CN111690433A - FCC feedstock liquid phase hydroprocessing system and method - Google Patents

FCC feedstock liquid phase hydroprocessing system and method Download PDF

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Publication number
CN111690433A
CN111690433A CN201910194179.1A CN201910194179A CN111690433A CN 111690433 A CN111690433 A CN 111690433A CN 201910194179 A CN201910194179 A CN 201910194179A CN 111690433 A CN111690433 A CN 111690433A
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hydrogen
reactor
liquid phase
reaction
gas
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CN111690433B (en
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李瑞峰
张文成
王刚
吴显军
马守涛
夏恩冬
葛冬梅
王锐
靳丽丽
张铁珍
郭立艳
王紫东
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Petrochina Co Ltd
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Petrochina Co Ltd
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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
    • 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
    • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
    • B01F23/00—Mixing according to the phases to be mixed, e.g. dispersing or emulsifying
    • B01F23/20—Mixing gases with liquids
    • B01F23/23—Mixing gases with liquids by introducing gases into liquid media, e.g. for producing aerated liquids
    • B01F23/235—Mixing gases with liquids by introducing gases into liquid media, e.g. for producing aerated liquids for making foam
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
    • B01F23/00—Mixing according to the phases to be mixed, e.g. dispersing or emulsifying
    • B01F23/20—Mixing gases with liquids
    • B01F23/23—Mixing gases with liquids by introducing gases into liquid media, e.g. for producing aerated liquids
    • B01F23/237—Mixing gases with liquids by introducing gases into liquid media, e.g. for producing aerated liquids characterised by the physical or chemical properties of gases or vapours introduced in the liquid media
    • B01F23/2373—Mixing gases with liquids by introducing gases into liquid media, e.g. for producing aerated liquids characterised by the physical or chemical properties of gases or vapours introduced in the liquid media for obtaining fine bubbles, i.e. bubbles with a size below 100 µm
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
    • B01F23/00—Mixing according to the phases to be mixed, e.g. dispersing or emulsifying
    • B01F23/20—Mixing gases with liquids
    • B01F23/23—Mixing gases with liquids by introducing gases into liquid media, e.g. for producing aerated liquids
    • B01F23/237—Mixing gases with liquids by introducing gases into liquid media, e.g. for producing aerated liquids characterised by the physical or chemical properties of gases or vapours introduced in the liquid media
    • B01F23/2376—Mixing gases with liquids by introducing gases into liquid media, e.g. for producing aerated liquids characterised by the physical or chemical properties of gases or vapours introduced in the liquid media characterised by the gas being introduced
    • B01F23/23764—Hydrogen
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
    • B01F25/00—Flow mixers; Mixers for falling materials, e.g. solid particles
    • B01F25/30—Injector mixers
    • B01F25/31—Injector mixers in conduits or tubes through which the main component flows
    • B01F25/311—Injector mixers in conduits or tubes through which the main component flows for mixing more than two components; Devices specially adapted for generating foam
    • B01F25/3111—Devices specially adapted for generating foam, e.g. air foam
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
    • B01F25/00—Flow mixers; Mixers for falling materials, e.g. solid particles
    • B01F25/30—Injector mixers
    • B01F25/31—Injector mixers in conduits or tubes through which the main component flows
    • B01F25/312—Injector mixers in conduits or tubes through which the main component flows with Venturi elements; Details thereof
    • B01F25/3121—Injector mixers in conduits or tubes through which the main component flows with Venturi elements; Details thereof with additional mixing means other than injector mixers, e.g. screens, baffles or rotating elements
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
    • B01F25/00—Flow mixers; Mixers for falling materials, e.g. solid particles
    • B01F25/30—Injector mixers
    • B01F25/31—Injector mixers in conduits or tubes through which the main component flows
    • B01F25/312—Injector mixers in conduits or tubes through which the main component flows with Venturi elements; Details thereof
    • B01F25/3123—Injector mixers in conduits or tubes through which the main component flows with Venturi elements; Details thereof with two or more Venturi elements
    • B01F25/31233—Injector mixers in conduits or tubes through which the main component flows with Venturi elements; Details thereof with two or more Venturi elements used successively
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
    • B01F33/00—Other mixers; Mixing plants; Combinations of mixers
    • B01F33/80—Mixing plants; Combinations of mixers
    • B01F33/81—Combinations of similar mixers, e.g. with rotary stirring devices in two or more receptacles
    • B01F33/811—Combinations of similar mixers, e.g. with rotary stirring devices in two or more receptacles in two or more consecutive, i.e. successive, mixing receptacles or being consecutively arranged
    • 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
    • Y02P20/10—Process efficiency

Abstract

The invention discloses a liquid phase hydrotreating system and a liquid phase hydrotreating method for FCC (fluid catalytic cracking) raw materials. The method comprises the following steps: step 1, fresh FCC raw material is subjected to heat exchange by a heat exchanger and is heated by a heating furnace and is fully mixed with hydrogen by a first hydrogen mixer; step 2, after the step 1, feeding the hydrogen-dissolved FCC raw material into a pre-reactor of a liquid phase hydrogenation pre-reaction unit for demetalization, carbon residue removal reaction and partial removal of sulfide and nitride; step 3, mixing the pre-reaction product generated in the step 2 with hydrogen again through a hydrogen stripping unit and a second hydrogen mixer, and then feeding the mixed product into a liquid phase hydrogenation main reactor of a main reaction unit to deeply remove sulfides, nitrides and aromatic hydrocarbons; and 4, performing gas-liquid separation on the main reaction product generated in the step 3 after pressure reduction without heat exchange, and performing heat exchange on the obtained liquid-phase material to obtain a refined product. The invention cancels a circulating hydrogen and circulating oil system, adopts a proper process and novel technical equipment, increases the hydrogen dissolving amount of the FCC raw material and the mutual dissolving uniformity of the FCC raw material and the hydrogen, not only improves the hydrogenation reaction efficiency, but also reduces the energy consumption of the device and the equipment investment cost.

Description

FCC feedstock liquid phase hydroprocessing system and method
Technical Field
The invention belongs to the field of petroleum processing, relates to a liquid phase hydrogenation process, and particularly relates to a system and a method for liquid phase hydrogenation treatment of an FCC (fluid catalytic cracking) raw material.
Background
With the stricter environmental regulations in China, the quality requirements on petroleum products, especially light fuels such as gasoline, diesel oil and the like, are higher and higher. The catalytic cracking (FCC) process is one of the important secondary processing means of crude oil due to its strong raw material adaptability, high added value of products and good economic benefit. At present, FCC gasoline in China accounts for about 70% of a gasoline pool, and FCC diesel oil accounts for about 30% of the diesel pool. The problem that how to effectively improve the quality of FCC raw materials, reduce the content of sulfur, nitrogen and other impurities in an FCC product which is increasing day by day and produce clean fuel meeting the environmental protection requirement is urgently solved at present is faced with the increase of the processing amount of inferior crude oil year by year.
At present, an important technical means aiming at oil product cleaning is hydrotreating, the traditional hydrotreating method is a trickle bed hydrogenation process, and a large amount of reaction heat is released in the process, and a large amount of H2 is consumed. To control the temperature rise of the catalyst bed, H2The circulation amount is large, resulting in high energy consumption of the device. And the gas phase is a continuous phase, and the liquid phase has short retention time, so that the actual reaction efficiency is low.
The liquid phase hydrogenation technology can greatly reduce the energy consumption and the investment cost of the device because a recycle hydrogen system is cancelled, and H2Dissolving in raw materials to take part in reaction, eliminating H2The influence of mass transfer, and simultaneously, the materials in the reactor contact the catalyst in a continuous liquid phase mode, so that the utilization rate of the active center of the catalyst is improved.
CN200910187765.X discloses a product recycling hydrotreatment method, which is implemented by increasing dissolved H through partial recycling of liquid-phase products2At least one stripping tray is arranged at the upper part of the reactor, and H is introduced below the stripping tray2Stripping H from the liquid phase2S and NH3Thereby improving the reaction efficiency and depth. But under high pressure conditions due to H2S and NH3The solubility in oil products is high, the gas stripping and removing effect is not obvious, and the improvement of hydrogenation reaction efficiency is limited. In addition, the method needs a high-temperature and high-pressure resistant circulating pump, the pump has high investment cost and high failure rate in the operation process, and the stable operation of the liquid phase hydrogenation device is influenced.
CN102120934B discloses a circulating liquid phase hydrogenation method, which comprises two liquid phase hydrogenation reactors connected in series, wherein the hydrogenation reaction product is cooled by a heat exchanger or is directly cooled by a heat exchanger
And the liquid phase material flow enters a hot high-pressure separation tank for gas-liquid separation, and the refined liquid phase material flow is partially circulated and returned to the inlet of each hydrogenation reactor and/or the bed layers of the hydrogenation reactors. The method adopts a hot high-pressure separation tank to carry out gas-liquid separation, H2S and NH3The separation effect is not ideal, the refining reaction depth is influenced, and a circulating pump is also used, so that the equipment investment is increased.
CN105713659A discloses a continuous liquid phase hydrogenation process for hydrocarbons, which comprises a plurality of reactors connected in series or in parallel, wherein each reactor is provided with a plurality of catalyst beds, a complex hydrogen distributor is arranged at the lower part of the catalyst bed, and a simple hydrogen mixing tank is arranged in front of the reactor. In this method, although a circulation pump and a hydrogen circulation system are eliminated, H2S and NH3The removal effect of the hydrogen distributor is not ideal, and hydrogen bubbles with the diameter of millimeter or micron are dispersed in the liquid-phase material, which causes the discontinuity of the liquid phase and influences the hydrogen mass transfer.
As the FCC raw material belongs to heavy and poor hydrocarbon oil, the process method for treating the FCC raw material by adopting liquid phase hydrogenation is not reported. Therefore, in order to solve the technical problems of the above methods, the development of a treatment method suitable for the liquid phase hydrogenation of FCC feedstock is an urgent problem to be solved in the art.
Disclosure of Invention
Aiming at the problems in the prior art, the invention provides a liquid phase hydrogenation treatment method for FCC raw materials, which cancels a circulating hydrogen and circulating oil system, adopts a proper process and invented technical equipment, increases the dissolved hydrogen amount of the FCC raw materials and the mutual solubility uniformity of the FCC raw materials and the hydrogen, not only improves the hydrogenation reaction efficiency, but also reduces the energy consumption of the device and the investment cost of the equipment.
The invention provides an FCC feed liquid phase hydroprocessing system, comprising:
the hydrogen containing unit comprises a raw material buffer tank, a feeding pump, a heat exchanger, a reaction feeding heating furnace and a first hydrogen mixer which are sequentially connected, wherein the first hydrogen mixer is connected with an inlet tank of a hydrogen compressor through the hydrogen compressor, and fresh FCC raw materials enter the heat exchanger from the raw material buffer tank through the feeding pump for heat exchange and then enter the first hydrogen mixer for full hydrogen mixing through the heating furnace;
the liquid phase hydrogenation pre-reaction unit comprises two pre-reactors which are connected with each other, inlets of the two pre-reactors are connected with an outlet of a first hydrogen mixing and mixing device, and FCC raw materials which are fully dissolved in hydrogen through the first hydrogen mixing and mixing device enter the two pre-reactors to carry out demetalization, residual carbon removal reaction and partial removal of sulfur and nitrogen compounds;
the hydrogen stripping unit comprises a hydrogen stripping tower, the hydrogen stripping tower is connected with outlets of the two pre-reactors, and pre-hydrogenated products obtained after the reaction of the two pre-reactors enter the hydrogen stripping tower for stripping;
the hydrogen re-dissolving unit is provided with a second hydrogen mixer and is connected with the inlet tank of the hydrogen compressor through the hydrogen compressor;
the main reaction unit comprises a liquid phase hydrogenation main reactor which is connected with the second hydrogen mixer to form a circulation pipeline, and the liquid phase hydrogenation main reactor is connected with the outlets of the two pre-reactors through a hydrogen stripping tower; the pre-hydrogenated product is lifted to a second hydrogen mixer through the gas of a hydrogen stripping tower and is subjected to hydrogen supplement again, and then enters a liquid-phase hydrogenation main reactor to be subjected to deep removal of sulfur, nitrogen and aromatic hydrocarbon;
the post-treatment unit comprises a pressure reducing valve, a high-temperature low-pressure flash tank and a desulphurization nitrogen tower, wherein the liquid-phase hydrogenation main reactor is connected with the high-temperature low-pressure flash tank through a pipeline provided with the pressure reducing valve, the high-temperature low-pressure flash tank is connected with a hydrogen stripping tower through a pipeline, the desulphurization nitrogen tower is respectively connected with the high-temperature low-pressure flash tank, the hydrogen stripping tower and a hydrogen compressor inlet tank, a main reaction product generated by the liquid-phase hydrogenation main reactor enters the high-temperature low-pressure flash tank for gas-liquid separation after being decompressed through the pressure reducing valve without heat exchange, an obtained liquid phase obtains a refined product through heat exchange, and an obtained gas phase is mixed with a gas phase of a hydrogen stripping tower and then returns.
In one embodiment, the cavity of the main liquid phase hydrogenation reactor is internally provided with a reactor inlet area, a reactor reaction area and a reactor outlet area which are communicated with each other from top to bottom;
the reactor inlet area is provided with a reactor inlet for injecting hydrocarbon oil, an inlet distributor for primarily distributing the hydrocarbon oil, a plurality of hydrogen feeding pipes for injecting hydrogen and a plurality of hydrogen mixers for mixing the hydrocarbon oil and the hydrogen, the outlet of the inlet distributor is communicated with the inlet of the hydrogen mixer, and the hydrogen feeding pipes are communicated with the hydrogen mixer;
the reactor reaction zone comprises a plurality of groups of reaction tubes, and each reaction tube is communicated with one hydrogen mixer;
and the outlet area of the reactor is provided with a regular packing type outlet collector and a reactor outlet, one side of the regular packing type outlet collector is connected with the reaction tubes, the other side of the regular packing type outlet collector is connected with the reactor outlet, and the reactor outlet is communicated with the outside.
In one embodiment, the hydrogen mixer comprises:
the hydrogen mixer body is internally provided with a cavity, and one end of the cavity is communicated with a feed inlet pipe;
the chamber is also internally provided with N +1 stages of hydrogen mixers which are sequentially connected in series step by step along the material inflow direction, N is more than or equal to 1 and is a natural number, each stage of the hydrogen mixer comprises a hydrogen mixing area and a filler mixing area which are mutually communicated, the filler mixing area of the previous stage is connected with the filler mixing area of the next stage, the hydrogen mixing area is provided with a gas-liquid mixing pipe, the gas-liquid mixing pipe is connected with the hydrogen feeding pipe, the number of gas-liquid mixing pipes in a hydrogen mixing area of the next-stage hydrogen mixer is larger than that of the gas-liquid mixing pipes of the previous-stage hydrogen mixer, the size of the gas-liquid mixing pipes in the hydrogen mixing area of the next-stage hydrogen mixer is smaller than that of the gas-liquid mixing pipes of the previous-stage hydrogen mixer, the gas-liquid mixing pipes of each stage of the hydrogen mixer are of a multilayer concentric circle uniform distribution structure, a discharge hole of the last-stage (N + 1) th gas-liquid mixing pipe penetrates through the hydrogen mixer body to be communicated with the outside, and an isolation net is arranged between the mixing area of the previous-stage and the mixing area of the next-stage; an isolation net is arranged between the hydrogen mixing area and the filler mixing area, and fillers in the filler mixing area can be selected according to the properties of hydrocarbon oil and are graded and filled according to a certain proportion.
In an embodiment, the reactor inlet area is further provided with a structured packing type inlet dispersion layer and a support disc, the structured packing type inlet dispersion layer is composed of an inert material or a structured metal packing and is filled between the reactor inlet and the inlet distributor, the support disc is fixed on the wall of the liquid phase hydrogenation main reactor, the structured packing type inlet dispersion layer is placed on the support disc, the inlet of the gas-liquid mixing pipe is connected with the inlet pipe, and the hydrogen mixer inlet pipe penetrates through the support disc to be connected with the structured packing type inlet dispersion layer.
In one embodiment, the gas-liquid mixing pipe is provided with a low-pressure inlet chamber, a throat and a diffusion pipe which are connected in sequence, a nozzle is arranged in the low-pressure inlet chamber, spoilers are arranged in the throat and the diffusion pipe respectively, the hydrogen inlet pipe is communicated with the low-pressure inlet chamber, and a plurality of spoilers are arranged in the throat and the diffusion pipe; the diameter of the diffusion pipe is gradually increased along the material inflow direction; the spoiler is welded on the inner walls of the throat pipe and the diffusion pipe in a spiral annular mode.
In one embodiment, the two prereactors of the liquid phase hydrogenation prereaction unit run in parallel or in a single switching mode, the prereactor is a conventional fixed bed reactor, at least two catalyst beds are arranged in the prereactor, and the heights of the catalyst beds are gradually increased along the direction of reactant flow.
In one embodiment, the liquid phase hydrogenation main reactor preferably selects at least one main reactor according to different raw material combinations, when a process scheme of a plurality of main reactors is used, a series operation mode is adopted among the main reactors, and a hydrogen mixer is arranged before the next stage of main reactor.
The invention also provides a liquid phase hydroprocessing process for FCC feedstocks,
step 1, fresh FCC raw material is subjected to heat exchange by a heat exchanger and is heated by a heating furnace and is fully mixed with hydrogen by a first hydrogen mixer;
step 2, after the step 1, feeding the hydrogen-dissolved FCC raw material into a pre-reactor of a liquid phase hydrogenation pre-reaction unit for demetalization, carbon residue removal reaction and partial removal of sulfide and nitride;
step 3, mixing the pre-reaction product generated in the step 2 with hydrogen again through a hydrogen stripping unit and a second hydrogen mixer, and then feeding the mixed product into a liquid phase hydrogenation main reactor of a main reaction unit to deeply remove sulfides, nitrides and aromatic hydrocarbons;
and 4, the main reaction product generated in the step 3 enters a high-temperature and low-pressure flash tank for gas-liquid separation after pressure reduction without heat exchange, the obtained liquid-phase material is subjected to heat exchange to obtain a refined product, and the obtained gas-phase material and the gas-phase material of the gas stripping tower are mixed, enter a desulfurizing nitrogen tower and then return to an inlet tank of a hydrogen compressor or exit the system.
In one embodiment, the operation conditions of the pre-reactor of the liquid phase hydrogenation pre-reaction unit are as follows: the reaction temperature is 320-400 ℃, the reaction pressure is 8.0-15.0 MPa, and the liquid hourly space velocity is 1.0-4.0 h-1The volume ratio of hydrogen to oil is 10-100.
In one embodiment, the liquid phase hydrogenation main reactor operating conditions of the main reaction unit are as follows: the reaction temperature is 280-390 ℃, the reaction pressure is 6.0-15.0 MPa, and the liquid hourly space velocity is 0.5-2.0 h-1The volume ratio of hydrogen to oil is 10-100.
In one embodiment, the catalyst used in the pre-reactor and the liquid phase hydrogenation main reactor may be a commercial catalyst, or may be prepared according to the prior art in the field.
In one embodiment, the FCC feedstock is at least one of a mixture of VGO, CGO, AR, VR.
The invention relates to a fluid phase hydrogenation treatment system and a method of FCC (fluid catalytic cracking) raw materials, which have the advantages that: a circulating hydrogen compressor system and a high-temperature and high-pressure liquid circulating pump are omitted, the volumes of the pre-reactor and the main reactor are smaller, the investment cost of the device is reduced, the use amount of the catalyst is small, and the reaction efficiency is improved; the process of connecting two pre-reactors in parallel or switching operation and connecting at least one tubular main reactor in series is adopted, and the device has higher operation flexibility on the premise of ensuring the hydrofining depth; sufficient and appropriate amount of hydrogen is dissolved in continuous liquid phase FCC raw material soaked with catalyst, and H is generated by reaction2S and NH3Harmful impurities are removed in time through special equipment at the bottom of the main reactor and a hydrogen stripping tower, so that the reaction efficiency is improved, and the reaction depth is enhanced; the main reactor fully utilizes the heat generated by the reaction in a tube array mode, and the liquid-phase reactant flow takes away the reaction heat in time, so that the temperature wave of a reaction system is small; the multi-point injection of hydrogen can not only realize the timely supplement of hydrogen consumption, but also effectively avoid excessive hydrogen bubbles in the catalyst bed layer, thereby influencing the liquid phase hydrogenation reaction efficiency.
Drawings
FIG. 1 is a process flow diagram of the FCC feed liquid phase hydroprocessing process of the present invention.
FIG. 2 is a schematic diagram of a main reactor for liquid phase hydrogenation.
FIG. 3 is a schematic view of the structure of the hydrogen mixer.
Fig. 4 is a schematic view of the gas-liquid mixing pipe.
The reference numbers in the figures are:
reference numerals in fig. 1:
1. the device comprises a hydrogen compressor inlet tank, 2, a hydrogen compressor, 3, a raw material buffer tank, 4, a feeding pump, 5, a heat exchanger, 6, a reaction feeding heating furnace, 7, a first hydrogen mixer, 8, an automatic control valve, 9-1, 1# pre-reactor, 9-2, 2# pre-reactor, 10, a hydrogen gas stripping tower, 11, a liquid phase hydrogenation main reactor, 12, a second hydrogen mixer, 13, a pressure reducing valve, 14, a high-temperature low-pressure flash tank, 15 and a desulfurization nitrogen tower.
The reference numerals in fig. 2 are:
3001 reactor inlet, 3002, manhole, 300 inlet distributor, 300 structured packing type inlet dispersion layer, 3005 support disc, 3006 inlet pipe, 3007, hydrogen inlet pipe, 3008 hydrogen mixer, 3009 upper support disc, 3010 heat exchange material outlet, 3011 reaction tube set, 3012 reactor wall, 3013 shell pass, 3014 cold material inlet, 3015 lower support disc, 3016 structured packing type outlet collector, 3017 reactor outlet, 3018 discharging agent pipe mouth, 3019 waste gas outlet.
The reference numerals in fig. 3 are:
a hydrogen mixer body 100, a first stage filler mixing zone 1001, a second stage filler mixing zone 1002; a first-stage gas-liquid mixing pipe 1003, a second-stage gas-liquid mixing pipe 1004, separation nets 1005, 1006 and 1007 and a first-stage hydrogen mixing area 1008; a second stage hydrogen mixing area 1009, and fillers 1010, 1011.
The reference numerals in fig. 4 are:
2000. nozzle 2001, low pressure inlet chamber, 2002, throat, 2003, diffuser, 2004, spoiler, 3007, hydrogen feed pipe.
Detailed Description
The detailed description and technical contents of the present invention are described below with reference to the drawings:
the FCC feedstock liquid phase hydroprocessing system and method of the present invention are described in detail below with reference to the drawings.
As shown in fig. 1, the hydrogen-containing unit includes a raw material buffer tank 3, a feed pump 4, a heat exchanger 5, a reaction feed heating furnace 6 and a first hydrogen mixer 7 which are connected in sequence, the first hydrogen mixer 7 is connected with a hydrogen compressor inlet tank 1 through a hydrogen compressor 2, and fresh FCC raw material enters the heat exchanger 5 from the raw material buffer tank 3 through the feed pump 4 for heat exchange and then enters the first hydrogen mixer 7 through the reaction feed heating furnace 6 for heating to fully mix hydrogen.
The liquid phase hydrogenation pre-reaction unit comprises two pre-reactors connected in parallel, inlets of the two pre-reactors (the No. 1 pre-reactor 9-1 and the No. 2 pre-reactor 9-2) are connected with an outlet of a first hydrogen mixing and mixing device 7 through a pipeline provided with an automatic control valve 8, and FCC raw materials which are fully dissolved in hydrogen through the first hydrogen mixing and mixing device 7 enter the two pre-reactors to carry out demetalization and residual carbon removal reactions and partial removal of sulfur and nitrogen compounds.
The hydrogen stripping unit comprises a hydrogen stripping tower 10, the hydrogen stripping tower 10 is connected with outlets of the two prereactors, and a prehydrogenation product obtained after the reaction of the two prereactors enters the hydrogen stripping tower 10 for stripping. The hydrogen stripper 10 is connected to a hydrogen injection line.
And the hydrogen re-dissolving unit is provided with a second hydrogen mixer 12 which is connected with the hydrogen compressor 2 and the hydrogen compressor inlet tank 1.
The main reaction unit is provided with a liquid phase hydrogenation main reactor 11 which is respectively connected with a second hydrogen mixer 12 and a hydrogen stripping tower 10; the pre-hydrogenated product is re-hydrogenated in a hydrogen stripping tower 10 and a second hydrogen mixer 12, and then enters a liquid phase hydrogenation main reactor 11 for deep removal of sulfur, nitrogen and aromatic hydrocarbon.
The post-treatment unit comprises a pressure reducing valve 13, a high-temperature low-pressure flash tank 14 and a desulfurization nitrogen tower 15, wherein the liquid-phase hydrogenation main reactor 11 is connected with the high-temperature low-pressure flash tank 14 through a pipeline provided with the pressure reducing valve 13, the high-temperature low-pressure flash tank 14 is connected with a hydrogen stripping tower 10 through a pipeline, and the desulfurization nitrogen tower 15 is respectively connected with the high-temperature low-pressure flash tank 14, the hydrogen stripping tower 10 and a hydrogen compressor inlet tank 1. The main reaction product generated by the liquid phase hydrogenation main reactor 11 is decompressed by a decompression valve 13 without heat exchange and enters a high-temperature low-pressure flash tank 14 for gas-liquid separation, the obtained liquid phase is subjected to heat exchange to obtain a refined product, and the obtained gas phase and the gas phase of the hydrogen stripping tower 10 are mixed and enter a nitrogen-removing tower 15 and then return to a hydrogen compressor inlet tank or are discharged out of the treatment system. The liquid phase hydrogenation pre-reactor is designed as a double-reactor, the two reactors can be operated in parallel or switched to operate singly, the reactor is a conventional fixed bed reactor, at least two catalyst bed layers are arranged in the reactor, and the height of the catalyst bed layers is increased step by step along the direction of reactant flow. The liquid phase hydrogenation main reactor 11 preferably selects at least one reactor according to different raw material combinations, when a process scheme of a plurality of main reactions is used, a series operation mode is adopted among the main reactions, and a hydrogen mixer is arranged in front of the next stage reactor.
The hydrogenation catalyst used in the invention can adopt a commercial heavy oil hydrotreating catalyst or a self-made catalyst according to the technology in the field, at least two of Co, Mo, Ni and W are generally used as active components, alumina or silicon-containing alumina is used as a carrier, and the main physical properties of the carrier need to meet the following requirements: specific surface area>250m2G, pore volume>0.4mL/g。
Referring to fig. 2, the structure of the main liquid phase hydrogenation reactor in fig. 2 is shown schematically. The cavity of the main liquid phase hydrogenation reactor 11 is internally provided with a reactor inlet area, a reactor reaction area and a reactor outlet area which are communicated with each other from top to bottom.
The inlet area of the reactor is provided with a reactor inlet 3001 for injecting hydrocarbon oil, an inlet distributor 3003 for primarily distributing hydrocarbon oil, a plurality of hydrogen feeding pipes 3007 for injecting hydrogen, a manhole 3002 for overhauling and a plurality of hydrogen mixers 3008 for mixing hydrocarbon oil and hydrogen, the outlet of the inlet distributor 3003 is communicated with the inlet of the hydrogen mixer 3008, and the hydrogen feeding pipe is communicated with the hydrogen mixer 3008; the reaction zone of the reactor comprises a plurality of groups of reaction tubes which are arranged in parallel along the axial direction of the main reactor, the upper and lower ends of the reaction tube set 3011 are respectively provided with a support disc, and the upper support disc 3009 and the lower support disc 3015 are used for fixing the reaction tube set 3011. The adopted reaction tubes are tubes with a height-diameter ratio, the hydrogen mixer 3008 is correspondingly connected with the inlets of the reaction tubes in the reaction area of the reactor one by one, the outlet ends of the reaction tubes are connected with the structured packing type outlet collector 3016 in the outlet area of the reactor, the structured packing type outlet collector 3016 is connected with the outlet 3017 of the reactor, and the outlet 3017 of the reactor is communicated with the outside. The wall of the reactor corresponding to the reaction zone of the reactor is provided with a cold raw material inlet 3014 and a heat-exchanged raw material outlet 3010 for recycling the hydrocarbon oil. When the device is in a start-up state, hydrocarbon oil enters the inlet 1 of the reactor after being heated by the heat exchanger and the heating furnace from the heat-exchanged raw material outlet 3010 of the reactor.
The hydrocarbon oil enters a reactor inlet distributor 3003 through a reactor inlet 1 for preliminary distribution, then is redistributed through a structured packing type inlet dispersing layer 3004, then enters a hydrogen mixer 3008 to realize that the hydrocarbon oil fully dissolves hydrogen and part of excessive hydrogen forms micro bubbles to be uniformly dispersed in the hydrocarbon oil, the hydrocarbon oil dissolving the hydrogen continuously enters a reactor tubular group for hydrogenation reaction and completes heat exchange with cold hydrocarbon oil of a shell side 3013, the hydrogenated hydrocarbon oil enters a reactor outlet 3017 through a structured packing type outlet collector 3016 to realize partial removal of impurities such as hydrogen sulfide and ammonia generated in the reaction process, and then is further processed by other separation equipment to obtain a hydrogenation product.
The inlet dispersion layer 3004 of structured packing type is composed of inert material or structured metal packing and is filled between the reactor inlet and the inlet distributor 3003, a support disc 3005 is fixed on the reactor wall 3012, and the inlet dispersion layer 3004 of structured packing type is placed on the support disc 3005. The inlet of the hydrogen mixer 3008 is connected with a feed inlet pipe 3006 of the hydrogen mixer 3008, and the feed inlet pipe 3006 of the hydrogen mixer 3008 penetrates through the supporting disc to be connected with the structured packing type inlet dispersion layer.
The outlet area of the reactor is also provided with a discharging agent pipe orifice 3018 and at least one waste gas outlet orifice 3019, the discharging agent pipe orifice 3018 is arranged on the wall of the reactor, and the waste gas outlet orifice 3019 is communicated with the outlet of the reactor. By adopting the preferable hydrogen mixer 3008, the hydrogen is fully dissolved in the liquid-phase hydrocarbon oil and reaches a supersaturated state, and the excessive hydrogen forms micro bubbles to be uniformly dispersed in the liquid-phase hydrocarbon oil, thereby being beneficial to deep hydrogenation; the tube array group with larger height-diameter ratio is adopted, so that the use amount of the catalyst is reduced, the utilization rate of the catalyst is improved, the retention time of reaction materials is prolonged, the equipment investment is reduced, and the product quality is improved.
As shown in fig. 3, fig. 3 is a schematic view of the structure of the hydrogen mixer. The hydrogen mixer 3008 comprises a hydrogen mixer body and a multi-stage gas-liquid mixing pipe, wherein a cavity is arranged in the hydrogen mixer body, and one end of the cavity is communicated with a feed inlet pipe 3006 of the hydrogen mixer 3008; still be equipped with in the cavity along the material inflow direction in order series connection's N +1 level mix hydrogen ware step by step, N more than or equal to 1, N is the natural number, each level mix hydrogen ware including the hydrogen district that mixes of intercommunication, the filler mixed region of preceding one-level is connected with the filler mixed region of back one-level, it is equipped with the gas-liquid mixing pipe to mix the hydrogen district, the gas-liquid mixing pipe is connected with the hydrogen inlet pipe, and the gas-liquid mixing pipe quantity in the hydrogen district that mixes of back one-level mixes hydrogen ware will be greater than the gas-liquid mixing pipe quantity of preceding one-level and mix the hydrogen ware, the size of the gas-liquid mixing pipe in the hydrogen district that mixes of back one-level and mix the hydrogen ware is less than the size of the gas-liquid mixing pipe of the hydrogen ware of preceding one-level, the gas-liquid mixing pipe of each level of hydrogen ware all is multilayer concentric circle evenly distributed structure, the discharge gate of.
In this embodiment, the hydrogen mixer is provided with a two-stage hydrogen mixer, referring to fig. 3, the first-stage hydrogen mixer 100 includes a first-stage hydrogen mixing region 1008 and a first-stage filler mixing region 1001, the second-stage hydrogen mixer 101 includes a second-stage hydrogen mixing region 1009 and a second-stage filler mixing region 1002, the first-stage filler mixing region 1001 is connected to the second-stage filler mixing region 1002, the first-stage hydrogen mixing region 1008 has a first-stage gas-liquid mixing pipe 1003, the second-stage hydrogen mixing region is provided with 4 second-stage gas-liquid mixing pipes 1004, the diameter of the first-stage gas-liquid mixing pipe 1003 is larger than that of the second-stage gas-liquid mixing pipe 1004, the outlet of the first-stage gas-liquid mixing pipe is connected to the first-stage hydrogen mixing region through an isolation net 1005, the second-stage hydrogen mixer feed inlet 1005 of the second-stage gas-liquid mixing pipe 1004 is connected to the second-stage filler mixing region 1002 through an isolation net 1006, and an isolation net 1007 is provided between.
It should be noted that, in the present invention, the gas-liquid mixing pipes at each stage have the same structure and only have a difference in size, each gas-liquid mixing pipe includes a low-pressure gas inlet chamber, a throat pipe and a diffuser pipe which are sequentially communicated, and a nozzle is arranged in the low-pressure gas inlet chamber. The low-pressure inlet chamber and the nozzle constitute the feed inlet of the hydrogen mixer, and in this embodiment, referring to fig. 4, fig. 4 is a schematic view of the gas-liquid mixing pipe. The gas-liquid mixing pipe has a low pressure inlet chamber 2001, a throat 2002 and a diffuser 2003 connected in sequence, a nozzle 2000 is installed in the low pressure inlet chamber 2001, spoilers 2004 are installed in the throat 2002 and the diffuser 2003, the low pressure inlet chamber 2001 is a flared inlet chamber which is gradually reduced in diameter from the inlet of the low pressure inlet chamber, and the hydrogen gas feed pipe 3007 is communicated with the low pressure inlet chamber 2001. The spoiler 2004 is installed in a spiral ring shape in the throat 2002 and the diffuser 2003. The diameter of the diffusion pipe is gradually increased along the material inflow direction, the low-pressure air inlet chamber is a flaring chamber, and the diameter of the low-pressure air inlet chamber is gradually decreased along the material inflow direction.
It is worth mentioning that the fillers 1010 and 1011 can be selected from fillers of corresponding types according to the properties of actual hydrocarbon oil, and are graded and filled according to a certain proportion; the hydrogen mixer is of a cylindrical structure. The gas-liquid mixing pipe is of a multilayer concentric circle uniform distribution structure, and the size of the gas-liquid mixing pipe is gradually reduced.
Naphtha, kerosene, diesel oil and light distillate oil with low impurity content are processed, the hydrogen mixing amount is required to be small, a hydrocarbon oil liquid phase hydrogenation hydrogen mixer adopts a primary series connection secondary mode as shown in figure 2, and the hydrocarbon oil liquid phase hydrogenation hydrogen mixer is arranged in front of a hydrogenation reactor to work.
When processing inferior heavy distillate oil such as VGO, CGO, atmospheric residue oil and mixtures thereof, and the like, a large hydrogen mixing amount is needed at the moment, the hydrocarbon oil liquid phase hydrogenation hydrogen mixer adopts at least more than two stages of hydrogen mixers, the number of gas-liquid mixing pipes of the next stage is larger than that of the gas-liquid mixing pipes of the previous stage, and the hydrogen mixing method is compared with the conventional hydrogenation system hydrogen mixing method, so that the invention obviously improves the hydrogen mixing amount in the liquid phase hydrocarbon oil by adopting a mixing area which is designed in a multi-stage mode, is diffused step by step and is filled with multiple types of fillers in a grading manner, and is beneficial to deep hydrogenation of the hydrocarbon oil; the gas-liquid mixing pipes are distributed step by step and uniformly according to a certain proportion, so that uniform mixing of hydrocarbon oil and hydrogen is facilitated; the method has the advantages of modular design, convenient installation and flexible matching according to the properties, the processing amount, the refining depth and other conditions of the actually processed hydrocarbon oil.
The liquid phase hydrotreating method of FCC raw material comprises the following steps:
step 1, fresh FCC raw material is subjected to heat exchange by a heat exchanger and is heated by a heating furnace and is fully mixed with hydrogen by a first hydrogen mixer;
step 2, feeding the FCC raw material with dissolved hydrogen into a pre-reactor of a liquid phase hydrogenation pre-reaction unit for demetalization, carbon residue removal reaction and partial removal of sulfide and nitride;
3, mixing the pre-reaction product generated in the step 2 again with hydrogen through a hydrogen stripping unit and a second hydrogen mixer, and then feeding the mixed product into a main reaction unit for deep removal of sulfide, nitride and aromatic hydrocarbon;
and 4, the main reaction product generated in the step 3 enters a high-temperature and low-pressure flash tank for gas-liquid separation after pressure reduction without heat exchange, the obtained liquid-phase material is subjected to heat exchange to obtain a refined product, and the obtained gas-phase material and the gas-phase material of the gas stripping tower are mixed and enter a desulfurizing nitrogen tower and then return to an inlet tank or an outlet device of a hydrogen compressor.
The operating conditions of the two prereactors of the liquid phase hydrogenation prereaction unit are as follows: the reaction temperature is 320-400 ℃, the reaction pressure is 8.0-15.0 MPa, the liquid hourly space velocity is 1.0-4.0 h < -1 >, and the volume ratio of hydrogen to oil is 10-100.
The operating conditions of the liquid phase hydrogenation main reactor of the main reaction unit are as follows: the reaction temperature is 280-390 ℃, the reaction pressure is 6.0-15.0 MPa, the liquid hourly space velocity is 0.5-2.0 h < -1 >, and the volume ratio of hydrogen to oil is 10-100.
The catalyst used in the pre-reactor and the liquid phase hydrogenation main reactor can be a commercial catalyst or can be prepared according to the prior art in the field.
The FCC raw material is at least one of a mixture composed of VGO, CGO, AR and VR.
The technical means and effects of the present invention will be described below by way of examples.
Examples 1 to 4. Example 1 is a process configuration in which two prereactors are operated in parallel and a main reactor is connected in series; example 2 is a process in which two pre-reactors are switched to operate and a main reactor is connected in series; example 3 is a process configuration in which two pre-reactors are operated in parallel and two main reactors are connected in series; example 4 is a process configuration in which two prereactors are switched into operation, with two main reactors connected in series.
Examples 1 to 4 the process flow shown in fig. 1 of the present invention was used, the properties of the raw materials used are shown in table 1, the process conditions used in examples 1 to 4 are shown in table 2, and the evaluation results of examples 1 to 4 are shown in table 3.
TABLE 1 Properties of the stock oils
Figure BDA0001995300280000111
TABLE 2 operating conditions used in examples 1 to 4
Figure BDA0001995300280000112
Table 3 evaluation results
Figure BDA0001995300280000113
When the pre-reactor and the main reactor adopt the four different combination forms, under the conditions of the same raw material, reaction temperature and reaction pressure, the refining depths are different, wherein the sulfur and nitrogen contents of the product of the embodiment 3 are the lowest. If the severity of the reaction conditions is increased, examples 1, 2 and 4 can also achieve desulfurization and denitrification rates comparable to example 3, but with corresponding increases in energy consumption and operating costs.
The invention adopts the liquid phase hydrogenation main reactor, the volume of the reactor is smaller than that of the traditional liquid phase hydrogenation reactor, the usage amount of the catalyst is less, and the reaction efficiency is improved, so the number of the reactors can be properly increased according to the characteristics of raw materials and the limit value of product impurities.
The technical advantages of the invention are as follows: compared with the conventional hydrogenation system, the invention obviously improves the mixing amount of hydrogen in liquid-phase hydrocarbon oil by adopting a mixing area with multi-stage design, gradual diffusion and multi-type filler graded filling, and is beneficial to deep hydrogenation of the hydrocarbon oil; the gas-liquid mixing pipes are distributed step by step and uniformly according to a certain proportion, so that uniform mixing of hydrocarbon oil and hydrogen is facilitated; the method has the advantages of modular design, convenient installation and flexible matching according to the properties, the processing amount, the refining depth and other conditions of the actually processed hydrocarbon oil.
The foregoing is considered as illustrative only of the principles, general features and advantages of the invention, and not as limiting the invention, which is to be read in connection with the following claims. In addition, equivalent transformations performed by those skilled in the art according to the technical solutions disclosed in the present invention are still considered to be within the scope of the present invention.

Claims (12)

1. An FCC feedstock liquid phase hydroprocessing system, comprising:
the hydrogen containing unit comprises a raw material buffer tank, a feeding pump, a heat exchanger, a reaction feeding heating furnace and a first hydrogen mixer which are sequentially connected, wherein the first hydrogen mixer is connected with an inlet tank of a hydrogen compressor through the hydrogen compressor, and fresh FCC raw materials enter the heat exchanger from the raw material buffer tank through the feeding pump for heat exchange and then enter the first hydrogen mixer for full hydrogen mixing through the heating furnace;
the liquid phase hydrogenation pre-reaction unit comprises two pre-reactors which are connected with each other, inlets of the two pre-reactors are connected with an outlet of a first hydrogen mixing and mixing device, and FCC raw materials which are fully dissolved in hydrogen through the first hydrogen mixing and mixing device enter the two pre-reactors to carry out demetalization, residual carbon removal reaction and partial removal of sulfur and nitrogen compounds;
the hydrogen stripping unit comprises a hydrogen stripping tower, the hydrogen stripping tower is connected with outlets of the two pre-reactors, and pre-hydrogenated products obtained after the reaction of the two pre-reactors enter the hydrogen stripping tower for stripping;
the hydrogen re-dissolving unit is provided with a second hydrogen mixer and is connected with the inlet tank of the hydrogen compressor through the hydrogen compressor;
the main reaction unit comprises a liquid phase hydrogenation main reactor and is connected with the second hydrogen mixer to form a circulating pipeline, and the liquid phase hydrogenation main reactor is connected with outlets of the two pre-reactors through the hydrogen stripping tower; the pre-hydrogenated product is lifted by the gas of the hydrogen stripping tower and the second hydrogen mixer for re-hydrogen supplement and then enters the liquid phase hydrogenation main reactor for deep removal of sulfur, nitrogen and aromatic hydrocarbon;
the post-processing unit comprises a pressure reducing valve, a high-temperature low-pressure flash tank and a desulfurizing nitrogen tower, wherein the liquid-phase hydrogenation main reactor is connected with the high-temperature low-pressure flash tank through a pipeline provided with the pressure reducing valve, the high-temperature low-pressure flash tank is connected with the hydrogen gas stripping tower through a pipeline, the desulfurizing nitrogen tower is respectively connected with the high-temperature low-pressure flash tank, the hydrogen gas stripping tower and a hydrogen compressor inlet tank, a main reaction product generated by the liquid-phase hydrogenation main reactor does not enter the high-temperature low-pressure flash tank for gas-liquid separation after being subjected to pressure reduction through the pressure reducing valve through heat exchange, an obtained liquid phase obtains a refined product through heat exchange, and an obtained gas phase and a gas phase of the hydrogen gas stripping tower are mixed and enter.
2. The FCC feed liquid phase hydroprocessing system of claim 1,
the cavity of the main liquid phase hydrogenation reactor is internally provided with a reactor inlet area, a reactor reaction area and a reactor outlet area which are communicated with each other from top to bottom;
the reactor inlet area is provided with a reactor inlet for injecting hydrocarbon oil, an inlet distributor for primarily distributing the hydrocarbon oil, a plurality of hydrogen feeding pipes for injecting hydrogen and a plurality of hydrogen mixers for mixing the hydrocarbon oil and the hydrogen, the outlet of the inlet distributor is communicated with the inlet of the hydrogen mixer, and the hydrogen feeding pipes are communicated with the hydrogen mixer;
the reactor reaction zone comprises a plurality of groups of reaction tubes, and each reaction tube is communicated with one hydrogen mixer;
and the outlet area of the reactor is provided with a regular packing type outlet collector and a reactor outlet, one side of the regular packing type outlet collector is connected with the reaction tubes, the other side of the regular packing type outlet collector is connected with the reactor outlet, and the reactor outlet is communicated with the outside.
3. The FCC feedstock liquid phase hydroprocessing system of claim 2, wherein the hydrogen mixer comprises:
the hydrogen mixer body is internally provided with a cavity, and one end of the cavity is communicated with a feed inlet pipe;
the chamber is also internally provided with N +1 stages of hydrogen mixers which are sequentially connected in series step by step along the material inflow direction, N is more than or equal to 1 and is a natural number, each stage of the hydrogen mixer comprises a hydrogen mixing area and a filler mixing area which are mutually communicated, the filler mixing area of the previous stage is connected with the filler mixing area of the next stage, the hydrogen mixing area is provided with a gas-liquid mixing pipe, the gas-liquid mixing pipe is connected with the hydrogen feeding pipe, the number of gas-liquid mixing pipes in a hydrogen mixing area of the next-stage hydrogen mixer is larger than that of the gas-liquid mixing pipes of the previous-stage hydrogen mixer, the size of the gas-liquid mixing pipes in the hydrogen mixing area of the next-stage hydrogen mixer is smaller than that of the gas-liquid mixing pipes of the previous-stage hydrogen mixer, the gas-liquid mixing pipes of each stage of the hydrogen mixer are of a multilayer concentric circle uniform distribution structure, a discharge port of the (N + 1) -th-stage gas-liquid mixing pipe penetrates through the hydrogen mixer body to be communicated with the outside, and an isolation net is arranged between the mixing area of the previous-stage and the mixing area of the next-stage; an isolation net is arranged between the hydrogen mixing area and the filler mixing area, and fillers in the filler mixing area can be selected according to the properties of hydrocarbon oil and are graded and filled according to a certain proportion.
4. The FCC feedstock liquid phase hydroprocessing system of claim 3, wherein the reactor inlet zone is further provided with a structured packing type inlet dispersion layer composed of inert material or structured metal packing filled between the reactor inlet and the inlet distributor, a support disc fixed on the wall of the main liquid phase hydrogenation reactor, the structured packing type inlet dispersion layer being placed on the support disc, the inlet of the gas-liquid mixing tube being connected to the inlet tube, and the inlet tube being connected to the structured packing type inlet dispersion layer through the support disc.
5. The FCC feed liquid phase hydroprocessing system of claim 3, wherein the gas-liquid mixing pipe has a low pressure inlet chamber, a throat and a diffuser connected in series, the low pressure inlet chamber having a nozzle mounted therein, and wherein baffles are provided in both the throat and the diffuser, the hydrogen feed pipe is in communication with the low pressure inlet chamber, and a plurality of baffles are provided in the throat and the diffuser; the diameter of the diffusion pipe is gradually increased along the material inflow direction; the spoiler is welded on the inner walls of the throat pipe and the diffusion pipe in a spiral annular mode.
6. The FCC feedstock liquid phase hydroprocessing system of claim 1, wherein the liquid phase hydrogenation pre-reaction unit has two pre-reactors operating in parallel or in single switching operation, the pre-reactors are conventional fixed bed reactors with at least two catalyst beds inside, and the catalyst bed heights increase step by step along the reactant flow direction.
7. The FCC feed liquid phase hydroprocessing system of claim 3, said liquid phase hydroprocessing main reactor prefers at least one main reactor for different feedstock combinations, when a multiple main reactor process scheme is used, a series operation is used between each main reactor, and a hydrogen mixer is placed before the next main reactor.
8. A liquid phase hydrogenation processing method of FCC raw material is characterized in that:
step 1, fresh FCC raw material is subjected to heat exchange by a heat exchanger and is heated by a heating furnace and is fully mixed with hydrogen by a first hydrogen mixer;
step 2, after the step 1, feeding the hydrogen-dissolved FCC raw material into a pre-reactor of a liquid phase hydrogenation pre-reaction unit for demetalization, carbon residue removal reaction and partial removal of sulfide and nitride;
step 3, mixing the pre-reaction product generated in the step 2 with hydrogen again through a hydrogen stripping unit and a second hydrogen mixer, and then feeding the mixed product into a liquid phase hydrogenation main reactor of a main reaction unit to deeply remove sulfides, nitrides and aromatic hydrocarbons;
and 4, the main reaction product generated in the step 3 enters a high-temperature and low-pressure flash tank for gas-liquid separation after pressure reduction without heat exchange, the obtained liquid-phase material is subjected to heat exchange to obtain a refined product, and the obtained gas-phase material and the gas-phase material of the gas stripping tower are mixed, enter a desulfurizing nitrogen tower and then return to an inlet tank of a hydrogen compressor or exit the system.
9. The FCC feedstock liquid phase hydroprocessing process of claim 8, wherein: the operation conditions of the pre-reactor of the liquid phase hydrogenation pre-reaction unit are as follows: the reaction temperature is 320-400 ℃, the reaction pressure is 8.0-15.0 MPa, and the liquid hourly space velocity is 1.0-4.0 h-1The volume ratio of hydrogen to oil is 10-100.
10. The FCC feedstock liquid phase hydroprocessing process of claim 8, wherein: the operating conditions of the liquid phase hydrogenation main reactor of the main reaction unit are as follows: the reaction temperature is 280-390 ℃, the reaction pressure is 6.0-15.0 MPa, and the liquid hourly space velocity is 0.5-2.0 h-1The volume ratio of hydrogen to oil is 10-100.
11. The FCC feedstock liquid phase hydroprocessing process of claim 8, wherein: the catalyst used in the pre-reactor and the liquid phase hydrogenation main reactor can be a commercial catalyst or can be prepared according to the prior art in the field.
12. The FCC feedstock liquid phase hydroprocessing process of claim 8, wherein: the FCC raw material is at least one of a mixture composed of VGO, CGO, AR and VR.
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