CN107267211B - A kind of processing method and system of inferior feedstock oil - Google Patents

A kind of processing method and system of inferior feedstock oil Download PDF

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Publication number
CN107267211B
CN107267211B CN201610211678.3A CN201610211678A CN107267211B CN 107267211 B CN107267211 B CN 107267211B CN 201610211678 A CN201610211678 A CN 201610211678A CN 107267211 B CN107267211 B CN 107267211B
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oil
catalytic cracking
hydrogen
catalyst
cracking catalyst
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CN107267211A (en
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唐津莲
龚剑洪
李泽坤
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Sinopec Research Institute of Petroleum Processing
China Petroleum and Chemical Corp
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Sinopec Research Institute of Petroleum Processing
China Petroleum and Chemical Corp
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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
    • C10G67/06—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 including a sorption process as the refining step in the absence of hydrogen
    • 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
    • C10G67/14—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 including at least two different refining steps in the absence of hydrogen
    • 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
    • C10G2300/20—Characteristics of the feedstock or the products
    • C10G2300/201—Impurities
    • C10G2300/202—Heteroatoms content, i.e. S, N, O, P
    • 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
    • C10G2300/20—Characteristics of the feedstock or the products
    • C10G2300/201—Impurities
    • C10G2300/205—Metal content

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  • Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)

Abstract

The invention discloses a kind of processing method of inferior feedstock oil and systems, this method comprises: a, the fluidized bed that hydrogen-containing gas and inferior feedstock oil are sent into fluidized bed riser reactor is faced contacting in hydrogen adsorption zone (I) with the first catalytic cracking catalyst and carrying out facing hydrogen adsorption reaction, obtain facing hydrogen adsorbed product；B, gained in step a is faced hydrogen adsorbed product and is sent into and contact and carry out catalytic cracking reaction in the riser cracking area (II) of the fluidized bed riser reactor with the second catalytic cracking catalyst, obtain catalytic cracking oil gas.Inferior feedstock oil conversion ratio can be increased substantially and reduce dry gas and coke yield by carrying out processing inferior feedstock oil using the method for the present invention on present system, to realize the clean and efficient utilization of inferior feedstock oil.

Description

A kind of processing method and system of inferior feedstock oil
Technical field
The present invention relates to a kind of processing method of inferior feedstock oil and systems.
Background technique
It is inferior former as petroleum resources shortage and the demand to high-quality gasoline, diesel oil and low-carbon alkene increasingly increase Expect that the oily such as processing technology of liquefied coal coil, tar sand oil and poor quality, heavy crude oil product is increasingly taken seriously.Inferior raw material Oil, liquefied coal coil, tar sand oil etc., similar natural oil, but contain more unsaturated hydrocarbons, and nitrogenous, sulphur than natural oil With the non-hydrocarbons organic compound such as oxygen, not only influence its secondary processing and utilization, and have an effect on product gasoline, the color of diesel oil and Stability, sulphur, nitrogen content are high.Inferior feedstock oil is other than producing chemicals on a small quantity at present, it is most of without secondary operation and It is sold directly as light-weight fuel oil, it is therefore necessary to the more technologies for efficiently utilizing inferior feedstock oil of exploitation.
Since the heteroatomic compounds content such as nitrogen, sulphur, oxygen is higher in inferior feedstock oil, especially nitrogen content generally exists 1%~3%, the lighting of inferior feedstock oil cannot be carried out directly as catalytically cracked material, and it is special to be primarily due to nitride Be basic nitrogen compound during catalytic cracking reaction can and acidity of catalyst central role and reduce catalyst activity and selection Property, show in product distribution it is that coking yield increases, slurry oil increases, yield of light oil decline.ARCO company points out, most of to urge Change cracking unit and is resistant to 2000 μ g/g total nitrogens and 1000 μ g/g alkali nitrogen.By using peracid center density, rare earth containing zeolite it is anti- Nitrogen Cracking catalyst such as RHZ-200, LC-7, CCC-1, RHZ-300, or use acid additive as the agent for capturing of nitrogen, catalysis Cracking unit can only also process 3000 μ g/g charging below of nitrogen content.In addition, inferior feedstock oil colloid and olefin(e) centent are higher. In catalytic cracking process, the colloid of one third can generate coke, and alkene is more active, and the two is readily adsorbed on catalyst Cover activated centre.Although colloid gasification needs higher temperature, the more higher easier generation coke of reaction temperature.
In summary factor, inferior feedstock oil generally require first hydrotreating modification, to remove the impurity such as oxygen, nitrogen, sulphur, so In refinery, oil refining processing technology routinely is processed into various oil products afterwards.United States Patent (USP) US 4342641 discloses a kind of inferior former Expect oily processing method, full fraction inferior feedstock oil is first subjected to hydrotreating, the obtained fraction less than 249 DEG C is directly as spray Gas fuel, the obtained fraction greater than 249 DEG C is hydrocracked again, to produce jet fuel；Wherein hydrotreating is in two steps It carries out, first carries out prerefining with the low catalyst of Ni-Mo content, then further refined with the high catalyst of Ni-Mo content. This method hydrogenation process is more, and hydrogen consumption is high, and operating cost is high, and construction investment is high.Chinese patent CN 1067089A, CN 102453546A and CN 102465036A disclose a kind of inferior feedstock oil hydrogenation fractionating, adds hydrogen heavy oil catalytic pyrolysis again Processing method, as described in Chinese patent CN 1067089A, inferior feedstock oil first passes through hydrotreating and obtains hydrogenated oil, adds Hydrogen, which generates oil and is separated into, adds hydrogen heavy oil and light-end products, and hydrogen heavy oil is added to obtain dry gas, liquefied gas, gasoline, bavin after catalytic cracking Oil and catalytic heavy, diesel oil and heavy-cycle oil can return to hydrotreating step；The only poor quality of Chinese patent CN 102465036A Feedstock oil adds hydrogen heavy oil to carry out catalytic cracking reactions using two riser reactors, and CN 102453546A is resulting plus hydrogen It generates oil and enters cat-cracker together with optional vacuum gas oil (VGO).In short, inferior feedstock oil carries out hydrofinishing, purification Inferior feedstock oil can be converted to lightweight production by processing method of the obtained heavy oil as the raw material of existing catalytic cracking technology Product.
Inferior feedstock oil hydrotreating has easy to operate, purpose product yield height, good product quality and three-waste free discharge The advantages that, it is 21 century environmental-friendly processing technology.But non-hydrocarbon compound impurity is in hydrotreating in inferior feedstock oil Harmful substance is the object to be removed or be converted, but itself is useful industrial chemicals, therefore is considered as extraction and benefit With；In addition, influencing service life and the efficiency of hydrogenation catalyst if inferior feedstock oil oxygen content is higher.Hydrogen addition technology is at present only There is Australian SPP company to reach the commerical test stage, super-low sulfur light-weight fuel oil is produced by hydrofinishing.
Non- hydrotreating mainly uses acid-alkali refining, and such as patent Chinese patent CN 101967389A, acid-alkali refining is not only A large amount of reluctant acid sludges can be generated, pollute environment, and oil yield is low；It is used although some researchers explore in recent years Single solvent or multi-solvent extracting and refining method, such as patent Chinese patent CN CN1746265A, but there are still solvent consumptions larger, energy Consume the problems such as high.With the raising of environmental protection requirement, the discharge standard of light-weight fuel oil combustion tail gas is constantly mentioned both at home and abroad Height, it is lower to the limitation of the sulphur of automobile-used light-weight fuel oil, nitrogen and arene content, so being extremely difficult to want using non-hydroprocessing process It asks.
Therefore, in order to efficiently utilize inferior feedstock oil resource, meet the demand of growing light-weight fuel oil, it is necessary to Develop it is a kind of by inferior feedstock oil Efficient Conversion be a large amount of lightweights and clean light-weight fuel oil method.
Summary of the invention
The object of the present invention is to provide a kind of processing method of inferior feedstock oil and systems, use this method on this system Inferior feedstock oil conversion ratio can be increased substantially and reduce dry gas and coke yield by carrying out processing inferior feedstock oil, to realize The clean and efficient utilization of inferior feedstock oil.
To achieve the goals above, the present invention provides a kind of processing method of inferior feedstock oil, this method comprises: a, will contain The fluidized bed that hydrogen is sent into fluidized bed riser reactor with inferior feedstock oil faces in hydrogen adsorption zone urges with the first catalytic cracking Agent contacts and carries out facing hydrogen adsorption reaction, obtains facing hydrogen adsorbed product；B, gained in step a is faced into hydrogen adsorbed product and is sent into institute It states and is contacted in the riser cracking area of fluidized bed riser reactor with the second catalytic cracking catalyst and carry out Catalytic Cracking Unit of Measure It answers, obtains catalytic cracking oil gas.
Preferably, this method further include: gained cycle oil pneumatic transmission in step b is entered into fractionating device and is carried out at fractionation Reason, obtain include rich gas catalytic cracking production；Gained rich gas is sent directly into absorption stabilizing apparatus without rich gas compressor Carry out Vapor recovery unit processing.
Preferably, this method further include: in stepb, Conventional catalytic cracking feedstock oil is faced into hydrogen adsorbed product with described The catalytic cracking reaction is carried out together；Wherein, the Conventional catalytic cracking feedstock oil is selected from wax oil, reduced crude and decompression At least one of wax oil.
Preferably, the hydrogen-containing gas includes hydrogen and/or dry gas, and the inferior feedstock oil is selected from shale oil, coal liquid At least one of carburetion, tar sand oil, wax tailings, residual oil, hydrogenated residue and deasphalted oil.
Preferably, the composition of first catalytic cracking catalyst and the second catalytic cracking catalyst is identical, includes 1- The clay of the zeolite of 50 weight %, the inorganic oxide of 5-99 weight % and 0-70 weight %.
Preferably, the zeolite includes mesopore zeolite and/or large pore zeolite, the mesopore zeolite be selected from ZSM-5 zeolite, In ZSM-11 zeolite, ZSM-12 zeolite, ZSM-23 zeolite, ZSM-35 zeolite, ZSM-38 zeolite, ZSM-48 zeolite and ZRP zeolite At least one, the large pore zeolite be selected from rare earth Y type zeolite, rare earth hydrogen Y zeolite, Y-type high-Si zeolite and ultrastable At least one of；The inorganic oxide is silica and/or aluminium oxide；The clay be selected from silica, kaolin, In halloysite, montmorillonite, diatomite, galapectite, saponite, rectorite, sepiolite, attapulgite, hydrotalcite and bentonite At least one.
Preferably, first catalytic cracking catalyst be supplement fresh catalyst Cracking catalyst, cooling regeneration urge At least one in the catalytic cracking catalyst to be generated of fluidized cracking catalysts, the semi regeneration catalytic cracking catalyst of cooling and cooling Kind, second catalytic cracking catalyst is regeneration catalyzing Cracking catalyst；The temperature of first catalytic cracking catalyst is 200-500 DEG C, the temperature of the second catalytic cracking catalyst is 580-680 DEG C.
Preferably, it is 200-450 DEG C that the condition for facing hydrogen adsorption reaction, which includes: temperature, and pressure is 0.5-5.0 megapascal, Adsorption time is 1-90 seconds, and agent oil weight ratio is (0.5-5): 1, hydrogen to oil volume ratio 100-1000；The catalytic cracking reaction Condition include: temperature be 460-540 DEG C, pressure be 0.5-5.0 megapascal, the oil gas residence time be -15 seconds 0.5 second, agent oil weight Amount is than being (5-30): 1.
Preferably, this method further include: cooling medium is sent into the fluidized bed faces and carry out temperature control in hydrogen adsorption zone；It is described Cooling medium is selected from least one of cold hydrogen, water, gasoline, diesel oil, recycle oil and fused salt.
The present invention also provides a kind of systems of processing of inferior feedstock oil, wherein the system of processing includes being provided with fluidized bed Section and the fluidized bed riser reactor for promoting pipeline section, are formed with fluidized bed in the fluid bed section and face hydrogen adsorption zone, described to mention Riser cracking area is formed in riser section；The fluidized bed face hydrogen adsorption zone connect with riser cracking area and fluid connect Logical, the fluid bed section is provided with hydrogen-containing gas entrance, inferior raw material oil-in and the first catalytic cracking catalyst entrance, described It promotes pipeline section and is provided with the second catalytic cracking catalyst entrance, the outlet of catalytic cracking oil gas and catalytic cracking catalyst outlet, if Set or be not provided with Conventional catalytic cracking raw material oil-in.
Preferably, the system of processing further includes fractionating device and absorption stabilizing apparatus, and the oil gas of the fractionating device enters Mouth and the catalytic cracking oil gas communication, the richness of the rich gas outlet and the absorption stabilizing apparatus of the fractionating device Gas entrance is in fluid communication.
Preferably, the system of processing further includes regenerator, the regenerator be provided with regenerator catalyst outlet and again Raw device catalyst inlet, the regenerator catalyst outlet are split with the first catalytic cracking catalyst entrance and the second catalysis Change catalyst inlet connection, the regenerator catalyst entrance and the catalytic cracking catalyst outlet.
Preferably, the regenerator catalyst outlet is connected by heat collector and the first catalytic cracking catalyst entrance It is logical.
Preferably, the promotion pipeline section is upstriker riser reactor, and the fluid bed section, which is located at, to be promoted under pipeline section Side, and the first catalytic cracking catalyst entrance is located at the lower part of the fluid bed section, second catalytic cracking catalyst Entrance is located at the lower part for promoting pipeline section, and the catalytic cracking catalyst outlet is located at the top for promoting pipeline section；Alternatively, The promotion pipeline section is downstriker riser reactor, and the fluid bed section is located at the top for promoting pipeline section, and described first urges Fluidized cracking catalysts entrance is located at the top of the fluid bed section, and the second catalytic cracking catalyst entrance is located at the promotion The top of pipeline section, the catalytic cracking catalyst outlet are located at the lower part for promoting pipeline section.
Preferably, the fluidized bed faces 0.5-5 times of the diameter that the diameter of hydrogen adsorption zone is riser cracking area, the stream Change bed and faces the length of hydrogen adsorption zone for the 1-30% of the length in riser cracking area.
Preferably, the fluid bed section is provided with cooling medium entrance, and the cooling medium entrance faces with the fluidized bed Hydrogen adsorption zone in direct fluid communication is in fluid communication with the heat collector that the fluidized bed faces in hydrogen adsorption zone is arranged in.
The present invention has following technical effect compared with prior art:
(1) inferior feedstock oil can be processed without refinement treatment and directly, the processing flow of inferior feedstock oil Short, hydrogen consumption is low, and can realize long period continuous production；
(2) present invention carries out processing inferior feedstock oil using " device two anti-", i.e., be packed into a reactor it is identical or Different the first catalytic cracking catalysts and the second catalytic cracking catalyst, both catalyst cooperate in same reaction atmosphere Complete the impurity such as inferior feedstock oil absorption sulfide, basic nitrogen compound, heavy metal and colloid and inferior feedstock oil catalytic cracking Function, then can in same regeneration atmosphere simultaneously activity recovery；
(3) inferior feedstock oil elder generation adsorbing and removing sulfide, basic nitrogen compound, heavy metal and colloid isopolarity substance are catalyzed again Cracking, inferior feedstock oil high conversion rate, dry gas is low with coke yield, reduces device green coke, liquid product (liquefied gas+gasoline+ Diesel oil) yield height；
(4) inferior feedstock oil is adsorbed in the case where facing hydrogen atmosphere, is more advantageous to the first catalytic cracking catalyst to inferior former Sulfur-bearing, nitrogenous and oxygenatedchemicals adsorbing and removing in material oil, the first catalytic cracking catalyst and inferior feedstock oil weight ratio drop Low, adsorption time is short, and liquid product sulphur, nitrogen content are low and quality is good；
(5) system of processing is facing hydrogen band pressing operation, has correspondinglyd increase the pressure into the rich gas of absorption stabilizing apparatus, has saved But the rich gas compressor of conventional FCC process, plant energy consumption reduce；
(6) fluidized bed riser reactor is more suitable for the fast feature of catalytic cracking reaction, compared with fixed bed and moving bed, Reactor volume utilization rate is high, is more suitable for the continuous operation of large-scale production, and can use existing riser reactor dress It sets and is transformed.
Other features and advantages of the present invention will the following detailed description will be given in the detailed implementation section.
Detailed description of the invention
The drawings are intended to provide a further understanding of the invention, and constitutes part of specification, with following tool Body embodiment is used to explain the present invention together, but is not construed as limiting the invention.In the accompanying drawings:
Fig. 1 be include processing method of the present invention the first specific embodiment flow diagram, and including this hair The structural schematic diagram of the first specific embodiment of bright system of processing；
Fig. 2 be include processing method of the present invention second of specific embodiment flow diagram, and including this hair The structural schematic diagram of second of specific embodiment of bright system of processing；
Fig. 3 be include processing method of the present invention the third specific embodiment flow diagram, and including this hair The structural schematic diagram of the third specific embodiment of bright system of processing.
Description of symbols
I fluidized bed faces the hydrogeneous pre-lift medium in hydrogen adsorption zone II riser cracking area 1
2 fluidized bed riser reactor, 3 inferior feedstock oil, 4 hydrogen-containing gas
5 stripped vapor, 6 settler, 7 pipeline
8 fractionating device, 9 pipeline, 10 absorption stabilizing apparatus
11 dry gas, 12 pipeline, 13 regenerator
14 regeneration gas, 15 flue gas, 16 pipeline
The outlet of 17 heat collector, 18 cooling medium entrance, 19 cooling medium
20 pipeline, 21 pipeline 22 promotes medium
23 Conventional catalytic cracking feedstock oils
24 Conventional catalytic cracking 25 liquefied gas of feedstock oil atomizing medium
26 gasoline, 27 diesel oil, 28 slurry oil
Specific embodiment
Below in conjunction with attached drawing, detailed description of the preferred embodiments.It should be understood that this place is retouched The specific embodiment stated is merely to illustrate and explain the present invention, and is not intended to restrict the invention.
The present invention provides a kind of processing method of inferior feedstock oil, this method comprises: a, by hydrogen-containing gas and inferior raw material The fluidized bed that oil is sent into fluidized bed riser reactor, which faces in hydrogen adsorption zone I, to be contacted and is faced with the first catalytic cracking catalyst Hydrogen adsorption reaction obtains facing hydrogen adsorbed product；B, gained in step a is faced into hydrogen adsorbed product to be sent into the fluidized bed riser anti- It answers and contacts and carry out catalytic cracking reaction in the riser cracking area II of device with the second catalytic cracking catalyst, obtain catalytic cracking Oil gas.
The present inventor passes through years of researches it was unexpectedly observed that nitrogenous compound, sulfur-bearing in inferior feedstock oil Compound and oxygenatedchemicals etc. can be by adsorbing and removings, and catalytic cracking catalyst itself can also be used as adsorbent；It is special It is not in the case where facing hydrogen atmosphere, adsorption time is short, is more advantageous to the first catalytic cracking catalyst to sulfur-bearing chemical combination in inferior feedstock oil Object, nitrogenous compound, oxygenatedchemicals and metal adsorbing and removing, make the high conversion rate of inferior feedstock oil, liquid product sulphur, nitrogen Content is low, and quality is good.
According to the present invention, this method can also include: by step b gained cycle oil pneumatic transmission enter fractionating device 8 into Row fractionation processing, obtain include rich gas catalytic cracking production；Gained rich gas is sent directly into absorption without rich gas compressor Stabilising arrangement 10 carries out Vapor recovery unit processing.Existing Conventional catalytic cracking device reaction and fractionating system are pressed in 0.1-0.25MPa It is operated under power, and absorption stabilizing apparatus need to be operated under the pressure of 1.1MPa or more, therefore Conventional catalytic cracking dress Setting must be provided with rich gas compressor and carries out compression pressure-raising to the rich gas from fractionating device, and reaction system of the present invention is to face hydrogen with pressure It is operated under (0.5-5.0MPa), has correspondinglyd increase the pressure that rich gas enters absorption stabilizing apparatus, can save in conventional FCC process Rich gas compressor, to reduce plant energy consumption and cost input.Fractionating device obtains rich gas, diesel oil and slurry oil, and fractionating device (divides Evaporate tower) at the top of rich gas can without rich gas compressor compress be directly entered absorption stabilizing apparatus further progress product separation, Obtain dry gas, liquefied gas and gasoline etc..The boiling ranges such as gasoline or diesel oil can be adjusted according to actual needs, be not limited only to full range Gasoline or diesel oil.
According to the present invention, in order to increase the treating capacity of processing method, this method can also include: in stepb, will be conventional Catalytically cracked stock with it is described face the catalytic cracking reaction is carried out together with hydrogen adsorbed product；Wherein, the Conventional catalytic is split Changing feedstock oil can be for selected from least one of wax oil, reduced crude and decompressed wax oil.The inferior feedstock oil is in the stream Change bed and face the charging of hydrogen adsorption zone, Conventional catalytic cracking feedstock oil is fed in the riser cracking area；Face hydrogen and is adsorbed and removed impurity Inferior feedstock oil and the first catalytic cracking catalyst of part afterwards enters the riser cracking area, with entrance riser cracking area Conventional catalytic cracking feedstock oil contact second catalytic cracking catalyst together, carry out the catalytic cracking reaction.
According to the present invention, hydrogen-containing gas is well-known to those skilled in the art, both can be used as hydrogen source use, can also be with It is used as inferior feedstock oil conveying gas, forms the present invention and be not particularly limited, for example, the hydrogen-containing gas may include Hydrogen and/or dry gas also may include that nitrogen and vapor etc. are non-containing hydrogen medium, non-not contain containing hydrogen medium or containing micro Oxygen, volume fraction of the oxygen in hydrogen-containing gas are not more than 1%；Inferior feedstock oil is known to those skilled in the art, can Think selected from least one of shale oil, liquefied coal coil, tar sand oil, wax tailings, residual oil, hydrogenated residue and deasphalted oil, Relative density can be 0.8-1.1, can be rich in alkane, aromatic hydrocarbons and some olefin, and carbon hydrogen element weight ratio can be 7-9, and And the non-hydrocarbons organic compound content such as nitrogen, sulphur and oxygen is higher, nitrogen content can be 0.5%-5%, and sulfur content can be 0.5%-10%, oxygen content can be 0.5%-20%.
In the present invention, the inferior feedstock oil can first pass through preheating after be sent into reactor in reacted, the preheating Temperature can be 150-400 DEG C, preferably 200-350 DEG C.
According to the present invention, catalytic cracking catalyst is well-known to those skilled in the art, and first catalytic cracking is urged Agent and second catalytic cracking catalyst can be it is same or different, the activity of catalytic cracking catalyst can be 40- 70, preferably 45-60.The composition of catalytic cracking catalyst may include: zeolite, inorganic oxide and optional clay；First The concrete composition and usage amount of catalytic cracking catalyst and second catalytic cracking catalyst both depend on inferior feedstock oil nitrogen Content and denitrogenation requirement, and are determined by catalytic cracking reaction condition, it is preferable that first catalytic cracking catalyst with it is described Second catalytic cracking catalyst composition is identical, may each comprise the zeolite of 1-50 weight %, the inorganic oxide of 5-99 weight % With the clay of 0-70 weight %.Wherein, zeolite can be mesopore zeolite and/or optional large pore zeolite, and mesopore zeolite can account for The 80-100 weight % of zeolite total weight preferably accounts for 90 weight %-100 weight %；Large pore zeolite can account for the 0-20 of zeolite total weight Weight % preferably accounts for 0 weight %-10 weight %.The mesopore zeolite can be ZSM series zeolite and/or ZRP zeolite, preferably be selected from ZSM-5 Zeolite, ZSM-11 zeolite, ZSM-12 zeolite, ZSM-23 zeolite, ZSM-35 zeolite, ZSM-38 zeolite, ZSM-48 zeolite and ZRP boiling At least one of stone also may include the zeolite of other similar structures.More description can be joined related ZSM-5 zeolite in detail See United States Patent (USP) US3,702,886, more description may refer to United States Patent (USP) US5 to related ZRP zeolite in detail, and 232,675.Institute Stating large pore zeolite can be Y-series zeolite, may include rare earth Y type zeolite (REY), rare earth hydrogen Y zeolite (REHY), superstable gamma-type At least one of zeolite (can be obtained by distinct methods) and Y-type high-Si zeolite.The inorganic oxide is generally as bonding Agent can be silica (SiO2) and/or aluminium oxide (Al2O3), with dry basis, silica can be accounted in inorganic oxide The heavy % of 50 weight -90, aluminium oxide can account for the heavy % of 10 weight -50.The clay, can be for selected from titanium dioxide as matrix (i.e. carrier) Silicon, kaolin, halloysite, montmorillonite, diatomite, galapectite, saponite, rectorite, sepiolite, attapulgite, hydrotalcite At least one of with bentonite.Under preferable case, can using the transition metal elements component such as iron, cobalt, nickel to above-mentioned macropore, Mesopore zeolite, inorganic oxide and clay etc. are modified.First catalytic cracking catalyst and the second catalytic cracking catalyst with Based on microspheroidal, diameter can be respectively greater than 0 to 200 micron, further preferably 40-150 microns, catalyst apparent density 0.4-1.9g/cm can be respectively3, further preferably 0.8-1.5g/cm3。
According to the present invention, the first catalytic cracking catalyst and the second catalytic cracking catalyst can be different for granular size Catalyst and/or the different catalyst of apparent bulk density.The different catalyst of granular size and/or apparent bulk density are different The active component of catalyst can also select different type zeolite or metal, nonmetallic modifying zeolite respectively, it is of different sizes The different catalyst of the catalyst and/or apparent bulk density of particle can respectively enter different riser cracking areas, for example, Short grained catalyst containing high silica alumina ratio extremely steady y-type zeolite of rare earth can enter fluidized bed and face hydrogen adsorption zone I (as first Catalytic cracking catalyst), the adsorbing and removing for increasing basic nitrogen compound, heavy metal and/or colloid, asphalitine isopolarity substance is anti- It answers.The catalyst of bulky grain containing ultrastable can enter riser cracking area II and (be catalyzed as the second catalytic cracking Agent), increase catalytic cracking reaction, the different catalyst of granular size is in same stripper stripping and the regeneration of same regenerator, so After isolate bulky grain and catalyst particle, catalyst particle faces hydrogen adsorption zone I through the cooling fluidized bed that enters.Granular size Different catalyst can demarcate between 30-40 microns, and the different catalyst of apparent bulk density can be in 0.6-0.7g/ cm3Between demarcate.
According to the present invention, in order to control the temperature for facing hydrogen adsorption reaction and catalytic cracking reaction, first catalytic cracking Catalyst can urge for the semi regeneration of the fresh catalyst Cracking catalyst of supplement, the regeneration catalyzing Cracking catalyst of cooling, cooling At least one of fluidized cracking catalysts and cooling catalytic cracking catalyst to be generated, second catalytic cracking catalyst can be with For regeneration catalyzing Cracking catalyst；The temperature of first catalytic cracking catalyst can be 200-500 DEG C, more preferably 230- 480 DEG C, the temperature of the second catalytic cracking catalyst can be 580-680 DEG C.Under preferable case, the first catalytic cracking catalysis Agent can be the intermixture after regeneration catalyzing Cracking catalyst and the heat exchange of fresh catalyst Cracking catalyst, using fresh after heat exchange Catalytic cracking catalyst is good to nitrogen especially basic nitrogen adsorption effect, and denitrification percent is high；And the fresh catalyst after adsorbing denitrogenation Cracking catalyst, activity reduce, and green coke is low in catalytic cracking process.
According to the present invention, face hydrogen adsorption reaction and catalytic cracking reaction is well-known to those skilled in the art, for example, institute State face hydrogen adsorption reaction condition may include: temperature be 200-450 DEG C, preferably 250-400 DEG C, pressure be 0.5-5.0 million Pa, preferably 1.0-4.0 megapascal, adsorption time are 1-90 seconds, and preferably 2-60 seconds, agent oil weight ratio was (0.5-5.0): 1, it is excellent It is selected as (1-4): 1, hydrogen to oil volume ratio 100-1000, preferably 300-800；The condition of the catalytic cracking reaction can wrap Include: temperature is 460-540 DEG C, and preferably 480-530 DEG C, pressure is 0.5-5.0 megapascal, and preferably 1.0-4.0 megapascal, oil gas stops Staying the time is 0.5-15 seconds, and preferably 1.0-10 seconds, agent oil weight ratio was (5-30): 1, preferably (6-30): 1.The fluidisation The linear speed that is apparently averaged that bed faces oil gas in hydrogen adsorption zone I can be 0.5-8.0 meter per second, oil gas in the riser cracking area II Apparently averagely linear speed can be 10-60 meter per second；Under preferable case, the fluidized bed, which faces the apparent of oil gas in hydrogen adsorption zone I, is put down The low 8-52 meter per second of linear speed that is apparently averaged of oil gas, first catalytic cracking are urged in riser cracking area II described in equal differential surface speed Agent is in fluidized state, is preferably in turbulent fluidization regimes.
According to the present invention, the division that fluidized bed faces hydrogen adsorption zone and riser cracking area can be the difference of reactor, Cooling medium can be injected in reactor bottom or top, by introducing cooling medium, hydrogen absorption and catalytic cracking process will be faced It organically combines, to realize inferior feedstock oil catalytic hydroprocessing cracking, and improves inferior feedstock oil conversion capability.Therefore this method It can also include: cooling medium is sent into the fluidized bed to face in hydrogen adsorption zone I to carry out temperature control；The cooling medium can be choosing At least one of self cooling hydrogen, water, gasoline, diesel oil, recycle oil and fused salt；Cooling medium can be directly injected into reactor, or pass through Arrange that heat production coil pipe etc. makes catalyst and cooling medium exchange heat in reactor, so that controlling fluidized bed faces hydrogen adsorption zone temperature Degree.
The present invention also provides a kind of systems of processing of inferior feedstock oil, wherein the system of processing includes being provided with fluidized bed Section and the fluidized bed riser reactor for promoting pipeline section, are formed with fluidized bed in the fluid bed section and face hydrogen adsorption zone I, described to mention Riser cracking area II is formed in riser section；The fluidized bed faces hydrogen adsorption zone I and connects and flow with riser cracking area II Body connection, the fluid bed section are provided with hydrogen-containing gas entrance, inferior raw material oil-in and the first catalytic cracking catalyst entrance, The promotion pipeline section is provided with the second catalytic cracking catalyst entrance, the outlet of catalytic cracking oil gas and catalytic cracking catalyst and goes out Mouthful, it is arranged or is not provided with Conventional catalytic cracking raw material oil-in.Wherein, the catalytic cracking oil gas outlet and catalytic cracking are urged Agent outlet may be the same or different.
A kind of specific embodiment according to the present invention, the system of processing can also include fractionating device 8 and absorb steady Determine device 10, the oil gas entrance of the fractionating device 8 can be with the catalytic cracking oil gas communication, the fractionation dress Setting 8 rich gas outlet can be in fluid communication with the rich gas entrance of the absorption stabilizing apparatus 10.Existing Conventional catalytic cracking device Reaction and fractionating device are generally operated under 0.1-0.25MPa pressure, and absorption stabilizing apparatus need to be 1.1MPa's or more It is carried out under pressure, therefore Conventional catalytic cracking device must be provided with rich gas compressor and compress to the rich gas from fractionating device Pressure-raising, system of processing of the present invention are operated in the case where facing hydrogen (0.5-5.0MPa) with pressure, have been correspondinglyd increase rich gas and have been entered Vapor recovery unit dress The pressure set can save rich gas compressor in conventional FCC process, to reduce plant energy consumption.
According to the present invention, in order to facilitate the regeneration of catalyst, the system of processing can also include regenerator 13, it is described again Regenerator catalyst outlet and regenerator catalyst entrance has can be set in raw device 13, and the regenerator catalyst outlet (should go out Mouth can be one, or two or more) can be with the first catalytic cracking catalyst entrance and second The connection of catalytic cracking catalyst entrance, the regenerator catalyst entrance can be with the catalytic cracking catalyst outlet. The regenerated temperature of regenerator is generally 550~700 DEG C, preferably 600-650 DEG C, and the regeneration catalyzing Cracking catalyst after regeneration is followed Ring uses, and in regenerative process, regeneration gas can be for selected from least one of air, oxygen and oxygen-containing gas.After regeneration The heat exchange of catalyst can be carried out using method well known to those of ordinary skill in the art, to control coke production quantity and oil Agent Contact Temperature.
Specific embodiment according to the present invention, the promotion pipeline section can be upstriker riser reactor, the stream The lower section for promoting pipeline section can be located at by changing bed section, and the first catalytic cracking catalyst entrance can be located at the fluid bed section Lower part, the second catalytic cracking catalyst entrance can be located at the lower part for promoting pipeline section, catalytic cracking catalysis Agent outlet can be located at the top for promoting pipeline section；Alternatively, the promotion pipeline section can be downstriker riser reactor, institute The top for promoting pipeline section can be located at by stating fluid bed section, and the first catalytic cracking catalyst entrance can be located at the fluidisation The top of bed section, the second catalytic cracking catalyst entrance can be located at the top for promoting pipeline section, the catalytic cracking Catalyst outlet can be located at the lower part for promoting pipeline section.
In the present invention, the fluidized bed that inferior feedstock oil enters reactor faces hydrogen adsorption zone, faces hydrogen adsorption zone according to fluidized bed Setting, inferior feedstock oil can using it is lower charging and also use upper feeding；If using lower charging, inferior feedstock oil is from upper Line fluidized bed riser reactor bottom enters fluidized bed and faces hydrogen adsorption zone, as hydrogen-containing gas flows from bottom to top；If Inferior feedstock oil uses upper feeding, and inferior feedstock oil enters fluidized bed at the top of downstriker fluidized bed riser reactor and faces hydrogen suction Attached area, inferior feedstock oil flow from top to bottom with hydrogen-containing gas；Inferior feedstock oil enters fluidized bed and faces hydrogen adsorption zone, is facing hydrogen Under atmosphere, first wherein basic nitrogen compound etc. is miscellaneous for adsorbing and removing on the first catalytic cracking catalyst with nitride adsorption function Matter.
According to the present invention, fluid bed section and promotion pipeline section are well-known to those skilled in the art, and fluidized bed faces hydrogen absorption Area, reaction temperature is lower, maintains certain catalyst inventory, apparently averagely linear speed is generally 0.5-8.0 meter per second, riser to oil gas The oil gas apparent linear velocity of the zone of cracking is generally 10-60 meter per second.The diameter that the fluidized bed faces hydrogen adsorption zone I can be riser 0.5-5 times of the diameter of zone of cracking II, preferably 1-4 times, more preferably 1.0-2.0 times, the fluidized bed face hydrogen adsorption zone I's Length can be the 1-30%, preferably 10-25%, more preferably 10-20% of the length of riser cracking area II.The fluidisation Bed faces hydrogen adsorption zone and riser cracking area refers to the sky for being able to carry out in reactor and facing hydrogen adsorption reaction and catalytic cracking reaction Between, it does not include reactor itself.If the reactor is expanding in riser cracking area end, inferior feedstock oil can be strengthened The conversion of crackate sulfide in petrol and alkene.Catalytic cracking reaction terminates, and can mentioned according to the needs for terminating reaction As terminator, cooling medium can be water, gasoline or diesel oil etc. for riser tube upper portion or exit injection cooling medium.
According to the present invention, different with the temperature of catalytic cracking reaction due to facing hydrogen adsorption reaction, the regenerator is urged Agent outlet can be connected to by heat collector 17 with the first catalytic cracking catalyst entrance, and the catalyst after making regeneration passes through The fluidized bed is entered back into after cooling to face in hydrogen adsorption zone.
A kind of specific embodiment, as shown in Figure 1-3, the fluid bed section is provided with cooling medium entrance, the cooling Medium inlet and the fluidized bed face hydrogen adsorption zone I in direct fluid communication or face in hydrogen adsorption zone I with being arranged in the fluidized bed Heat collector 17 be in fluid communication.
The present invention will be further illustrated by specific embodiment below, but the present invention is not therefore and by any Limitation.
As shown in FIG. 1, FIG. 1 is the process flow diagrams of the first specific embodiment of the invention, in the specific implementation In mode, using the compound reactor being made of fluid bed section and promotion pipeline section, the promotion pipeline section is that upstriker riser is anti- Device is answered, expanding fluidized bed faces hydrogen adsorption zone I in riser pars infrasegmentalis, and inferior feedstock oil is adopted in fluidized bed riser reactor Enter fluidized bed with lower charging and face hydrogen adsorption zone I, after adsorbing denitrogenation, is above advanced into riser cracking area II and carries out Catalytic Cracking Unit of Measure It answers.Its process flow is as follows:
Inferior feedstock oil uses the fluidized bed riser reactor being made of fluid bed section and promotion pipeline section first to adsorb denitrogenation Catalytic cracking again, reactor lower part is expanding to face hydrogen adsorption zone I for fluidized bed, is introduced by pipeline 20 after regeneration through external warmer 17 first catalytic cracking catalysts after cooling；Inferior feedstock oil 3 enters fluidized bed from the expanding bottom of reactor 2 and faces hydrogen absorption Area I carries out reaction suction with hydrogeneous pre-lift medium 1 and hydrogen-containing gas 4 together uplink on the first catalytic cracking catalyst It is attached to remove the wherein impurity such as basic nitrogen compound, sulfide, colloid and/or heavy metal；Face hydrogen adsorbed product therewith on be advanced into it is anti- The riser cracking area II for answering device 2, the second catalytic cracking catalyst with the high temperature high activity through pipeline 21 from regenerator 13 It carries out contact and catalytic cracking reaction occurs；Oil gas and catalyst (the first catalytic cracking catalyst of part and the second catalysis of generation Cracking catalyst) enter the progress sedimentation separation of settler 6, the oil gas after separation enters fractionating device 8 and obtains diesel oil 27, slurry oil 28, fractionating device tower top rich gas is directly entered 10 further progress product of absorption stabilizing apparatus point without rich gas compressor compression From obtaining the products such as dry gas 11, liquefied gas 25 and gasoline 26, the selected section as needed of dry gas 11 is recycled back to fluidized bed and faces hydrogen suction As hydrogen-containing gas or pre-lift medium, slurry oil 28 selects freshening or not freshening as needed in attached area；Catalyst after separation After stripped vapor 5 strips the oil gas of removing absorption, it is sent into regenerator 13 and is regenerated in regeneration gas (air) 14, regenerated 600-680 DEG C of temperature, the regenerant recycle after regeneration uses.
As shown in Fig. 2, Fig. 2 is the process flow diagram of second of specific embodiment of the invention, in the specific implementation In mode, Conventional catalytic cracking feedstock oil mixes refining inferior feedstock oil, the process flow of process flow and specific embodiment one Schematic diagram is essentially identical, only the specific embodiment increase newly one conventional raw material oil and its atomizing medium respectively through pipeline 23, 24 injecting lift pipe zone of cracking II, specific location are the regeneration that the second catalytic cracking catalyst enters fluidized bed riser reactor Refining is mixed in the top of pipeline 21 together with inferior feedstock oil.In this specific embodiment, the fluidized bed faces in hydrogen adsorption zone I The low 8-25 meter per second of linear speed that is apparently averaged of oil gas, maintains stream in riser cracking area II described in the apparent averagely differential surface speed of oil gas Changing bed to face hydrogen adsorption zone is turbulent fluidization regimes.
As shown in figure 3, Fig. 3 is the process flow diagram of the third embodiment of the invention, in the specific embodiment In, the reactor is downstriker fluidized bed riser reactor, and expanding fluidized bed faces hydrogen adsorption zone I and inhales in the riser The top of attached area II, inferior feedstock oil enter fluidized bed using upper feeding in the reactor and face hydrogen adsorption zone I, are facing hydrogen atmosphere Enclose catalytic cracking again after lower absorption denitrogenation, under be advanced into riser cracking area II and carry out catalytic cracking reaction.In addition, being different from the A kind of heat collector of embodiment being arranged in outside reactor, heat collector is arranged in fluid bed section in this embodiment In.Its process flow is as follows:
Inferior feedstock oil first adsorbs denitrogenation catalytic cracking again using the downstriker fluidized bed riser reactor 2, described 2 top of reactor is expanding to face hydrogen adsorption zone I for fluidized bed；Inferior feedstock oil 3 and hydrogen-containing gas 4 use upper feeding, inferior raw material Oil 3 enters fluidized bed from the expanding top of reactor 2 and faces hydrogen adsorption zone I, as hydrogen-containing gas flows downward, is coming from pipeline 20 The first catalytic cracking catalyst on carry out reaction adsorbing and removing wherein basic nitrogen compound, sulfide, colloid and/or heavy metal etc. Impurity, and carry out taking thermal control temperature using heat collector 17；Face the promotion that hydrogen adsorbed product is advanced into down the reactor 2 therewith The pipe zone of cracking II carries out contact with the second catalytic cracking catalyst of the high temperature high activity of the pipeline 21 from regenerator 13 Catalytic cracking reaction；The oil gas and catalyst of generation enter settler 6 and carry out sedimentation separation, and the oil gas after separation enters fractionation dress It sets 8 and obtains diesel oil 27, slurry oil 28, fractionation tower top rich gas is directly entered absorption stabilizing apparatus 10 into one without rich gas compressor compression Step carries out product separation, obtains the products such as dry gas 11, liquefied gas 25 and gasoline 26, the selected section as needed of dry gas 11 is recycled back to Fluidized bed faces hydrogen adsorption zone I as hydrogen-containing gas or pre-lift medium, and slurry oil 28 selects freshening or not freshening as needed；Point Catalyst from after is sent into regenerator 13 in regeneration gas (air) 14 after stripped vapor 5 strips the oil gas of removing absorption It is regenerated, 600-680 DEG C of regeneration temperature, the regenerant recycle after regeneration uses.
The present invention will be further illustrated by embodiment below, but the present invention is not therefore subject to any restriction.
The product inspection method of embodiment and comparative example are as follows: reaction product is by N2It brings into -10 DEG C of liquid receipts bottle and carries out gas Liquid separation, gaseous product, which is collected, to be completed to be made of Agilent 6890GC (TCD detector) on-line analysis；After liquid product collection Weighed off line carries out simulation distillation and gasoline detailed hydrocarbon analysis (being tested using RIPP81-90 test method), gasoline respectively Fraction cut point with diesel oil is respectively 221 DEG C and 343 DEG C；Green coke catalyst draw off after in 2000 analysis of carbon and sulfur of multi EA Coke analysis (being tested using RIPP106-90 test method) is carried out on instrument, it is flat that all product quality adductions calculate material Weighing apparatus is faced hydrogen adsorbed product and sulfur in gasoline nitrogen content and is carried out using RIPP 62-90 test method and RIPP 63-90 test method Measurement, tenor are measured using RIPP 124-90 test method.
Inferior feedstock oil used in embodiment and comparative example is shale oil (A), residual oil (B) and decompressed wax oil C, property As shown in table 1.
First catalytic cracking catalyst used in embodiment is identical as the second catalytic cracking catalyst, preparation method letter It states as follows:
1), by 20gNH4Cl is dissolved in 1000g water, and 100g (butt) crystallization product DASY zeolite is added into this solution (production of Qilu Petrochemical Company's catalyst plant, unit cell dimension 2.445-2.448nm, content of rare earth is (with RE2O3Meter)=2.0 Weight %), after 90 DEG C of exchange 0.5h, filter to obtain filter cake；By 4.0gH3PO4(concentration 85%) and 5.4gCo (NO3)2·6H2O is dissolved in It in 90g water, is dried after being mixed with dipping with filter cake, is then handled in 550 DEG C of roasting temperatures and obtain within 2 hours phosphorous and cobalt macropore Zeolite, chemical element composition are as follows: 0.1Na2O·5.1Al2O3·2.4P2O5·1.5Co2O3·3.8RE2O3·88.1SiO2。
2), with 250Kg decationized Y sieve water by 75.4Kg halloysite (Suzhou china clay company industrial products, solid content 71.6m%) be beaten, add 54.8Kg boehmite (Shandong Aluminum Plant's industrial products, solid content 63m%), with hydrochloric acid by its PH is adjusted to 2-4, stirs evenly, and stands aging 1 hour at 60-70 DEG C, holding PH be 2-4, cool the temperature to 60 DEG C hereinafter, plus Enter 41.5Kg Aluminum sol (Qilu Petrochemical Company's catalyst plant product, Al2O3Content is 21.7m%), it stirs 40 minutes, is mixed Close slurries.
By the large pore zeolite (butt 33.8Kg) of the phosphorous and cobalt of step 1) preparation and MFI structure mesoporous ZRP-1 boiling Stone (Qilu Petrochemical Company's catalyst plant industrial products, SiO2/Al2O3=30, butt 3.0Kg) it is added to what step 2) obtained It in mixed serum, stirs evenly, and appropriate extraordinary adhesive, structural promoter and pore creating material is added, be put in bonder after mixing, Suitable quantity of water is added, stirs, places 4 hours in air, spray drying forming, 120 DEG C of drying 3 are small in drying box Shi Hou is washed with ammonium dihydrogen phosphate (phosphorus content 1m%), washes away free Na+, the free Na of washing removing+, drying again is It obtains catalyst and is denoted as CAT-3.The group of the catalyst becomes 4.1 weight %MFI structure mesoporous zeolites, % are phosphorous and cobalt for 20.6 weights DASY zeolite, 29.4 weight % boehmites, 5.5 heavy % Aluminum sols and balance kaolin.Its property is listed in table 2.
Embodiment 1
The embodiment is tested according to the process of Fig. 1, raw material of the shale oil A as catalytic cracking, it is small-sized it is continuous again It is tested on raw fluidized bed riser reactor, is fed under shale oil A, expanding reactor bottom is the riser cracking area 5 times of II internal diameter and become fluidized bed and face hydrogen adsorption zone I, the length for facing hydrogen adsorption zone I is the length of riser cracking area II 14%.Adsorption zone I introduces the cold renewal catalytic cracking agent of outside heat removing as the first catalytic cracking catalyst, with hydrogen volume score 85% dry gas (remaining is methane, ethane and ethylene etc.) flows from bottom to top as hydrogen-containing gas, the conveying of riser cracking area Enter high-temperature thermal regeneration catalytic cracking agent as the second catalytic cracking catalyst；First catalysis is used as using CAT-3 catalyst simultaneously Cracking catalyst and the second catalytic cracking catalyst, micro- reactivity (MAT) of CAT-3 poising agent are 65.Shale oil is through 260 DEG C Preheat the expanding bottom adsorption zone I of laggard fluidized bed riser reactor, at reaction pressure 4.2MPa, H2/ shale oil Volume ratio is 500, as hydrogen-containing gas flows from bottom to top, in 300 DEG C of adsorption temp, the first catalytic cracking catalyst and shale The weight ratio 4.8 of oily A, adsorption time are to carry out facing hydrogen adsorption reaction under the conditions of 12 seconds, removing basic nitrogen compound, sulfide and again Metal impurities；Face hydrogen adsorbed product therewith on be advanced into riser cracking area, 500 DEG C, the second catalytic cracking catalyst with Face the weight ratio 6.4 of hydrogen adsorbed product, catalytic cracking reaction occurs together under the conditions of 3.5 seconds reaction time；The oil gas of generation into Enter fractionating device and obtain diesel oil, slurry oil, fractionating device tower top rich gas is directly entered Vapor recovery unit without rich gas compressor compression and fills The separation of further progress product is set, the products such as dry gas, liquefied gas and gasoline are obtained, slurry oil recycle ratio is 0.1.React certain time Afterwards, catalytic cracking catalyst to be generated is through N2After its internal oil gas adsorbed of stripping removing, it is sent into regenerator and uses air as again Angry body is contacted with catalytic cracking catalyst to be generated at 600~680 DEG C of regeneration temperature and is regenerated；Regenerative agent after regeneration It is recycled.Operating condition and product distribution are listed in table 3.
From table 3 it can be seen that shale oil A first faces hydrogen absorption catalytic cracking again, absorption desulfurization degree 82 is % heavy, denitrification percent 87 Weight %, demetallization per 62.0 are % heavy；Shale oil A faces catalytic cracking again after hydrogen absorption, conversion ratio (100%- diesel yield-slurry oil Yield) it is 68.1 heavy %, slurry oil yield 5.5 is % heavy, and dry gas yied 2.3 is % heavy, % heavy, the liquid product yield of coke yield 7.8 (yield of liquefied gas+yield of gasoline+diesel yield) is up to 84.4 heavy %, and wherein gasoline yield is up to 41.8 heavy %, productivity of propylene Up to 4.9 heavy %；Product gasoline sulfur content 52.5ppm, nitrogen content 85.2ppm.
Comparative example 1
The comparative example is that the first catalytic cracking catalyst and the second catalytic cracking are urged with CAT-3 using shale oil A as raw material Agent, poising agent MAT are 65, are tested on the small-sized fluidized bed riser fluid catalytic cracking of embodiment 1, are different from real It applies example 1: hydrogen-containing gas being replaced with to not hydrogeneous vapor, reactor pressure 0.22MPa, and is not injected into cooling Jie Matter, and shale oil A and water vapour are directly injected into the reaction zone of fluidized-bed reactor, i.e. shale oil A is without absorption directly second Catalytic cracking reaction is carried out on catalytic cracking catalyst；After reaction, fractionating device tower top rich gas compresses pressure-raising through rich gas compressor Enter absorption stabilizing apparatus further progress product after to 1.2-1.6MPa to separate；Heavy oil recycle ratio 0.3.Operating condition and product Distribution is listed in table 3.
From table 3 it can be seen that shale oil A directly carries out non-hydrogen catalytic cracking reaction, conversion ratio 66.6 without absorption Weight %, slurry oil yield 6.5 is % heavy, and dry gas yied 3.0 is % heavy, and coke yield 9.8 is % heavy, and liquid product yield 80.7 is % heavy, Middle gasoline yield 39.3 is % heavy, and productivity of propylene is up to 4.4 heavy %；Product gasoline sulfur content 291.5ppm, nitrogen content 458.6ppm.
It can be seen that from the data of table 3 and processing shale oil A carried out using method of the invention, shale oil conversion capability is high, Recycle ratio is low, and conversion ratio improves 1.5 percentage points, and slurry oil low yield 1.0 percentage points, and dry gas is low with coke yield, Dry gas+coke yield is 2.7 percentage points low, and liquid product yield improves 3.7 percentage points；Product gasoline sulfur content reduces 249.0ppm, nitrogen content reduce 373.4ppm.
Embodiment 2
Embodiment 2 is tested according to the equipment and process of Fig. 2, uses in table 1 residual oil B and decompressed wax oil C as being catalyzed The raw material of cracking, residual oil B and decompressed wax oil C subregion are fed, i.e. residual oil B faces hydrogen adsorption zone I in fluidized bed and feeds and decompressed wax oil C It is fed in riser cracking area II；Reactor bottom fluidized bed it is expanding for turbulent fluidized bed face hydrogen adsorption zone (fluidized bed face hydrogen suction The internal diameter in attached area is 3 times of riser cracking area internal diameter, and the length that fluidized bed faces hydrogen adsorption zone is the riser cracking The 10% of section length), and the first catalytic cracking catalyst of the cooling of outside heat removing is introduced, the dry gas for being 80% with volume fraction (remaining is methane, ethane and ethylene etc.) is used as hydrogen-containing gas；The riser cracking area lower part II is conveyed into the catalysis of high temperature second and splits Change catalyst, forms riser cracking area II promoting pipeline section middle and upper part.The residual oil B for accounting for 30 weight % of combined feed is preheated through 300 DEG C Enter the lower part that the expanding turbulent fluidized bed of riser reactor bottom fluidization bed faces hydrogen adsorption zone I afterwards, with hydrogen-containing gas by Under flow up, weight ratio 3.0, pressure 3.5MPa in 350 DEG C of adsorption temp, the first catalyst and residual oil, adsorption time It is to carry out facing hydrogen adsorption reaction, the impurity such as removing basic nitrogen compound, sulfide and heavy metal, the fluidized bed under the conditions of 5.0 seconds The linear speed that is apparently averaged for facing oil gas in hydrogen adsorption zone I is 0.5 meter per second；Residual oil and the first catalytic cracking catalyst of part are on It is advanced into riser cracking area II, after mixing with the second catalytic cracking catalyst of high temperature from regenerator, with charging, warp at this The decompressed wax oil C of 210 DEG C of preheatings 510 DEG C, oil gas partial pressure be 0.22MPa, the gross weight of the second catalytic cracking catalyst and face hydrogen The ratio between adsorbed product and decompressed wax oil C total weight be 6.0, catalytic cracking reaction occur together under the conditions of 2.5 seconds reaction time, institute It states oil gas in riser cracking area II and is averaged linear speed apparently as 22 meter per seconds (fast bed fluidized state)；The oil gas of generation, which enters, to be divided Distillation unit is fractionated to obtain diesel oil, slurry oil, and fractionating device tower top rich gas is directly entered Vapor recovery unit without rich gas compressor compression and fills The separation of further progress product is set, the products such as dry gas, liquefied gas and gasoline, heavy oil recycle ratio 0.1 are obtained.React certain time Afterwards, it after its internal oil gas adsorbed of catalytic cracking catalyst stripping removing to be generated, is sent into regenerator and uses air as regeneration gas Body is contacted with catalytic cracking catalyst to be generated at 600~680 DEG C of regeneration temperature and is regenerated；Regenerant recycle after regeneration It uses.Operating condition and product distribution are listed in table 4.
From table 4, it can be seen that residual oil B and decompressed wax oil C subregion feed catalytic cracking, and residual oil adsorbs desulfurization in embodiment 2 Rate is 72 heavy %, and denitrification percent is 70 heavy %, and demetallization per 45.0 is % heavy；Its slurry oil yield is 5.0 heavy %, dry gas yied 2.3 Weight %, coke yield 8.5%, liquid product yield (yield of liquefied gas+yield of gasoline+diesel yield) are up to 84.2 heavy %, Wherein gasoline yield is up to 39.5 heavy %, and productivity of propylene is up to 5.3 heavy %；Product gasoline sulfur content 98.6ppm, nitrogen content 10.1ppm。
Comparative example 2
Catalytic cracking is carried out by method same as Example 2, difference is in comparative example 2: hydrogen-containing gas is replaced For not hydrogeneous vapor, reactor pressure 0.22MPa, and it is not injected into cooling medium, and residual oil B is mixed with wax oil C and water Steam is directly injected into the riser cracking area of fluidized bed riser reactor, i.e. residual oil B is directly split in the second catalysis without absorption Change and carries out catalytic cracking reaction on catalyst；After reaction, fractionating device tower top rich gas through rich gas compressor compress pressure-raising to 1.2~ Enter absorption stabilizing apparatus further progress product after 1.6MPa to separate；Heavy oil recycle ratio 0.2.Operating condition and product distribution column In table 4.
From table 4, it can be seen that residual oil B is directly catalyzed with decompressed wax oil C mixed feeding without absorption in comparative example 2 Cracking reaction, slurry oil yield are 6.5 heavy %, and dry gas yied is 3.4 heavy %, coke yield 9.3%, liquid product yield (yield of liquefied gas+yield of gasoline+diesel yield) is 80.8, and wherein gasoline yield is 36.1 heavy %, productivity of propylene 5.0 Weight %；Product gasoline sulfur content 352.0ppm, nitrogen content 33.6ppm.
It can be seen that from the data of table 4 and processing page residual oil B and wax oil C, conversion capability carried out using method of the invention Height, heavy oil recycle ratio is low, and slurry oil low yield 1.5 percentage points, and dry gas is low with coke yield, and dry gas+coke yield is low 1.9 percentage points, liquid product yield improves 3.4 percentage points；Product gasoline sulfur content reduces 253.4ppm, nitrogen content Reduce 23.5ppm.
Embodiment 3
The embodiment is tested according to the process of Fig. 3, raw material of the residual oil B as catalytic cracking, in small-sized cyclic regeneration It is tested on downflow fluidized bed riser reactor, residual oil B upper feeding, reactor head is expanding to face hydrogen absorption for fluidized bed Area, fluidized bed face 4.2 times of the diameter that the diameter of hydrogen adsorption zone I is riser cracking area II, and the fluidized bed faces hydrogen adsorption zone I Length be riser cracking area II length 30% and it is built-in in cooling first catalytic cracking catalyst of heat production coil pipe, promoted Pipeline section is conveyed into the second catalytic cracking catalyst of high temperature；Using CAT-3 catalyst, poising agent MAT=63.Residual oil is pre- through 350 DEG C Enter at the top of the expanding fluidised bed adsorption reaction zone I of reactor after heat, as hydrogen-containing gas flows from top to bottom, in reaction pressure Under 1.8MPa, with hydrogen volume score 70% plus hydrogen tail gas and part dry gas mixed gas as hydrogen-containing gas on to Lower flowing, H2The volume ratio of/feedstock oil is 300, in the weight of 420 DEG C of adsorption temp, the first catalytic cracking catalyst and residual oil Adsorption reaction, the impurity such as removing basic nitrogen compound, sulfide and heavy metal are carried out under the conditions of being 8 seconds than 4.9, adsorption time；Slag Oil is advanced into down downstriker riser cracking area II therewith, 505 DEG C, it is the weight ratio 15 of catalyst and absorption denitrogenation product, anti- Catalytic cracking reaction occurs together under the conditions of 1.5 seconds between seasonable；The oil gas of generation enters fractionating device and obtains diesel oil, slurry oil, point Distillation unit tower top rich gas is directly entered the separation of absorption stabilizing apparatus further progress product without rich gas compressor compression, is done Air-liquid gas, gasoline etc., dry gas are partially recycled back to fluidized bed as needed and face hydrogen adsorption zone I as hydrogen-containing gas.Reaction is certain After time, after its internal oil gas adsorbed of catalytic cracking catalyst stripping removing to be generated, regeneration gas is used air as, again It contacts and is regenerated with catalytic cracking catalyst to be generated at raw 600~700 DEG C of temperature；Regeneration catalyzing cracking agent circulation after regeneration It uses.Operating condition and product distribution are listed in table 5.
As can be seen from Table 5, residual oil B first carries out facing hydrogen absorption and carries out catalytic cracking again, and absorption desulfurization degree 76 is % heavy, takes off Nitrogen rate 85 is % heavy, and demetallization per 58.0 is % heavy；Catalytic cracking again after residual oil B absorption, conversion ratio 67.4 is % heavy, slurry oil yield 6.0 Weight %, dry gas yied 3.3 is % heavy, and coke yield 10.2 is % heavy, and liquid product yield is up to 80.5 heavy %, and wherein gasoline yield is high Up to 39.4 heavy %, productivity of propylene is up to 4.4 heavy %；Product gasoline sulfur content 96.4ppm, nitrogen content 13.3ppm.
Comparative example 3
The comparative example is using residual oil B as raw material, and using CAT-3 as catalyst, poising agent MAT is 63, in the small-sized of embodiment 3 It is tested on downflow fluidized bed riser fluid catalytic cracking, different from embodiment 3: hydrogen-containing gas being replaced with and is free of The vapor of hydrogen, reactor pressure 0.14MPa, and it is not injected into cooling medium, and residual oil B and water vapour are directly injected into fluidized bed The riser cracking area of reactor, i.e. residual oil B go downstream with catalyst, residual oil without be adsorbed under non-hydrogen atmosphere directly into Row catalytic cracking reaction；After reaction, fractionating device tower top rich gas enters after rich gas compressor compresses pressure-raising to 1.2-1.6MPa The separation of absorption stabilizing apparatus further progress product；Heavy oil recycle ratio 0.2.Operating condition and product distribution are listed in table 5.
As can be seen from Table 5, residual oil B directly carries out catalytic cracking reaction without being adsorbed under non-hydrogen atmosphere, converts Rate 66.9 is % heavy, and slurry oil yield 7.5 is % heavy, and dry gas yied 4.0 is % heavy, and coke yield 11.0 is % heavy, liquid product yield 77.5 Weight %, wherein gasoline yield 38.1 is % heavy, and productivity of propylene is up to 4.1 heavy %；Product gasoline sulfur content 401.5ppm, nitrogen content 88.8ppm。
It can be seen that from the data of table 5 and processing residual oil B carried out using method of the invention, crude conversion ability is high, freshening Than low, conversion ratio improves 0.5 percentage point, and slurry oil low yield 1.5 percentage points, and dry gas is low with coke yield, and dry gas+ Coke yield is 1.5 percentage points low, and liquid product yield improves 3.0 percentage points；Product gasoline sulfur content reduces 305.1ppm, nitrogen content reduce 75.5ppm.
The property of inferior feedstock oil used in 1 embodiment of the present invention of table and comparative example
Inferior feedstock oil title Shale oil Residual oil Decompressed wax oil
Number A B C
Density (20 DEG C), kg/m3 928 942.7 919
100 DEG C of kinematic viscosity, millimeter2/ the second 9.03 62.8 8.6
Carbon residue, weight % 3.1 6.5 0.12
Condensation point, DEG C 24 33 /
Asphalitine, weight % 1.3 2.4 /
Colloid, weight % 35.7 13.0 /
Element composition
Carbon, weight % 83.28 86.82 86.33
Hydrogen, weight % 11.65 12.07 12.66
Sulphur, weight % 0.53 0.53 0.64
Nitrogen, weight % 2.34 0.37 0.12
Oxygen, weight % 2.2 0.21 /
Tenor, ppm
Iron 11.0 11.2 1.8
Nickel 6.6 7.6 3.8
Calcium 0.1 8.5 3.3
Vanadium <0.1 8.2 0.4
Sodium 1.3 1.2 2.0
Boiling range, DEG C
Initial boiling point 305 340 347
30% 410 421 420
50% 510 558 437
Catalyst CAT-3 used in 2 embodiment of the present invention of table and comparative example
Catalyst number CAT-3
Zeolite type Mesoporous and large pore zeolite
Chemical composition, weight %
Silica 52.7
Aluminium oxide 42.0
Sodium oxide molybdena 0.30
Cobalt oxide 1.6
Rare earth 3.4
Apparent density, kg/m3 750
Pore volume, ml/g 0.40
Specific surface area, rice2/ gram 196
Abrasion index, again when %-1 1.5
Screening composition, weight %
0~40 micron 20.5
40~80 microns 55.2
> 80 microns 24.3
Table 3 is the operating condition and product distribution of the embodiment of the present invention 1 and comparative example 1
Embodiment 1 Comparative example 1
Feedstock oil Shale oil A Shale oil A
Feeding manner Fluidized bed faces the charging of hydrogen adsorption zone The charging of riser cracking area
Catalyst title CAT-3 CAT-3
Leveler activity (MAT) 65 65
Recycle ratio 0.1 0.3
Reactor top pressure, MPa 4.2 0.22
Fluidized bed faces hydrogen adsorption zone operating condition
Raw material preheating temperature, DEG C 260 260
H2The volume ratio of/feedstock oil 500 /
Adsorption temp, DEG C 300 /
Adsorption time, s 12.0 /
Catalyst/shale oil weight ratio 4.8 /
Desulfurization degree, weight % 82.0
Denitrification percent, weight % 87.0 /
Demetallization per, weight % 62.0
Riser cracking area operating condition
Reaction zone temperature of lower, DEG C 530 530
Reaction zone middle portion temperature, DEG C 510 510
Reaction zone upper temp, DEG C 500 500
Catalyst/shale oil weight ratio 6.4 6.4
Oil gas residence time, s 3.5 3.5
Vapor/total raw material weight ratio 0.5 0.5
Product distribution, weight %
Dry gas 2.3 3.0
Liquefied gas 16.2 14.5
Propylene 4.9 4.4
Gasoline 41.8 39.3
Diesel oil 26.4 26.9
Slurry oil 5.5 6.5
Coke 7.8 9.8
It is total 100.0 100.0
Conversion ratio, weight % 68.1 66.6
Liquid product yield, weight % 84.4 80.7
Gasoline quality
Sulfur content, ppm 52.5 291.5
Nitrogen content, ppm 85.2 458.6
Table 4 is the operating condition and product distribution of the embodiment of the present invention 2 and comparative example 2
Embodiment 2 Comparative example 2
Feedstock oil 30%B+70%C 30%B+70%C
Feeding manner Subregion charging Mixed feeding
Catalyst title CAT-3 CAT-3
Leveler activity (MAT) 65 65
Recycle ratio 0.1 0.2
Reactor top pressure, MPa 3.5 0.22
Fluidized bed faces hydrogen adsorption zone operating condition
Raw material preheating temperature, DEG C 300 210
H2The volume ratio of/residual oil B 500 /
Adsorption temp, DEG C 350 /
Adsorption time, s 5.0 /
Catalyst/residual oil B weight ratio 3.0 /
Slag oil desulfurization rate, weight % 72.0 /
Residual oil denitrification percent, weight % 70.0 /
Residual oil demetallization per, weight % 45.0 /
Riser cracking area operating condition
Reaction zone temperature of lower, DEG C 540 540
Reaction zone middle portion temperature, DEG C 515 515
Reaction zone upper temp, DEG C 510 510
The weight ratio of catalyst/feed oil (B+C) 6.0 6.0
Oil gas residence time, s 2.5 2.5
Vapor/total raw material weight ratio 0.5 0.5
Product distribution, weight %
Dry gas 2.3 3.4
Liquefied gas 17.2 16.5
Propylene 5.3 5.0
Gasoline 39.5 36.1
Diesel oil 27.5 28.2
Slurry oil 5.0 6.5
Coke 8.5 9.3
It is total 100.0 100.0
Conversion ratio, weight % 67.5 65.3
Liquid product yield, weight % 84.2 80.8
Gasoline quality
Sulfur content, ppm 98.6 352.0
Nitrogen content, ppm 10.1 33.6
Table 5 is the operating condition and product distribution of the embodiment of the present invention 3 and comparative example 3

Claims (16)

1. a kind of processing method of inferior feedstock oil, this method comprises:
A, the fluidized bed that hydrogen-containing gas and inferior feedstock oil are sent into fluidized bed riser reactor is faced in hydrogen adsorption zone (I) with the One catalytic cracking catalyst contacts and carries out facing hydrogen adsorption reaction, obtains facing hydrogen adsorbed product；The item for facing hydrogen adsorption reaction Part includes: that temperature is 200-450 DEG C, and pressure is 0.5-5.0 megapascal, and adsorption time is 1-90 seconds, and agent oil weight ratio is (0.5- 5): 1, hydrogen to oil volume ratio 100-1000；
B, gained in step a is faced hydrogen adsorbed product to be sent into the riser cracking area (II) of the fluidized bed riser reactor Catalytic cracking reaction is contacted and carried out with the second catalytic cracking catalyst, obtains catalytic cracking oil gas；The catalytic cracking reaction Condition include: temperature be 460-540 DEG C, pressure be 0.5-5.0 megapascal, the oil gas residence time be -15 seconds 0.5 second, agent oil weight Amount is than being (5-30): 1.
2. processing method according to claim 1, this method further include: enter gained cycle oil pneumatic transmission in step b Fractionating device (8) carries out fractionation processing, obtain include rich gas catalytic cracking production；By gained rich gas without rich gas compressor It is sent directly into absorption stabilizing apparatus (10) and carries out Vapor recovery unit processing.
3. processing method according to claim 1, this method further include: in stepb, by Conventional catalytic cracking feedstock oil With it is described face the catalytic cracking reaction is carried out together with hydrogen adsorbed product；Wherein, the Conventional catalytic cracking feedstock oil be selected from At least one of wax oil, reduced crude and decompressed wax oil.
4. processing method according to claim 1, wherein the hydrogen-containing gas includes hydrogen and/or dry gas, the poor quality Feedstock oil is at least one in shale oil, liquefied coal coil, tar sand oil, wax tailings, residual oil, hydrogenated residue and deasphalted oil Kind.
5. processing method according to claim 1, wherein first catalytic cracking catalyst and the second catalytic cracking are urged The composition of agent is identical, the inorganic oxide of zeolite, 5-99 weight % including 1-50 weight % and gluing for 0-70 weight % Soil.
6. processing method according to claim 5, wherein the zeolite includes mesopore zeolite and/or large pore zeolite, described Mesopore zeolite is selected from ZSM-5 zeolite, ZSM-11 zeolite, ZSM-12 zeolite, ZSM-23 zeolite, ZSM-35 zeolite, ZSM-38 boiling At least one of stone, ZSM-48 zeolite and ZRP zeolite, the large pore zeolite be selected from rare earth Y type zeolite, rare earth hydrogen Y zeolite, At least one of Y-type high-Si zeolite and ultrastable；The inorganic oxide is silica and/or aluminium oxide；It is described viscous Soil is selected from silica, kaolin, halloysite, montmorillonite, diatomite, galapectite, saponite, rectorite, sepiolite, recessed At least one of convex stick stone, hydrotalcite and bentonite.
7. processing method according to claim 1, wherein first catalytic cracking catalyst is the fresh catalyst of supplement Cracking catalyst, the regeneration catalyzing Cracking catalyst of cooling, the semi regeneration catalytic cracking catalyst of cooling and the to be generated of cooling are urged At least one of fluidized cracking catalysts, second catalytic cracking catalyst are regeneration catalyzing Cracking catalyst；Described first The temperature of catalytic cracking catalyst is 200-500 DEG C, and the temperature of the second catalytic cracking catalyst is 580-680 DEG C.
8. processing method according to claim 1, wherein the condition for facing hydrogen adsorption reaction includes: that temperature is 250- 400 DEG C, pressure is 1.0-4.0 megapascal, and adsorption time is 2-60 seconds, and agent oil weight ratio is (1-4): 1, hydrogen to oil volume ratio 300- 800；The condition of the catalytic cracking reaction includes: that temperature is 480-530 DEG C, and pressure is 1.0-4.0 megapascal, oil gas residence time It is 1.0-10 seconds, agent oil weight ratio is (6-30): 1.
9. processing method according to claim 1, this method further include: cooling medium is sent into the fluidized bed and faces hydrogen suction Temperature control is carried out in attached area (I)；The cooling medium is at least one in cold hydrogen, water, gasoline, diesel oil, recycle oil and fused salt Kind.
10. a kind of system of processing of inferior feedstock oil, which is characterized in that the system of processing includes being provided with fluid bed section and promotion The fluidized bed riser reactor of pipeline section is formed with fluidized bed in the fluid bed section and faces hydrogen adsorption zone (I), the promotion pipeline section Inside it is formed with riser cracking area (II)；
The fluidized bed faces hydrogen adsorption zone (I) and connects and be in fluid communication with riser cracking area (II), and the fluid bed section is set It is equipped with hydrogen-containing gas entrance, inferior raw material oil-in and the first catalytic cracking catalyst entrance, the promotion pipeline section is provided with Two catalytic cracking catalyst entrances, the outlet of catalytic cracking oil gas and catalytic cracking catalyst outlet, are arranged or are not provided with routine Catalytically cracked stock entrance.
11. system of processing according to claim 10, wherein the system of processing further includes fractionating device (8) and absorbs Stabilising arrangement (10), the oil gas entrance and the catalytic cracking oil gas communication of the fractionating device (8), the fractionation The rich gas outlet of device (8) and the rich gas entrance of the absorption stabilizing apparatus (10) are in fluid communication.
12. system of processing according to claim 10, wherein the system of processing further includes regenerator (13), it is described again Raw device (13) are provided with regenerator catalyst outlet and regenerator catalyst entrance, the regenerator catalyst outlet and described the One catalytic cracking catalyst entrance and the second catalytic cracking catalyst entrance connection, the regenerator catalyst entrance with it is described Catalytic cracking catalyst outlet.
13. system of processing according to claim 12, wherein regenerator catalyst outlet by heat collector (17) with The first catalytic cracking catalyst entrance connection.
14. system of processing according to claim 10, wherein the promotion pipeline section is upstriker riser reactor, institute It states fluid bed section and is located at the lower section for promoting pipeline section, and the first catalytic cracking catalyst entrance is located under the fluid bed section Portion, the second catalytic cracking catalyst entrance are located at the lower part for promoting pipeline section, and the catalytic cracking catalyst exports position In the top for promoting pipeline section；
Alternatively, the promotion pipeline section is downstriker riser reactor, the fluid bed section is located at the top for promoting pipeline section, and institute The top that the first catalytic cracking catalyst entrance is located at the fluid bed section is stated, the second catalytic cracking catalyst entrance is located at The top for promoting pipeline section, the catalytic cracking catalyst outlet are located at the lower part for promoting pipeline section.
15. system of processing according to claim 10, wherein the fluidized bed faces the diameter of hydrogen adsorption zone (I) to be promoted 0.5-5 times of the diameter of the pipe zone of cracking (II), the length that the fluidized bed faces hydrogen adsorption zone (I) is riser cracking area (II) The 1-30% of length.
16. system of processing according to claim 10, wherein the fluid bed section is provided with cooling medium entrance, described Cooling medium entrance and the fluidized bed face hydrogen adsorption zone (I) in direct fluid communication or face hydrogen absorption in the fluidized bed with setting Heat collector (17) in area (I) is in fluid communication.
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CN109705910B (en) * 2017-10-26 2021-01-08 中国石油化工股份有限公司 Method and system for hydrocracking heavy raw oil
CN109705901B (en) * 2017-10-26 2021-01-08 中国石油化工股份有限公司 Method and system for hydrocracking heavy raw oil
CN109701460B (en) * 2017-10-26 2021-11-16 中国石油化工股份有限公司 Method and system for on-line cyclic regeneration of hydrocracking catalyst
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CN110819383A (en) * 2018-08-14 2020-02-21 何巨堂 Process for the upflow hydrogenation of poor quality hydrocarbons using reactors with internal parallel reaction zones
CN111040807B (en) * 2018-10-12 2021-11-16 中国石油化工股份有限公司 Method and system for processing inferior oil by adopting double lifting pipes
CN111040809B (en) * 2018-10-12 2021-11-16 中国石油化工股份有限公司 Hydrogen process method and system for inferior oil
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