 DEG C)/gcm-3 | 0.9664 |
| Viscosity (50 DEG C)/mm2·s-1 | 300.85 |
| (80℃) | 92.40 |
| W (carbon residue)/% | 12.0 |
| Freezing point/DEG C | -4 |
| Chemical composition (mass fraction)/% | |
| Saturation point | 41.92 |
| Fragrance point | 34.99 |
| Colloid | 17.32 |
| C7- asphalitine | 5.77 |
| Elementary analysis (mass fraction)/% | |
| C | 85.06 |
| H | 11.17 |
| S | 2.54 |
| N | 0.43 |
| H/C | 1.58 |
| Tenor/μ gg-1 | |
| Ni | 34.0 |
| V | 196 |
| Fe | 6.7 |
| Ca | 47.7 |
| Fractional composition (mass fraction)/% | |
| <180℃ | 2.93 |
| 180~360 DEG C | 18.71 |
| 360~500 DEG C | 26.19 |
| >500℃ | 52.17 |
The process conditions of table 2
The operation result of table 3
Embodiment 2
A kind of high-efficiency heavy oil conversion process, using following steps：
(1) feedstock oil is imported into mixed phase generator, mixed phase generator is provided with wire packing as mixing inner member, and hydrogen exists
Mix with feedstock oil before into mixed phase generator, in mixed phase generator, hydrogen, feedstock oil and coke load iron, cobalt, molybdenum base
Catalyst forms gas-liquid mixed phase under the further effect of mixing inner member, wherein, the addition of catalyst is feedstock oil
0.1wt%, hydrogen is 10 with the volume ratio of feedstock oil:1, iron, cobalt, the mass ratio of molybdenum element are 10:30:60；
(2) gas-liquid mixed phase by gas-liquid mixed phase nozzle spray into flow-guiding type slurry bubble bed hydrogenation reactor, gas-liquid mixed phase nozzle be by
Pressure energy is converted into the part of fluid dynamic energy, undergauge center pipe is used in the present embodiment, in deflector and the work of fluid dynamic energy
Under, circulation disturbance forms full back-mixing reaction system and hydrocracking reaction, the flow-guiding type slurries used in the present embodiment occurs
Bed hydroprocessing reactor is the barrel type reactor of built-in deflector, and multiple spot hydrogen injection point is set on reactor, is anti-
Device inside Liquid Flow is answered to provide kinetic energy, the deflector of inside reactor is a monoblock flat board, axial arranged along reactor, is being led
Streaming slurries bed hydroprocessing.Reaction mass is by the reaction condition of flow-guiding type slurry bubble bed hydrogenation reactor with feedstock property, treatment mesh
Target changes and changes, and reaction temperature is 360 DEG C in the present embodiment, and reaction pressure is 10MPa, and volume space velocity is 1h-1。
(3) hydrocracking gas of reaction generation leave flow-guiding type slurry bubble bed hydrogenation reactor and go subsequent treatment to walk from top
Suddenly, the difficult cracking heavy distillat containing solid particle is extracted out from flow-guiding type slurry bubble bed hydrogenation reactor bottom, into pyrolysis apparatus；
(4) the high-temperature coke powder particles mixing that difficult cracking heavy distillat comes in pyrolysis apparatus with gasifier is contacted, and is absorbed heat and is occurred
Heat scission reaction, the reaction condition of pyrolysis apparatus changes with feedstock property, the change for the treatment of target, reaction temperature in the present embodiment
It it is 450 DEG C, reaction pressure is 0.1MPa, volume space velocity is 0.1h-1.The pyrolysis gas of generation leave pyrolysis apparatus and go follow-up step from top
Suddenly, pyrogenous origin coke circulates inflow gasifier with coke powder particle；
(5) coke contacted with gasifying agent in gasifier generation gasification reaction, gasification reaction conditions with feedstock oil property,
The change of gasifier form and change, in the present embodiment gasification reaction pressure be 4MPa, gasification reaction temperature be 500 DEG C, volume
Air speed is 0.1h-1.The oxygen of gasifier, the addition of vapor change with the change of properties of feedstock oil, and oxygen oil quality ratio is
0.1:1, water oil quality ratio is 0.1:1.The synthesis gas of generation leaves gasifier from top, and remaining high-temperature coke powder particles are recycled into
Pyrolysis apparatus, the coke powder particle part in pyrolysis apparatus may be utilized for preparing the carrier of catalyst.
Embodiment 3
A kind of high-efficiency heavy oil conversion process, using following steps：
(1) feedstock oil is imported into mixed phase generator, mixed phase generator is provided with Venturi nozzles, deflection plate as in mixing
Component, coke load iron, cobalt, molybdenum catalyst mixed before mixed phase generator is entered with feedstock oil, iron, cobalt, the matter of molybdenum element
Amount is than being 30:40:30, in mixed phase generator, hydrogen, feedstock oil and catalyst mixing inner member further effect under,
Gas-liquid mixed phase is formed, wherein, the addition of catalyst is the 10wt% of feedstock oil, and hydrogen is 2000 with the volume ratio of feedstock oil:
1；
(2) gas-liquid mixed phase by gas-liquid mixed phase nozzle spray into flow-guiding type slurry bubble bed hydrogenation reactor, gas-liquid mixed phase nozzle be by
Pressure energy is converted into the part of fluid dynamic energy, and perforate pipe is used in the present embodiment, in the presence of deflector and fluid dynamic energy,
Circulation is disturbed, and forms full back-mixing reaction system and hydrocracking reaction occurs, and the flow-guiding type slurry bubble bed used in the present embodiment adds
Hydrogen reactor is the barrel type reactor of built-in deflector, and multiple spot hydrogen injection point is set on reactor, is reactor
Internal Liquid Flow provides kinetic energy, and the deflector of inside reactor is a monoblock flat board, axial arranged along reactor, in flow-guiding type
Slurries bed hydroprocessing.Reaction mass is by the reaction condition of flow-guiding type slurry bubble bed hydrogenation reactor with feedstock property, treatment target
Change and change, reaction temperature is 470 DEG C in the present embodiment, and reaction pressure is 22MPa, and volume space velocity is 10h-1。
(3) hydrocracking gas of reaction generation leave flow-guiding type slurry bubble bed hydrogenation reactor and go subsequent treatment to walk from top
Suddenly, the difficult cracking heavy distillat containing solid particle is extracted out from flow-guiding type slurry bubble bed hydrogenation reactor bottom, into pyrolysis apparatus；
(4) the high-temperature coke powder particles mixing that difficult cracking heavy distillat comes in pyrolysis apparatus with gasifier is contacted, and is absorbed heat and is occurred
Heat scission reaction, the reaction condition of pyrolysis apparatus changes with feedstock property, the change for the treatment of target, reaction temperature in the present embodiment
It it is 650 DEG C, reaction pressure is 22MPa, volume space velocity is 20h-1.The pyrolysis gas of generation leave pyrolysis apparatus and go follow-up step from top
Suddenly, pyrogenous origin coke circulates inflow gasifier with coke powder particle；
(5) coke contacted with gasifying agent in gasifier generation gasification reaction, gasification reaction conditions with feedstock oil property,
The change of gasifier form and change, in the present embodiment gasification reaction pressure be 22MPa, gasification reaction temperature be 2000 DEG C, body
Product air speed is 100h-1.The oxygen of gasifier, the addition of vapor change with the change of properties of feedstock oil, oxygen oil quality ratio
It is 10:1, water oil quality ratio is 10:1.The synthesis gas of generation leaves gasifier from top, and remaining high-temperature coke powder particles are recycled into
Pyrolysis apparatus, the coke powder particle part in pyrolysis apparatus may be utilized for preparing the carrier of catalyst.
Specific embodiment of the invention is described above.It is to be appreciated that the invention is not limited in above-mentioned
Particular implementation, those skilled in the art can within the scope of the claims make various deformations or amendments, this not shadow
Sound substance of the invention.
Claims (10)
1. a kind of high-efficiency heavy oil conversion process, it is characterised in that the technique uses following steps：
(1) feedstock oil is imported into mixed phase generator, gas-liquid mixed phase is mixed to form with catalyst and hydrogen；
(2) gas-liquid mixed phase sprays into flow-guiding type slurry bubble bed hydrogenation reactor by gas-liquid mixed phase nozzle, in deflector and fluid dynamic energy
Under effect, circulation disturbance forms full back-mixing reaction system and hydrocracking reaction occurs；
(3) hydrocracking gas of reaction generation leave flow-guiding type slurry bubble bed hydrogenation reactor and go subsequent processing steps from top, contain
The difficult cracking heavy distillat for having solid particle is extracted out from flow-guiding type slurry bubble bed hydrogenation reactor bottom, into pyrolysis apparatus；
(4) the high-temperature coke powder particles mixing that difficult cracking heavy distillat comes in pyrolysis apparatus with gasifier is contacted, and concurrent heat of absorbing heat is split
Solution reaction, the pyrolysis gas of generation leave pyrolysis apparatus and go subsequent step, pyrogenous origin coke to be followed with coke powder particle from top
Circulation enters gasifier, while part coke powder particle is extracted for preparing coke load iron, cobalt, catalyst with base of molybdenum；
(5) coke contacts generation gasification reaction in gasifier with gasifying agent, and the synthesis gas of generation leaves gasifier from top, remains
Reinforcement temperature coke powder particle is recycled into pyrolysis apparatus.
2. a kind of high-efficiency heavy oil conversion process according to claim 1, it is characterised in that described catalyst is negative for coke
Iron, cobalt, catalyst with base of molybdenum are carried, iron, cobalt, the mass ratio of molybdenum element are 30~100:0~70:0~70.
3. a kind of high-efficiency heavy oil conversion process according to claim 1, it is characterised in that described catalyst is also entering
Mix with feedstock oil before mixed phase generator, hydrogen also mixed before mixed phase generator is entered with feedstock oil.
4. a kind of high-efficiency heavy oil conversion process according to claim 1, it is characterised in that the addition of described catalyst
It is 0.1%~10wt% of feedstock oil, hydrogen is 10 with the volume ratio of feedstock oil:1~2000:1.
5. a kind of high-efficiency heavy oil conversion process according to claim 1, it is characterised in that described mixed phase generator is built-in
The combination of one or more in wire packing, spiral deflector, Venturi nozzles, deflection plate or sieve tray.
6. a kind of high-efficiency heavy oil conversion process according to claim 1, it is characterised in that described gas-liquid mixed phase nozzle is
Pressure energy is converted into the part of fluid dynamic energy, including undergauge center pipe or perforate pipe.
7. a kind of high-efficiency heavy oil conversion process according to claim 1, it is characterised in that described flow-guiding type slurry bubble bed adds
Hydrogen reactor is the barrel type reactor of built-in deflector, and described deflector is a monoblock or is divided into several pieces of flat board and arc
Plate, it is axial arranged along reactor, multiple spot hydrogen injection point is set on flow-guiding type slurry bubble bed hydrogenation reactor, it is inside reactor
Liquid Flow provides kinetic energy.
8. a kind of high-efficiency heavy oil conversion process according to claim 1, it is characterised in that described flow-guiding type slurry bubble bed adds
Controlling reaction temperature is 360 DEG C~470 DEG C in hydrogen reactor, and reaction pressure is 10~22MPa, and volume space velocity is 1~10h-1。
9. a kind of high-efficiency heavy oil conversion process according to claim 1, it is characterised in that control is anti-in described pyrolysis apparatus
It is 450 DEG C~650 DEG C to answer temperature, and reaction pressure is 0.1~22MPa, and volume space velocity is 0.1~20h-1。
10. a kind of high-efficiency heavy oil conversion process according to claim 1, it is characterised in that control in described gasifier
Gasification reaction pressure is 4~22MPa, and gasification reaction temperature is 500 DEG C~2000 DEG C, and volume space velocity is 0.1~100h-1。
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201611128469.9A CN106753557A (en) | 2016-12-09 | 2016-12-09 | A kind of high-efficiency heavy oil conversion process |
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| CN115725332A (en) * | 2021-08-27 | 2023-03-03 | 中国石化工程建设有限公司 | Light hydrocarbon isomerization device and light hydrocarbon isomerization method |
| CN115806838A (en) * | 2021-09-14 | 2023-03-17 | 中国石化工程建设有限公司 | Straight-chain hydrocarbon branch degree increasing device and straight-chain hydrocarbon branch degree increasing method |
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