CN107267211A - The processing method and system of a kind of inferior feedstock oil - Google Patents
The processing method and system of a kind of inferior feedstock oil Download PDFInfo
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- CN107267211A CN107267211A CN201610211678.3A CN201610211678A CN107267211A CN 107267211 A CN107267211 A CN 107267211A CN 201610211678 A CN201610211678 A CN 201610211678A CN 107267211 A CN107267211 A CN 107267211A
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- oil
- catalytic cracking
- hydrogen
- catalyst
- fluid bed
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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
Abstract
The invention discloses a kind of processing method of inferior feedstock oil and system, this method includes：A, the fluid bed that hydrogen-containing gas and inferior feedstock oil are sent into fluid bed riser reactor, which face, to contact with the first catalytic cracking catalyst in hydrogen adsorption zone (I) and carries out facing hydrogen adsorption reaction, obtains facing hydrogen adsorbed product；B, gained in step a faced into hydrogen adsorbed product send into and contacted in the riser cracking area (II) of the fluid bed riser reactor with the second catalytic cracking catalyst and carry out catalytic cracking reaction, obtain catalytic cracking oil gas.Inferior feedstock oil conversion ratio can be increased substantially and reduce dry gas and coke yield by being processed inferior feedstock oil using the inventive method on present system, so as to realize the clean and efficient utilization of inferior feedstock oil.
Description
Technical field
The present invention relates to a kind of processing method of inferior feedstock oil and system.
Background technology
With petroleum resources shortage and the demand of high-quality gasoline, diesel oil and low-carbon alkene is increasingly increased
Plus, the process technology of the inferior feedstock oil such as oil product such as liquefied coal coil, tar sand oil and poor quality, heavy crude
Increasingly it is taken seriously.Inferior feedstock oil, liquefied coal coil, tar sand oil etc., similar natural oil, but
Contain the non-hydrocarbons organic compounds such as more unsaturated hydrocarbons, and nitrogenous, sulphur and oxygen than natural oil, no
Only influence its secondary processing and utilization, and have an effect on product gasoline, the color of diesel oil and stability, sulphur,
Nitrogen content is high.Current inferior feedstock oil is most of without secondary operation in addition to production chemicals on a small quantity
And sold directly as light-weight fuel oil, it is therefore necessary to develop the skill of more efficient utilization inferior feedstock oils
Art.
Because the heteroatomic compound content such as nitrogen, sulphur, oxygen is higher in inferior feedstock oil, especially nitrogen quality
Fraction is general 1%~3%, it is impossible to the lighting of inferior feedstock oil is carried out directly as catalytically cracked material,
It is primarily due to nitride particularly basic nitrogen compound energy and catalyst acid during catalytic cracking reaction
Property central role and reduce catalyst activity and selectivity, show product distribution on be coking yield increase,
Slurry oil increase, yield of light oil declines.ARCO companies point out that most of catalytic cracking units are 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 made with acid additive
For the agent for capturing of nitrogen, catalytic cracking unit can only also process below the μ g/g of nitrogen content 3000 charging.Separately
Outside, inferior feedstock oil colloid and olefin(e) centent are higher.In catalytic cracking process, 1/3rd colloid
Coke can be generated, and alkene is more active, the two, which is readily adsorbed on catalyst, covers activated centre.Although
The higher temperature of colloid gasification needs, but the more high easier generation coke of reaction temperature.
In summary factor, inferior feedstock oil generally requires first hydrotreating modification, with remove oxygen, nitrogen,
The impurity such as sulphur, then the oil refining processing technology in refinery routinely be processed into various oil products.United States Patent (USP)
US 4342641 discloses a kind of inferior feedstock oil processing method, is first added full cut inferior feedstock oil
Hydrogen processing, the obtained cut for being less than 249 DEG C is directly as jet fuel, and what is obtained is more than 249 DEG C
Cut is hydrocracked again, to produce jet fuel；Wherein hydrotreating is carried out in two steps, and is first used
The low catalyst of Ni-Mo contents carries out prerefining, then is carried out further with the high catalyst of Ni-Mo contents
It is refined.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, the processing method of hydrogenation heavy oil catalytic pyrolysis again, such as Chinese patent CN 1067089A institutes
State, inferior feedstock oil first passes through hydrotreating and obtains hydrogenated oil, hydrogenated oil is separated into hydrogenation weight
Oil and light-end products, hydrogenation heavy oil obtain dry gas, liquefied gas, gasoline, diesel oil and urged after catalytic cracking
Change heavy oil, diesel oil and heavy-cycle oil can return to hydrotreating step；Simply Chinese patent CN 102465036A
Inferior feedstock oil hydrogenation heavy oil carry out catalytic cracking reactions using two riser reactors, and
Hydrogenated oil obtained by CN 102453546A enters catalytic pyrolysis together with optional vacuum gas oil (VGO) and filled
Put.In a word, inferior feedstock oil carries out hydrofinishing, and the heavy oil being refining to obtain is used as existing catalytic cracking skill
The processing method of the raw material of art, can change into light-end products by inferior feedstock oil.
Inferior feedstock oil hydrotreating has high simple to operate, purpose product yield, good product quality and nothing
The advantages of three waste discharge, be 21 century environment-friendly processing technology.But, nonhydrocarbon in inferior feedstock oil
Compound impurities are harmful substance in hydrotreating, are the objects to be removed or converted, but itself
It is useful industrial chemicals, therefore is considered as extracting and utilizes；In addition, if inferior feedstock oil oxygen contains
Amount is higher, then influences life-span and the efficiency of hydrogenation catalyst.Hydrogen addition technology only has Australia SPP at present
Company reaches the commerical test stage, and super-low sulfur light-weight fuel oil is produced by hydrofinishing.
Non- hydrotreating, which is mainly, uses acid-alkali refining, such as patent Chinese patent CN 101967389A, acid
Alkali refining can not only produce a large amount of reluctant acid sludges, pollute environment, and oil yield is low；Though
So some researchers are explored with single solvent or multi-solvent extracting and refining method, such as patent Chinese patent in recent years
The problems such as CN CN1746265A, but it is larger to still suffer from solvent consumption, high energy consumption.As environmental protection will
The raising asked, both at home and abroad to the discharge standard continuous improvement of light-weight fuel oil combustion tail gas, to automobile-used lightweight
The limitation of the sulphur of fuel oil, nitrogen and arene content is lower, so be extremely difficult to using non-hydroprocessing process will
Ask.
Therefore, in order to efficiently utilize inferior feedstock oil resource, the need of growing light-weight fuel oil are met
Ask, it is necessary to develop a kind of light-weight fuel oil that inferior feedstock oil Efficient Conversion is a large amount of lightweights and cleaned
Method.
The content of the invention
It is an object of the invention to provide a kind of processing method of inferior feedstock oil and system, adopt on this system
Inferior feedstock oil is processed with this method can increase substantially inferior feedstock oil conversion ratio and reduce dry
Gas and coke yield, so as to realize the clean and efficient utilization of inferior feedstock oil.
To achieve these goals, the present invention provides a kind of processing method of inferior feedstock oil, this method bag
Include：A, the fluid bed that hydrogen-containing gas and inferior feedstock oil are sent into fluid bed riser reactor face hydrogen and inhaled
Contacted in attached area with the first catalytic cracking catalyst and carry out facing hydrogen adsorption reaction, obtain facing hydrogen absorption production
Thing；B, gained in step a faced into the lifting that hydrogen adsorbed product sends into the fluid bed riser reactor
Contacted in the pipe zone of cracking with the second catalytic cracking catalyst and carry out catalytic cracking reaction, obtain catalytic cracking
Oil gas.
Preferably, this method also includes：Gained cycle oil pneumatic transmission in step b is entered into fractionating device to enter
Row fractionation is handled, and obtains including the catalytic cracking production of rich gas；By gained rich gas without rich gas compressor
It is sent directly into absorption stabilizing apparatus and carries out Vapor recovery unit processing.
Preferably, this method also includes：In stepb, Conventional catalytic cracking feedstock oil is faced with described
Hydrogen adsorbed product carries out the catalytic cracking reaction together；Wherein, the Conventional catalytic cracking feedstock oil is
Selected from least one of wax oil, reduced crude and decompressed wax oil.
Preferably, the hydrogen-containing gas includes hydrogen and/or dry gas, and the inferior feedstock oil is selected from page
In shale oil, liquefied coal coil, tar sand oil, wax tailings, residual oil, hydrogenated residue and deasphalted oil at least
It is a kind of.
Preferably, the composition of first catalytic cracking catalyst and the second catalytic cracking catalyst is identical,
Include the clay of 1-50 weight % zeolite, 5-99 weight % inorganic oxide and 0-70 weight %.
Preferably, the zeolite include mesopore zeolite and/or large pore zeolite, the mesopore zeolite be selected from
ZSM-5 zeolite, ZSM-11 zeolites, ZSM-12 zeolites, ZSM-23 zeolites, ZSM-35 zeolites,
At least one of ZSM-38 zeolites, ZSM-48 zeolites and ZRP zeolites, the large pore zeolite are choosing
From in rare earth Y type zeolite, rare earth hydrogen Y zeolites, Y-type high-Si zeolite and ultrastable at least
It is a kind of；The inorganic oxide is silica and/or aluminum oxide；The clay is selected from silica, height
It is ridge soil, halloysite, montmorillonite, diatomite, galapectite, saponite, rectorite, sepiolite, recessed
At least one of convex rod stone, hydrotalcite and bentonite.
Preferably, first catalytic cracking catalyst is the fresh catalyst Cracking catalyst of supplement, cooling
Regeneration catalyzing Cracking catalyst, the semi regeneration catalytic cracking catalyst of cooling and the catalysis to be generated of cooling split
Change at least one of catalyst, 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
For 580-680 DEG C.
Preferably, the condition for facing hydrogen adsorption reaction includes：Temperature is 200-450 DEG C, and pressure is
0.5-5.0 MPas, adsorption time is 1-90 seconds, and agent weight of oil ratio is (0.5-5)：1, hydrogen to oil volume ratio
For 100-1000；The condition of the catalytic cracking reaction includes：Temperature is 460-540 DEG C, and pressure is
0.5-5.0 MPas, the oil gas residence time is -15 seconds 0.5 second, and agent weight of oil ratio is (5-30)：1.
Preferably, this method also includes：Cooling medium is sent into the fluid bed and faces progress in hydrogen adsorption zone
Temperature control；The cooling medium be in cold hydrogen, water, gasoline, diesel oil, recycle oil and fused salt at least
It is a kind of.
The present invention also provides a kind of system of processing of inferior feedstock oil, wherein, the system of processing includes setting
Have in the fluid bed riser reactor of fluid bed section and lifting pipeline section, the fluid bed section and be formed with fluidisation
Bed, which faces in hydrogen adsorption zone, the lifting pipeline section, is formed with riser cracking area；The fluid bed faces hydrogen absorption
Area connects and is in fluid communication with riser cracking area, the fluid bed section be provided with hydrogen-containing gas entrance,
Inferior raw material oil-in and the first catalytic cracking catalyst entrance, the lifting pipeline section are provided with the second catalysis
Cracking catalyst entrance, the outlet of catalytic cracking oil gas and catalytic cracking catalyst outlet, set or are not provided with
There is Conventional catalytic cracking raw material oil-in.
Preferably, the system of processing also includes fractionating device and absorption stabilizing apparatus, the fractionating device
Oil gas entrance and the catalytic cracking oil gas communication, the rich gas outlet of the fractionating device with
The rich gas entrance of the absorption stabilizing apparatus is in fluid communication.
Preferably, the system of processing also includes regenerator, and the regenerator is provided with regenerator catalyst
Outlet and regenerator catalyst entrance, the regenerator catalyst outlet are catalyzed with first catalytic cracking
Agent entrance and the connection of the second catalytic cracking catalyst entrance, the regenerator catalyst entrance are urged with described
Fluidized cracking catalysts outlet.
Preferably, the regenerator catalyst outlet passes through heat collector and first catalytic cracking catalyst
Entrance is connected.
Preferably, the lifting pipeline section is upstriker riser reactor, and the fluid bed section is located at lifting
The lower section of pipeline section, and the first catalytic cracking catalyst entrance is located at the bottom of the fluid bed section, institute
State the bottom that the second catalytic cracking catalyst entrance is located at the lifting pipeline section, the catalytic cracking catalyst
Outlet is located at the top of the lifting pipeline section；Or, the lifting pipeline section is downstriker riser reactor,
The fluid bed section is located at the top of lifting pipeline section, and the first catalytic cracking catalyst entrance is located at institute
The top of fluid bed section is stated, the second catalytic cracking catalyst entrance is located at the upper of the lifting pipeline section
Portion, the catalytic cracking catalyst outlet is located at the bottom of the lifting pipeline section.
Preferably, the fluid bed faces the 0.5-5 of the diameter in a diameter of riser cracking area of hydrogen adsorption zone
Times, the fluid bed faces 1-30% of the length of hydrogen adsorption zone for the length in riser cracking area.
Preferably, the fluid bed section is provided with cooling medium entrance, the cooling medium entrance with it is described
Fluid bed faces hydrogen adsorption zone in direct fluid communication or faces taking in hydrogen adsorption zone with being arranged on the fluid bed
Hot device is in fluid communication.
The present invention has following technique effect compared with prior art：
(1) inferior feedstock oil can be directly processed without refinement treatment, inferior feedstock oil
Work flow it is short, hydrogen consumption is low, and can realize long period continuous production；
(2) present invention is processed inferior feedstock oil using " device two is anti-", i.e., in a reactor
Interior to load identical or different the first catalytic cracking catalyst and the second catalytic cracking catalyst, both are urged
Agent cooperates with completion inferior feedstock oil absorption sulfide, basic nitrogen compound, a huge sum of money in same reaction atmosphere
The impurity such as category and colloid and the function of inferior feedstock oil catalytic cracking, then can be in same regeneration atmosphere
While activity recovery；
(3) pole such as the first adsorbing and removing sulfide of inferior feedstock oil, basic nitrogen compound, heavy metal and colloid
Property material catalytic cracking again, inferior feedstock oil high conversion rate, dry gas and coke yield are low, reduce device
Green coke, fluid product (liquefied gas+gasoline+diesel oil) yield is high；
(4) inferior feedstock oil is adsorbed in the case where facing hydrogen atmosphere, is more beneficial for the first catalytic cracking catalysis
Agent is to sulfur-bearing, nitrogenous and oxygenatedchemicals adsorbing and removing in inferior feedstock oil, the first catalytic cracking catalysis
Agent and inferior raw material weight of oil are than reducing, and adsorption time is short, and fluid product sulphur, nitrogen content be low and quality better；
(5) system of processing is facing hydrogen band pressing operation, accordingly improves the richness into absorption stabilizing apparatus
The pressure of gas, eliminates the rich gas compressor of conventional FCC process, plant energy consumption reduction；
(6) fluid bed riser reactor is more suitable for the characteristics of catalytic cracking reaction is fast, with fixed bed and
Moving bed is compared, and reactor volume utilization rate is high, is more suitable for the continuous operation of large-scale production, and can
To be transformed using existing riser reactor device.
Other features and advantages of the present invention will be described in detail in subsequent embodiment part.
Brief description of the drawings
Accompanying drawing is, for providing a further understanding of the present invention, and to constitute a part for specification, with
Following embodiment is used to explain the present invention together, but is not construed as limiting the invention.
In accompanying drawing：
Fig. 1 is the schematic flow sheet for the first embodiment for including processing method of the present invention, is also
The structural representation of the first embodiment including system of processing of the present invention；
Fig. 2 is the schematic flow sheet for second of embodiment for including processing method of the present invention, is also
The structural representation of second of embodiment including system of processing of the present invention；
Fig. 3 is the schematic flow sheet for the third embodiment for including processing method of the present invention, is also
The structural representation of the third embodiment including system of processing of the present invention.
Description of reference numerals
I fluid beds face the hydrogeneous pre-lift medium in hydrogen adsorption zone II riser crackings area 1
The hydrogen-containing gas of 2 fluid bed riser reactor, 3 inferior feedstock oil 4
The pipeline of 5 stripped vapor, 6 settler 7
The absorption stabilizing apparatus of 8 fractionating device, 9 pipeline 10
The regenerator of 11 dry gas, 12 pipeline 13
The pipeline of 14 regeneration gas, 15 flue gas 16
The cooling medium of 17 heat collector, 18 cooling medium entrance 19 is exported
The pipeline 22 of 20 pipeline 21 lifts medium
23 Conventional catalytic cracking feedstock oils
The 24 Conventional catalytic cracking liquefied gas of feedstock oil atomizing medium 25
The slurry oil of 26 gasoline, 27 diesel oil 28
Embodiment
The embodiment of the present invention is described in detail below in conjunction with accompanying drawing.It should be appreciated that
Embodiment described herein is merely to illustrate and explain the present invention, and is not limited to this hair
It is bright.
The present invention provides a kind of processing method of inferior feedstock oil, and this method includes：A, by hydrogen-containing gas
With inferior feedstock oil send into fluid bed riser reactor fluid bed face in hydrogen adsorption zone I with first catalysis
Cracking catalyst contacts and carries out facing hydrogen adsorption reaction, obtains facing hydrogen adsorbed product；B, by step a
Gained faces hydrogen adsorbed product and sent into the riser cracking area II of the fluid bed riser reactor with the
Two catalytic cracking catalysts contact and carry out catalytic cracking reaction, obtain catalytic cracking oil gas.
The present inventor passes through years of researches it was unexpectedly observed that nitrogenous chemical combination in inferior feedstock oil
Thing, sulfur-containing compound and oxygenatedchemicals etc. can be by adsorbing and removings, and catalytic cracking catalyst is in itself
Adsorbent can also be used as；Particularly in the case where facing hydrogen atmosphere, adsorption time is short, is more beneficial for the first catalysis
Cracking catalyst is to sulfur-containing compound in inferior feedstock oil, nitrogen-containing compound, oxygenatedchemicals and metal
Adsorbing and removing, makes the high conversion rate of inferior feedstock oil, and fluid product sulphur, nitrogen content are low, quality better.
According to the present invention, this method can also include：Gained cycle oil pneumatic transmission in step b is entered to divide
Distillation unit 8 carries out fractionation processing, obtains including the catalytic cracking production of rich gas；By gained rich gas without
Rich gas compressor is sent directly into absorption stabilizing apparatus 10 and carries out Vapor recovery unit processing.Existing Conventional catalytic splits
Change device reaction and fractionating system is operated under 0.1-0.25MPa pressure, and absorption stabilizing apparatus is needed
Operated under more than 1.1MPa pressure, therefore Conventional catalytic cracking device must be provided with rich gas pressure
Contracting machine is compressed pressure-raising to the rich gas from fractionating device, and reaction system of the present invention is to face hydrogen with pressure
Operated under (0.5-5.0MPa), accordingly improve the pressure that rich gas enters absorption stabilizing apparatus, can save
Rich gas compressor in conventional FCC process, so as to reduce plant energy consumption and cost input.Fractionating device
Obtaining the rich gas at the top of rich gas, diesel oil and slurry oil, fractionating device (fractionating column) can compress without rich gas
Machine compression is directly entered absorption stabilizing apparatus and further carries out product separation, obtains dry gas, liquefied gas and vapour
Oil etc..The boiling range 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 step
In b, by Conventional catalytic cracking feedstock oil with it is described face hydrogen adsorbed product together with carry out the Catalytic Cracking Unit of Measure
Should；Wherein, the Conventional catalytic cracking feedstock oil can be selected from wax oil, reduced crude and decompressed wax oil
At least one of.The inferior feedstock oil faces the charging of hydrogen adsorption zone in the fluid bed, and Conventional catalytic splits
Change feedstock oil to feed in the riser cracking area；Face hydrogen absorption and remove inferior feedstock oil and portion after impurity
The first catalytic cracking catalyst is divided to enter the riser cracking area, the routine with entering riser cracking area
Catalytically cracked stock contacts second catalytic cracking catalyst together, carries out the Catalytic Cracking Unit of Measure
Should.
According to the present invention, hydrogen-containing gas is well-known to those skilled in the art, can both be made as hydrogen source
With, can also as inferior feedstock oil conveying gas use, it constitutes the present invention and is not particularly limited, example
Such as, the hydrogen-containing gas can include hydrogen and/or dry gas, can also include that nitrogen and vapor etc. are non-to be contained
Hydrogen medium, non-not contained containing hydrogen medium or containing micro oxygen, volume integral of the oxygen in hydrogen-containing gas
Number is not more than 1%；Inferior feedstock oil is known to those skilled in the art, can be selected from shale oil,
At least one of 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, carbon hydrogen element weight ratio
Can be 7-9, and the non-hydrocarbons organic compound content such as nitrogen, sulphur and oxygen is higher, and nitrogen content can be
0.5%-5%, sulfur content can be 0.5%-10%, and oxygen content can be 0.5%-20%.
In the present invention, the inferior feedstock oil can be first passed through to be reacted after preheating in feeding reactor,
The temperature of the preheating 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 described first urges
Fluidized cracking catalysts can be identical or difference with second catalytic cracking catalyst, and catalytic cracking is urged
The activity of agent can be 40-70, preferably 45-60.The composition of catalytic cracking catalyst can include：
Zeolite, inorganic oxide and optional clay；First catalytic cracking catalyst and second catalytic cracking
The concrete composition and usage amount of catalyst, both depending on inferior feedstock oil nitrogen content and denitrogenation requirement, and by
Catalytic cracking reaction condition is determined, it is preferable that first catalytic cracking catalyst is urged with described second
Fluidized cracking catalysts composition is identical, may each comprise 1-50 weight % zeolite, 5-99 weight % it is inorganic
The clay of oxide and 0-70 weight %.Wherein, zeolite can be mesopore zeolite and/or optional macropore
Zeolite, mesopore zeolite can account for the 80-100 weight % of zeolite gross weight, preferably account for 90 weight %-100 weights %；
Large pore zeolite can account for the 0-20 weight % of zeolite gross weight, preferably account for 0 weight %-10 weights %.The mesopore
Zeolite can be ZSM series zeolites and/or ZRP zeolites, preferably be selected from ZSM-5 zeolite, ZSM-11 boilings
Stone, ZSM-12 zeolites, ZSM-23 zeolites, ZSM-35 zeolites, ZSM-38 zeolites, ZSM-48
At least one of zeolite and ZRP zeolites, can also include the zeolite of other similar structures.It is relevant
More description may refer to United States Patent (USP) US3,702,886, relevant ZRP zeolites to ZSM-5 zeolite in detail
More detailed description may refer to United States Patent (USP) US5,232,675.The large pore zeolite can be Y systems
Row zeolite, can include rare earth Y type zeolite (REY), rare earth hydrogen Y zeolites (REHY), super steady Y
At least one of type zeolite (can be obtained by distinct methods) and Y-type high-Si zeolite.The inorganic oxygen
Compound, generally as bonding agent, can be silica (SiO2) and/or aluminum oxide (Al2O3), with butt
Silica can account for the heavy % of 50 weight -90 in weight meter, inorganic oxide, and aluminum oxide can account for 10 weights -50
Weight %.The clay, as matrix (i.e. carrier), can be selected from silica, kaolin, many water
Kaolin, montmorillonite, diatomite, galapectite, saponite, rectorite, sepiolite, attapulgite, water
At least one of talcum and bentonite., can be using transition metal such as iron, cobalt, nickel under preferable case
Elemental constituent is modified to above-mentioned macropore, mesopore zeolite, inorganic oxide and clay etc..First catalysis
Cracking catalyst and the second catalytic cracking catalyst based on microspheroidal, diameter can be respectively be more than 0 to
200 microns, more preferably 40-150 microns, catalyst apparent density can be respectively 0.4-1.9
g/cm3, more preferably 0.8-1.5g/cm3。
According to the present invention, the first catalytic cracking catalyst and the second catalytic cracking catalyst can be big for particle
Small different catalyst and/or the different catalyst of apparent bulk density.The different catalyst of granular size and
/ or the active component of the different catalyst of apparent bulk density can also select different type zeolite respectively, or
Person's metal, nonmetallic modifying zeolite, the catalyst and/or apparent bulk density of particle of different sizes are different
Catalyst can respectively enter different riser cracking areas, for example, containing high silica alumina ratio hyperastable Y-type RE
The short grained catalyst of type zeolite can enter fluidized bed and face hydrogen adsorption zone I (as the first catalytic cracking
Catalyst), increase basic nitrogen compound, heavy metal and/or colloid, the absorption of asphalitine isopolarity material take off
Except reaction.The catalyst of bulky grain containing ultrastable can enter riser cracking area II and (make
For the second catalytic cracking catalyst), increase catalytic cracking reaction, the different catalyst of granular size is same
One stripper is stripped and the regeneration of same regenerator, and bulky grain and catalyst particle, small is then demultiplex out
Grain catalyst faces hydrogen adsorption zone I through cooling down into fluidized bed.The different catalyst of granular size can be
Demarcate between 30-40 microns, the different catalyst of apparent bulk density can be in 0.6-0.7g/cm3Between point
Boundary.
According to the present invention, in order to control the temperature for facing hydrogen adsorption reaction and catalytic cracking reaction, described first
Catalytic cracking catalyst can urge for the fresh catalyst Cracking catalyst of supplement, the regeneration catalyzing cracking of cooling
In the catalytic cracking catalyst to be generated of agent, the semi regeneration catalytic cracking catalyst of cooling and cooling at least
One kind, second catalytic cracking catalyst can be regeneration catalyzing Cracking catalyst；First catalysis
The temperature of Cracking catalyst can be 200-500 DEG C, and more preferably 230-480 DEG C, the second catalytic cracking is urged
The temperature of agent can be 580-680 DEG C.Under preferable case, first catalytic cracking catalyst can be with
Intermixture after being exchanged heat for regeneration catalyzing Cracking catalyst and fresh catalyst Cracking catalyst, after heat exchange
Fresh catalyst Cracking catalyst to nitrogen especially basic nitrogen advantages of good adsorption effect, denitrification percent is high；And through inhaling
Fresh catalyst Cracking catalyst after attached denitrogenation, activity reduction, green coke is low in catalytic cracking process.
According to the present invention, it is well known to those skilled in the art to face hydrogen adsorption reaction and catalytic cracking reaction
, for example, the condition for facing hydrogen adsorption reaction can include：Temperature is 200-450 DEG C, is preferably
250-400 DEG C, pressure is 0.5-5.0 MPas, and preferably 1.0-4.0 MPas, adsorption time is 1-90 seconds,
Preferably 2-60 seconds, agent weight of oil ratio was (0.5-5.0)：1, be preferably (1-4)：1, hydrogen oil volume
Than for 100-1000, preferably 300-800；The condition of the catalytic cracking reaction can include：Temperature
For 460-540 DEG C, preferably 480-530 DEG C, pressure be 0.5-5.0 MPas, preferably 1.0-4.0 MPas,
The oil gas residence time is 0.5-15 seconds, and preferably 1.0-10 seconds, agent weight of oil ratio was (5-30)：1, it is excellent
Elect as (6-30):1.The apparent average linear speed that the fluid bed faces oil gas in hydrogen adsorption zone I can be 0.5-8.0
The apparent average linear speed of oil gas can be 10-60 meter per seconds in meter per second, the riser cracking area II；It is excellent
In the case of choosing, the fluid bed faces riser described in the apparent average differential surface speed of oil gas in hydrogen adsorption zone I and split
Change the low 8-52 meter per seconds of apparent average linear speed of oil gas in area II, first catalytic cracking catalyst is in
Fluidized state, is preferably in turbulent fluidization regimes.
According to the present invention, it can be reactor that fluid bed, which faces hydrogen adsorption zone and the division in riser cracking area,
Difference, by introducing cooling medium, can also will face in reactor bottom or top injection cooling medium
Hydrogen is adsorbed and catalytic cracking process is organically combined, so that inferior feedstock oil catalytic hydroprocessing cracking is realized, and
Improve inferior feedstock oil conversion capability.Therefore this method can also include：Cooling medium is sent into the stream
Change bed, which faces in hydrogen adsorption zone I, carries out temperature control；The cooling medium can be selected from cold hydrogen, water, gasoline,
At least one of diesel oil, recycle oil and fused salt；Cooling medium can be directly injected into reactor, or by
Arrangement heat production coil pipe etc. causes catalyst to be exchanged heat with cooling medium in reactor, so as to control fluid bed to face hydrogen
Adsorption zone temperature.
The present invention also provides a kind of system of processing of inferior feedstock oil, wherein, the system of processing includes setting
Have in the fluid bed riser reactor of fluid bed section and lifting pipeline section, the fluid bed section and be formed with fluidisation
Bed, which faces in hydrogen adsorption zone I, the lifting pipeline section, is formed with riser cracking area II；The fluid bed faces hydrogen
Adsorption zone I connects and is in fluid communication with riser cracking area II, and the fluid bed section is provided with hydrogen
Body entrance, inferior raw material oil-in and the first catalytic cracking catalyst entrance, the lifting pipeline section are provided with
Second catalytic cracking catalyst entrance, the outlet of catalytic cracking oil gas and catalytic cracking catalyst outlet, are set
Or it is not provided with Conventional catalytic cracking raw material oil-in.Wherein, the outlet of catalytic cracking oil gas and catalysis
Cracking catalyst outlet can be with identical, can also be different.
According to a kind of embodiment of the present invention, the system of processing can also include fractionating device 8
With absorption stabilizing apparatus 10, the oil gas entrance of the fractionating device 8 can go out with the catalytic cracking oil gas
Mouth is in fluid communication, and the rich gas of the fractionating device 8 exports richness that can be with the absorption stabilizing apparatus 10
Gas entrance is in fluid communication.Existing Conventional catalytic cracking device reaction and fractionating device typically exist
Operated under 0.1-0.25MPa pressure, and absorption stabilizing apparatus need to enter under more than 1.1MPa pressure
OK, thus Conventional catalytic cracking device must be provided with rich gas compressor to from fractionating device rich gas carry out
Pressure-raising is compressed, system of processing of the present invention is operated in the case where facing hydrogen (0.5-5.0MPa) with pressure, accordingly improved
Rich gas enters the pressure of absorption stabilizing apparatus, can save rich gas compressor in conventional FCC process, so that
Reduce plant energy consumption.
According to the regeneration of the present invention, for convenience catalyst, the system of processing can also include regenerator
13, the regenerator 13 can be provided with regenerator catalyst outlet and regenerator catalyst entrance, institute
State regenerator catalyst outlet (outlet can be one, or two or more) can be with
Connected with the first catalytic cracking catalyst entrance and the second catalytic cracking catalyst entrance, it is described again
Raw device catalyst inlet can be with the catalytic cracking catalyst outlet.The temperature one of regenerator regeneration
As be 550~700 DEG C, preferably 600-650 DEG C, the circulation of regeneration catalyzing Cracking catalyst after regeneration makes
With in regenerative process, regeneration gas can be at least one in air, oxygen and oxygen-containing gas
Kind.The heat exchange of regenerated catalyst can be carried out using method well known to those of ordinary skill in the art,
So as to control coke growing amount and finish Contact Temperature.
According to the embodiment of the present invention, the lifting pipeline section can lift tube reaction for upstriker
Device, the fluid bed section can be located at the lower section of lifting pipeline section, and first catalytic cracking catalyst enters
Mouth can be located at the bottom of the fluid bed section, and the second catalytic cracking catalyst entrance can be located at institute
The bottom of lifting pipeline section is stated, the catalytic cracking catalyst outlet can be located at the upper of the lifting pipeline section
Portion；Or, the lifting pipeline section can be downstriker riser reactor, and the fluid bed section can position
In the top of lifting pipeline section, and the first catalytic cracking catalyst entrance can be located at the fluid bed section
Top, the second catalytic cracking catalyst entrance can be located at it is described lifting pipeline section top, it is described
Catalytic cracking catalyst outlet can be located at the bottom of the lifting pipeline section.
In the present invention, the fluid bed that inferior feedstock oil enters reactor faces hydrogen adsorption zone, is faced according to fluid bed
The setting of hydrogen adsorption zone, inferior feedstock oil can also use upper feeding using lower charging；If using
Lower charging, inferior feedstock oil enters fluidized bed from upstriker fluid bed riser reactor bottom and faces hydrogen absorption
Area, as hydrogen-containing gas flows from bottom to top；If inferior feedstock oil uses upper feeding, inferior feedstock oil
Enter fluidized bed at the top of the downstriker fluid bed riser reactor and face hydrogen adsorption zone, inferior feedstock oil with
Hydrogen-containing gas flows from top to bottom；Inferior feedstock oil enters fluidized bed and faces hydrogen adsorption zone, in the case where facing hydrogen atmosphere,
The first adsorbing and removing wherein alkali nitride on the first catalytic cracking catalyst with nitride adsorption function
The impurity such as thing.
According to the present invention, fluid bed section and lifting pipeline section are well-known to those skilled in the art, fluid beds
Face hydrogen adsorption zone, reaction temperature is relatively low, maintain certain catalyst inventory, the apparent average linear speed of oil gas is general
For 0.5-8.0 meter per seconds, the oil gas apparent linear velocity in riser cracking area is generally 10-60 meter per seconds.The stream
The diameter that change bed faces hydrogen adsorption zone I can be 0.5-5 times of riser cracking area II diameter, be preferably
1-4 times, more preferably 1.0-2.0 times, the length that the fluid bed faces hydrogen adsorption zone I can be riser
The 1-30% of zone of cracking II length, preferably 10-25%, more preferably 10-20%.The fluid bed
Face hydrogen adsorption zone and riser cracking area refers to carry out facing hydrogen adsorption reaction in reactor and catalysis is split
Change the space of reaction, not including reactor in itself.If the reactor is in riser cracking area end
It is expanding, the conversion of inferior feedstock oil crackate sulfide in petrol and alkene can be strengthened.Catalytic cracking
Reaction terminates, can be according to terminating reaction the need for, riser top or exit injection cooling medium
As terminator, cooling medium can be water, gasoline or diesel oil etc..
It is different therefore described with the temperature of catalytic cracking reaction due to facing hydrogen adsorption reaction according to the present invention
Regenerator catalyst outlet can be connected by heat collector 17 with the first catalytic cracking catalyst entrance,
Make the catalyst after regeneration enter back into the fluid bed after cooling to face in hydrogen adsorption zone.
A kind of embodiment, as Figure 1-3, the fluid bed section are provided with cooling medium entrance,
The cooling medium entrance faces hydrogen adsorption zone I in direct fluid communications or described with being arranged on the fluid bed
The heat collector 17 that fluid bed faces in hydrogen adsorption zone I is in fluid communication.
To further illustrate the present invention by embodiment below, but the present invention not therefore and
It is any way limited.
As shown in figure 1, Fig. 1 is the process flow diagram of the first embodiment of the invention,
It is described to carry using the compound reactor being made up of fluid bed section and lifting pipeline section in the embodiment
Riser section is upstriker riser reactor, and expanding fluid bed faces hydrogen adsorption zone I in riser pars infrasegmentalis,
Inferior feedstock oil, which is fed under being used in fluid bed riser reactor into fluidized bed, faces hydrogen adsorption zone I,
Adsorb after denitrogenation, be above advanced into riser cracking area II and carry out catalytic cracking reaction.Its technological process is as follows：
Inferior feedstock oil uses the fluid bed riser reactor elder generation being made up of fluid bed section and lifting pipeline section
Denitrogenation catalytic cracking again is adsorbed, reactor lower part is expanding to face hydrogen adsorption zone I for fluid bed, passes through pipeline 20
The first catalytic cracking catalyst introduced after being cooled down after regeneration through external warmer 17；Inferior feedstock oil 3
Enter fluidized bed from the expanding bottom of reactor 2 and face hydrogen adsorption zone I, with hydrogeneous pre-lift medium 1
It is up together with hydrogen-containing gas 4, reaction adsorbing and removing wherein alkali is carried out on the first catalytic cracking catalyst
The impurity such as property nitride, sulfide, colloid and/or heavy metal；Face hydrogen adsorbed product therewith on be advanced into it is anti-
The riser cracking area II of device 2 is answered, with second through high temperature high activity of the pipeline 21 from regenerator 13
Catalytic cracking catalyst carries out contact and occurs catalytic cracking reaction；The oil gas of generation and catalyst (part the
One catalytic cracking catalyst and the second catalytic cracking catalyst) enter the progress sedimentation separation of settler 6, point
Oil gas from after obtains diesel oil 27, slurry oil 28 into fractionating device 8, fractionating device tower top rich gas without
Rich gas compressor compression is directly entered absorption stabilizing apparatus 10 and further carries out product separation, obtains dry gas
11st, the product such as liquefied gas 25 and gasoline 26, the selected section as needed of dry gas 11 is recycled back to fluid bed
Face hydrogen adsorption zone as hydrogen-containing gas or pre-lift medium, the selection freshening or not as needed of slurry oil 28
Freshening；After catalyst after separation strips the oil gas for removing absorption through stripped vapor 5, regenerator 13 is sent into
Regenerated in regeneration gas (air) 14,600-680 DEG C of regeneration temperature, the regenerative agent after regeneration
Recycle.
As shown in Fig. 2 Fig. 2 is the process flow diagram of second of embodiment of the invention,
In the embodiment, Conventional catalytic cracking feedstock oil mixes refining inferior feedstock oil, its technological process and tool
The process flow diagram of body embodiment one is essentially identical, and simply to increase one newly normal for the embodiment
Feedstock oil and its atomizing medium are advised respectively through pipeline 23,24 injecting lift pipe zone of cracking II, particular location
Enter the top of the regeneration pipeline 21 of fluidized bed riser reactor for the second catalytic cracking catalyst, with
Inferior feedstock oil mixes refining together.In this specific embodiment, the fluid bed faces oily in hydrogen adsorption zone I
In riser cracking area II described in the apparent average differential surface speed of gas the apparent average linear speed of oil gas it is low 8-25 meters/
Second, maintain fluid bed to face hydrogen adsorption zone for turbulent fluidization regimes.
As shown in figure 3, Fig. 3 is the process flow diagram of the third embodiment of the invention, in the tool
In body embodiment, the reactor is downstriker fluid bed riser reactor, and expanding fluid bed faces
Hydrogen adsorption zone I is used in the top of the riser adsorption zone II, inferior feedstock oil in the reactor
Upper feeding enters fluidized bed and faces hydrogen adsorption zone I, the catalytic cracking again after denitrogenation is adsorbed under facing hydrogen atmosphere, under
It is advanced into riser cracking area II and carries out catalytic cracking reaction.In addition, different from the first embodiment
The heat collector outside reactor is arranged on, heat collector is arranged in fluid bed section in this embodiment.
Its technological process is as follows：
Inferior feedstock oil is first adsorbed denitrogenation and be catalyzed again using the downstriker fluid bed riser reactor 2 to be split
Change, the top of reactor 2 is expanding to face hydrogen adsorption zone I for fluid bed；Inferior feedstock oil 3 and hydrogen
Body 4 uses upper feeding, and inferior feedstock oil 3 enters fluidized bed from the expanding top of reactor 2 and faces hydrogen absorption
Area I, as hydrogen-containing gas flows downward, is carried out on the first catalytic cracking catalyst from pipeline 20
The adsorbing and removing wherein impurity such as basic nitrogen compound, sulfide, colloid and/or heavy metal is reacted, and use takes
Hot device 17 carries out taking thermal control temperature；Face hydrogen adsorbed product and be advanced into carrying for the reactor 2 down therewith
The riser zone of cracking II, the second catalytic cracking with the high temperature high activity of the pipeline 21 from regenerator 13 is urged
Agent carries out contact and occurs catalytic cracking reaction；The oil gas of generation is sunk with catalyst into settler 6
Drop separation, the oil gas after separation obtains diesel oil 27, slurry oil 28 into fractionating device 8, and fractionation tower top is rich
Gas is directly entered absorption stabilizing apparatus 10 without rich gas compressor compression and further carries out product separation, obtains
To 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
Fluid bed faces hydrogen adsorption zone I as hydrogen-containing gas or pre-lift medium, and slurry oil 28 is selected as needed
Freshening or not freshening；After catalyst after separation strips the oil gas for removing absorption through stripped vapor 5, feeding
Regenerator 13 is regenerated in regeneration gas (air) 14,600-680 DEG C of regeneration temperature, regeneration
Regenerant recycle afterwards is used.
The present invention will be further illustrated by embodiment below, but therefore the present invention is not taken office
What is limited.
The product inspection method of embodiment and comparative example is：Reaction product is by N2The liquid for bringing -10 DEG C into receives bottle
Middle carry out gas-liquid separation, gaseous product, which is collected, to be completed to be existed by Agilent 6890GC (TCD detectors)
Line analysis is constituted；Weighed off line after liquid product collection, carries out simulation distillation and gasoline detailed hydrocarbon point respectively
Analyse (being tested using RIPP81-90 test methods), the cut cut point of gasoline and diesel oil is respectively
221 DEG C and 343 DEG C；Green coke catalyst carries out coke after drawing off on the carbon and sulfur analytical instruments of multi EA 2000
Analyze (being tested using RIPP106-90 test methods), all product qualities add and calculated material to put down
Weighing apparatus, faces hydrogen adsorbed product and sulfur in gasoline nitrogen content uses RIPP 62-90 test methods and RIPP 63-90
Test method is measured, and tenor is measured using RIPP 124-90 test methods.
Inferior feedstock oil used is shale oil (A), residual oil (B) and decompression in embodiment and comparative example
Wax oil C, its property is as shown in table 1.
The first catalytic cracking catalyst used is identical with the second catalytic cracking catalyst in embodiment, and it is made
Preparation Method is summarized as follows：
1), by 20gNH4Cl is dissolved in 1000g water, 100g (butt) is added into this solution brilliant
Change product DASY zeolites (Qilu Petrochemical Company's catalyst plant production, unit cell dimension is 2.445-2.448nm,
Content of rare earth is (with RE2O3Meter)=2.0 heavy %), after 90 DEG C exchange 0.5h, filter to obtain filter cake；
By 4.0gH3PO4(concentration 85%) and 5.4gCo (NO3)2·6H2O is dissolved in 90g water, mixed with filter cake
Close and dried after dipping, the macropore for then obtaining phosphorous and cobalt for 2 hours in 550 DEG C of roasting temperatures processing boils
Stone, chemical element, which is constituted, is：0.1Na2O·5.1Al2O3·2.4P2O5·1.5Co2O3·3.8RE2O3·88.1SiO2。
2), with 250Kg decationized Y sieves water, by 75.4Kg halloysites, (industry of Suzhou china clay company is produced
Product, solid content 71.6m%) mashing, add 54.8Kg boehmites (Shandong Aluminum Plant's industrial products,
Solid content 63m%), its PH is adjusted to 2-4 with hydrochloric acid, stirred, is stood at 60-70 DEG C old
Change 1 hour, holding PH is 2-4, cool the temperature to less than 60 DEG C, add 41.5Kg Alumina gels (neat
Shandong petro-chemical corporation catalyst plant product, Al2O3Content is 21.7m%), stir 40 minutes, mixed
Close slurries.
By step 1) large pore zeolite (butt is 33.8Kg) of phosphorous and cobalt for preparing and MFI structure
Mesopore ZRP-1 zeolites (Qilu Petrochemical Company's catalyst plant industrial products, SiO2/Al2O3=30, butt is
3.0Kg) it is added to step 2) in obtained mixed serum, stir, and add appropriate extraordinary bonding
It is put in after agent, structural promoter and pore creating material, mixing in bonder, adds suitable quantity of water, stir,
In atmosphere place 4 hours, spray drying forming, in drying box 120 DEG C drying 3 hours after, use
Ammonium dihydrogen phosphate (phosphorus content is 1m%) is washed, and washes away free Na+, the free Na of washing removing+,
Catalyst is drying to obtain again is designated as CAT-3.The composition of the catalyst is 4.1 heavy %MFI structure mesoporous
Phosphorous and cobalt the DASY zeolites of zeolite, 20.6 weight %, 29.4 weight % boehmites, 5.5 heavy % aluminium
Colloidal sol and balance kaolin.Its property is listed in table 2.
Embodiment 1
The embodiment is tested according to Fig. 1 flow, shale oil A as catalytic cracking raw material,
Tested, fed under shale oil A, reactor bottom on small-sized cyclic regeneration fluid bed riser reactor
Expanding 5 times for the riser cracking area II internal diameters in portion turn into fluid bed and face hydrogen adsorption zone I, face hydrogen
Adsorption zone I length is the 14% of riser cracking area II length.Adsorption zone I introduces the cold of outside heat removing
Regeneration catalyzing cracking agent is as the first catalytic cracking catalyst, with dry gas (its of hydrogen volume fraction 85%
Remaining is methane, ethane and ethene etc.) flowed 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；Using CAT-3 catalyst simultaneously
As the first catalytic cracking catalyst and the second catalytic cracking catalyst, micro- reaction of CAT-3 poising agents is lived
Property (MAT) be 65.Shale oil is through the expanding suction of 260 DEG C of laggard fluidized bed riser reactors of preheating
Attached area I bottoms, under reaction pressure 4.2MPa, H2The volume ratio of/shale oil is 500, with hydrogeneous
Gas flows from bottom to top, in 300 DEG C of adsorption temp, the first catalytic cracking catalyst and shale oil A
Weight is to carry out facing hydrogen adsorption reaction under the conditions of 12 seconds than 4.8, adsorption time, removing basic nitrogen compound,
The impurity such as sulfide and heavy metal；Face hydrogen adsorbed product therewith on be advanced into riser cracking area,
500 DEG C, the second catalytic cracking catalyst and face the weight of hydrogen adsorbed product than 3.5 seconds 6.4, reaction time
Under the conditions of catalytic cracking reaction occurs together；The oil gas of generation obtains diesel oil, slurry oil into fractionating device,
Fractionating device tower top rich gas is directly entered absorption stabilizing apparatus without rich gas compressor compression and further carried out
Product is separated, and obtains the products such as dry gas, liquefied gas and gasoline, and slurry oil recycle ratio is 0.1.Reaction is certain
After time, catalytic cracking catalyst to be generated is through N2After the oil gas of its internal absorption of stripping removing, feeding is again
Raw device uses air as regeneration gas, is catalyzed at 600~680 DEG C of regeneration temperature with catalytic cracking to be generated
Agent contact is regenerated；Regenerant recycle after regeneration is used.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, it adsorbs desulfurization degree 82
Weight %, the heavy % of denitrification percent 87, the heavy % of demetallization per 62.0；Shale oil A, which faces to be catalyzed again after hydrogen absorption, to be split
Change, conversion ratio (100%- diesel yields-slurry oil yield) be 68.1 heavy %, the heavy % of slurry oil yield 5.5,
The heavy % of dry gas yied 2.3, the heavy % of coke yield 7.8, liquid product yield (receive by yield of liquefied gas+gasoline
Rate+diesel yield) 84.4 heavy % are up to, wherein gasoline yield is up to 41.8 heavy %, and productivity of propylene is up to
4.9 heavy %；Product gasoline sulfur content 52.5ppm, nitrogen content 85.2ppm.
Comparative example 1
The comparative example is using shale oil A as raw material, using CAT-3 as the first catalytic cracking catalyst and
Two catalytic cracking catalysts, poising agent MAT is 65, is urged in the small-sized fluidized bed riser of embodiment 1
Change and tested on cracking unit, what it is different from embodiment 1 is：Hydrogen-containing gas is replaced with not hydrogeneous
Vapor, reactor pressure is 0.22MPa, and is not injected into cooling medium, and shale oil A and water vapour
The reaction zone of fluidized-bed reactor, i.e. shale oil A are directly injected into without absorption directly in the second catalytic cracking
Catalytic cracking reaction is carried out on catalyst；After reaction, fractionating device tower top rich gas compresses through rich gas compressor
Pressure-raising into absorption stabilizing apparatus to further carrying out product separation after 1.2-1.6MPa；Heavy oil recycle ratio
0.3.Operating condition and product distribution are listed in table 3.
From table 3 it can be seen that shale oil A directly carries out non-hydrogen catalytic cracking reaction without absorption, turn
The heavy % of rate 66.6, the heavy % of slurry oil yield 6.5, the heavy % of dry gas yied 3.0, the heavy % of coke yield 9.8,
The heavy % of liquid product yield 80.7, the wherein heavy % of gasoline yield 39.3, productivity of propylene is up to 4.4 heavy %；Production
Product content of sulfur in gasoline 291.5ppm, nitrogen content 458.6ppm.
It can be seen that from the data of table 3 and processing shale oil A, shale oil carried out using the method for the present invention
Conversion capability is high, and recycle ratio is low, conversion ratio improves 1.5 percentage points, and slurry oil low yield 1.0
Percentage point, and dry gas and coke yield are low, dry gas+coke yield is low 2.7 percentage points, liquid production
Product yield improves 3.7 percentage points；Product gasoline sulfur content reduces 249.0ppm, nitrogen content reduction
373.4ppm。
Embodiment 2
Embodiment 2 is tested according to Fig. 2 equipment and flow, uses residual oil B in table 1 and decompression wax
Oily C is as the raw material of catalytic cracking, and residual oil B and decompressed wax oil C subregions feed, i.e. residual oil B is in stream
Change bed faces hydrogen adsorption zone I chargings and decompressed wax oil C is fed in riser cracking area II；Reactor bottom stream
It is that turbulent fluidized bed faces hydrogen adsorption zone (fluid bed faces the internal diameter of hydrogen adsorption zone for the riser to change bed expanding
3 times of zone of cracking internal diameter, it is the riser cracking section length that fluid bed, which faces the length of hydrogen adsorption zone,
10%), and introduce outside heat removing cooling the first catalytic cracking catalyst, using volume fraction as 80%
Dry gas (remaining is methane, ethane and ethene etc.) is used as hydrogen-containing gas；Riser cracking area II bottoms are defeated
The catalytic cracking catalyst of high temperature second is sent into, riser cracking area II is formed in lifting pipeline section middle and upper part.Account for
The weight % of combined feed 30 residual oil B enters riser reactor bottom fluidization bed after being preheated through 300 DEG C expanding
Turbulent fluidized bed faces hydrogen adsorption zone I bottom, as hydrogen-containing gas flows from bottom to top, in adsorption temp
350 DEG C, the weight of the first catalyst and residual oil than 3.0, pressure be 3.5MPa, adsorption time is 5.0 seconds
Under the conditions of carry out facing hydrogen adsorption reaction, the impurity such as removing basic nitrogen compound, sulfide and heavy metal is described
The apparent average linear speed that fluid bed faces oil gas in hydrogen adsorption zone I is 0.5 meter per second；Residual oil is urged with part first
Fluidized cracking catalysts therewith on be advanced into riser cracking area II, be catalyzed with the high temperature from regenerator second
After Cracking catalyst mixing, with charging, the decompressed wax oil C through 210 DEG C of preheatings at this in 510 DEG C, oil
Qi leel pressure is 0.22MPa, and the gross weight of the second catalytic cracking catalyst is with facing hydrogen adsorbed product and decompressed wax oil
The ratio between C gross weights are 6.0, catalytic cracking reaction occurs together under the conditions of 2.5 seconds reaction time, described to carry
The apparent average linear speed of oil gas is 22 meter per seconds (fast bed fluidized state) in the II of the riser zone of cracking；Generation
Oil gas enters fractionating device fractionation and obtains diesel oil, slurry oil, and fractionating device tower top rich gas is without rich gas compressor
Compression is directly entered absorption stabilizing apparatus and further carries out product separation, obtains dry gas, liquefied gas and gasoline
Deng product, heavy oil recycle ratio 0.1.React after certain time, catalytic cracking catalyst stripping removing to be generated
After oil gas of its internal absorption, feeding regenerator uses air as regeneration gas, regeneration temperature 600~
Contact and regenerated with catalytic cracking catalyst to be generated at 680 DEG C；Regenerant recycle after regeneration is used.
Operating condition and product distribution are listed in table 4.
From table 4, it can be seen that in embodiment 2, the charging catalysis of residual oil B and decompressed wax oil C subregions is split
Change, residual oil absorption desulfurization degree is 72 heavy %, denitrification percent is 70 heavy %, the heavy % of demetallization per 45.0；Its
Slurry oil yield is 5.0 heavy %, and dry gas yied is 2.3 heavy %, and coke yield is 8.5%, and fluid product is received
Rate (yield of liquefied gas+yield of gasoline+diesel yield) is up to 84.2 heavy %, and wherein gasoline yield is up to
39.5 heavy %, 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：It will contain
Hydrogen replaces with not hydrogeneous vapor, and reactor pressure is 0.22MPa, and is not injected into cooling medium,
And residual oil B mixes the riser for being directly injected into fluid bed riser reactor with vapor with wax oil C and split
Change area, i.e. residual oil B and catalytic cracking reaction is directly carried out on the second catalytic cracking catalyst without absorption；
After reaction, fractionating device tower top rich gas enters after rich gas compressor compression pressure-raising to 1.2~1.6MPa to be inhaled
Receive stabilising arrangement and further carry out product separation；Heavy oil recycle ratio 0.2.Operating condition and product Distribution of A Sequence
In table 4.
From table 4, it can be seen that in comparative example 2, residual oil B is mixed directly with decompressed wax oil C without absorption
Close charging and carry out catalytic cracking reaction, its slurry oil yield is 6.5 heavy %, and dry gas yied is 3.4 heavy %, burnt
Charcoal yield is 9.3%, and liquid product yield (yield of liquefied gas+yield of gasoline+diesel yield) is 80.8,
Wherein gasoline yield is 36.1 heavy %, and productivity of propylene is 5.0 heavy %；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 carried out using the method for the present invention,
Conversion capability is high, heavy oil recycle ratio is low, and 1.5 percentage points of slurry oil low yield, and dry gas and coke
Low yield, dry gas+coke yield is low 1.9 percentage points, and liquid product yield improves 3.4 percentages
Point；Product gasoline sulfur content reduces 253.4ppm, nitrogen content reduction 23.5ppm.
Embodiment 3
The embodiment is tested according to Fig. 3 flow, residual oil B as catalytic cracking raw material, small
Tested on the downflow fluidized bed riser reactor of type cyclic regeneration, residual oil B upper feedings, reactor top
Portion is expanding to face hydrogen adsorption zone for fluid bed, and fluid bed faces hydrogen adsorption zone I a diameter of riser cracking area II
4.2 times of diameter, the length that the length that the fluid bed faces hydrogen adsorption zone I is riser cracking area II
30% and it is built-in in heat production coil pipe cool down the first catalytic cracking catalyst, lifting pipeline section is conveyed into high temperature the
Two catalytic cracking catalysts；Using CAT-3 catalyst, poising agent MAT=63.Residual oil is pre- through 350 DEG C
Enter after heat at the top of the expanding fluidised bed adsorption reaction zone I of reactor, as hydrogen-containing gas flows from top to bottom
It is dynamic, under reaction pressure 1.8MPa, with hydrogenation tail gas and the part dry gas of hydrogen volume fraction 70%
Mixed gas flowed from top to bottom as hydrogen-containing gas, H2The volume ratio of/feedstock oil is 300, in absorption
The weight of 420 DEG C of temperature, the first catalytic cracking catalyst and residual oil is 8 seconds conditions than 4.9, adsorption time
Lower carry out adsorption reaction, removes the impurity such as basic nitrogen compound, sulfide and heavy metal；Residual oil is descending therewith
Into downstriker riser cracking area II, 505 DEG C, the weight of catalyst and absorption denitrogenation product than 15,
Catalytic cracking reaction occurs together under the conditions of 1.5 seconds reaction time；The oil gas of generation is obtained into fractionating device
To diesel oil, slurry oil, fractionating device tower top rich gas is directly entered Vapor recovery unit without rich gas compressor compression and filled
Put and further carry out product separation, obtain dry gas, liquefied gas, gasoline etc., dry gas is partly followed as needed
Loopback fluid bed faces hydrogen adsorption zone I as hydrogen-containing gas.React after certain time, catalytic cracking to be generated is urged
After the oil gas of its internal absorption of agent stripping removing, regeneration gas is used air as, in regeneration temperature
Contact and regenerated with catalytic cracking catalyst to be generated at 600~700 DEG C；Regeneration catalyzing cracking after regeneration
Agent is recycled.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 it adsorbs desulfurization
The heavy % of rate 76, the heavy % of denitrification percent 85, the heavy % of demetallization per 58.0；It is catalyzed and splits again after residual oil B absorption
Change, the heavy % of conversion ratio 67.4, the heavy % of slurry oil yield 6.0, the heavy % of dry gas yied 3.3, coke yield 10.2
Weight %, liquid product yield is up to 80.5 heavy %, and wherein gasoline yield is up to 39.4 heavy %, productivity of propylene
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, using CAT-3 as catalyst, and poising agent MAT is 63,
Tested on the small-sized downflow fluidized bed riser fluid catalytic cracking of embodiment 3, different from implementing
Example 3 is：Hydrogen-containing gas is replaced with to not hydrogeneous vapor, reactor pressure is 0.14MPa, and
Cooling medium is not injected into, and residual oil B is directly injected into the riser cracking of fluidized-bed reactor with water vapour
Area, i.e. residual oil B are gone downstream with catalyst, and residual oil is directly urged without absorption under non-hydrogen atmosphere
Change cracking reaction；After reaction, fractionating device tower top rich gas compresses pressure-raising extremely through rich gas compressor
After 1.2-1.6MPa product separation is further carried out into absorption stabilizing apparatus；Heavy oil recycle ratio 0.2.Behaviour
Make condition and product distribution is listed in table 5.
As can be seen from Table 5, residual oil B directly carries out Catalytic Cracking Unit of Measure without absorption under non-hydrogen atmosphere
Should, its conversion ratio 66.9 heavy %, the heavy % of slurry oil yield 7.5, the heavy % of dry gas yied 4.0, coke yield
11.0 heavy %, the heavy % of liquid product yield 77.5, the wherein heavy % of gasoline yield 38.1, productivity of propylene is up to 4.1
Weight %；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, crude conversion carried out using the method for the present invention
Ability is high, and recycle ratio is low, conversion ratio improves 0.5 percentage point, and 1.5 percentages of slurry oil low yield
Point, and dry gas and coke yield are low, dry gas+coke yield is low 1.5 percentage points, and fluid product is received
Rate improves 3.0 percentage points；Product gasoline sulfur content reduces 305.1ppm, nitrogen content reduction
75.5ppm。
The property of inferior feedstock oil used in the embodiment of the present invention of table 1 and comparative example
| Inferior feedstock oil title | Shale oil | Residual oil | Decompressed wax oil |
| Numbering | 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 is constituted | |||
| 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 the embodiment of the present invention of table 2 and comparative example
| Catalyst is numbered | CAT-3 |
| Zeolite type | Mesopore and large pore zeolite |
| Chemical composition, weight % | |
| Silica | 52.7 |
| Aluminum 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, during weight %-1 | 1.5 |
| Screening composition, weight % | |
| 0~40 micron | 20.5 |
| 40~80 microns | 55.2 |
| >80 microns | 24.3 |
Table 3 is operating condition and the 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 | Fluid bed faces the charging of hydrogen adsorption zone | Riser cracking area is fed |
| 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 |
| Fluid 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 | / |
| The weight ratio of catalyst/shale oil | 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 |
| The weight ratio of catalyst/shale oil | 6.4 | 6.4 |
| Oil gas residence time, s | 3.5 | 3.5 |
| The weight ratio of vapor/total raw material | 0.5 | 0.5 |
| Product is distributed, 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 operating condition and the 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 is fed | 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 |
| Fluid bed faces hydrogen adsorption zone operating condition | ||
| Raw material preheating temperature, DEG C | 300 | 210 |
| H2/ residual oil B volume ratio | 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 |
| The weight ratio of vapor/total raw material | 0.5 | 0.5 |
| Product is distributed, 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 operating condition and the 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 includes：
A, the fluid bed that hydrogen-containing gas and inferior feedstock oil are sent into fluid bed riser reactor face hydrogen and inhaled
Contacted in attached area (I) with the first catalytic cracking catalyst and carry out facing hydrogen adsorption reaction, obtain facing hydrogen suction
Accessory substance；
B, gained in step a faced into the lifting that hydrogen adsorbed product sends into the fluid bed riser reactor
Contacted in the pipe zone of cracking (II) with the second catalytic cracking catalyst and carry out catalytic cracking reaction, urged
Change cracking oil gas.
2. processing method according to claim 1, this method also includes：By gained in step b
Cycle oil pneumatic transmission enters fractionating device (8) and carries out fractionation processing, obtains including the catalytic cracking of rich gas
Product；Gained rich gas is sent directly into absorption stabilizing apparatus (10) without rich gas compressor to be absorbed
Stable processing.
3. processing method according to claim 1, this method also includes：In stepb, will
Conventional catalytic cracking feedstock oil with it is described face hydrogen adsorbed product together with carry out the catalytic cracking reaction；Its
In, the Conventional catalytic cracking feedstock oil is at least one in wax oil, reduced crude and decompressed wax oil
Kind.
4. processing method according to claim 1, wherein, the hydrogen-containing gas include hydrogen and/
Or dry gas, the inferior feedstock oil is selected from shale oil, liquefied coal coil, tar sand oil, wax tailings, slag
At least one of oil, hydrogenated residue and deasphalted oil.
5. processing method according to claim 1, wherein, first catalytic cracking catalyst
It is identical with the composition of the second catalytic cracking catalyst, zeolite, 5-99 weight % including 1-50 weight %
Inorganic oxide and 0-70 weight % clay.
6. processing method according to claim 5, wherein, the zeolite include mesopore zeolite and/
Or large pore zeolite, the mesopore zeolite is selected from ZSM-5 zeolite, ZSM-11 zeolites, ZSM-12 boilings
Stone, ZSM-23 zeolites, ZSM-35 zeolites, ZSM-38 zeolites, ZSM-48 zeolites and ZRP zeolites
At least one of, the large pore zeolite is selected from rare earth Y type zeolite, rare earth hydrogen Y zeolites, high silicon Y
At least one of type zeolite and ultrastable；The inorganic oxide is silica and/or oxidation
Aluminium；The clay be selected from silica, kaolin, halloysite, montmorillonite, diatomite, angstrom
At least one of Lip river stone, saponite, rectorite, sepiolite, attapulgite, hydrotalcite and bentonite.
7. processing method according to claim 1, wherein, first catalytic cracking catalyst
For the fresh catalyst Cracking catalyst of supplement, the regeneration catalyzing Cracking catalyst of cooling, the semi regeneration cooled down
At least one of catalytic cracking catalyst and the catalytic cracking catalyst to be generated of cooling, second catalysis
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.
8. processing method according to claim 1, wherein, the condition for facing hydrogen adsorption reaction
Including：Temperature is 200-450 DEG C, and pressure is 0.5-5.0 MPas, and adsorption time is 1-90 seconds, agent oil weight
Amount is than being (0.5-5)：1, hydrogen to oil volume ratio is 100-1000；The condition of the catalytic cracking reaction includes：
Temperature is 460-540 DEG C, and pressure is 0.5-5.0 MPas, and the oil gas residence time is -15 seconds 0.5 second, agent oil
Weight ratio is (5-30)：1.
9. processing method according to claim 1, this method also includes：Cooling medium is sent into
The fluid bed, which faces, carries out temperature control in hydrogen adsorption zone (I)；The cooling medium be selected from cold hydrogen, water,
At least one of gasoline, diesel oil, recycle oil and fused salt.
10. a kind of system of processing of inferior feedstock oil, it is characterised in that the system of processing includes being provided with
Fluid bed is formed with the fluid bed riser reactor of fluid bed section and lifting pipeline section, the fluid bed section
Face in hydrogen adsorption zone (I), the lifting pipeline section and be formed with riser cracking area (II)；
The fluid bed faces hydrogen adsorption zone (I) and connects and be in fluid communication with riser cracking area (II),
The fluid bed section is provided with hydrogen-containing gas entrance, inferior raw material oil-in and the first catalytic cracking catalyst
Entrance, the lifting pipeline section be provided with the second catalytic cracking catalyst entrance, catalytic cracking oil gas outlet and
Catalytic cracking catalyst is exported, and sets or be not provided with Conventional catalytic cracking raw material oil-in.
11. system of processing according to claim 10, wherein, the system of processing also includes dividing
Distillation unit (8) and absorption stabilizing apparatus (10), the oil gas entrance of the fractionating device (8) with it is described
Catalytic cracking oil gas communication, the rich gas outlet of the fractionating device (8) absorbs steady with described
The rich gas entrance for determining device (10) is in fluid communication.
12. system of processing according to claim 10, wherein, the system of processing also includes again
Raw device (13), the regenerator (13) is provided with regenerator catalyst outlet and regenerator catalyst enters
Mouthful, the regenerator catalyst outlet is split with the first catalytic cracking catalyst entrance and the second catalysis
Change catalyst inlet connection, the regenerator catalyst entrance is exported with the catalytic cracking catalyst to be connected
It is logical.
13. system of processing according to claim 12, wherein, the regenerator catalyst outlet
Connected by heat collector (17) with the first catalytic cracking catalyst entrance.
14. system of processing according to claim 10, wherein, the lifting pipeline section is upstriker
Riser reactor, the fluid bed section is located at the lower section of lifting pipeline section, and first catalytic cracking is urged
Agent entrance is located at the bottom of the fluid bed section, and the second catalytic cracking catalyst entrance is located at described
The bottom of pipeline section is lifted, the catalytic cracking catalyst outlet is located at the top of the lifting pipeline section；
Or, the lifting pipeline section is downstriker riser reactor, and the fluid bed section is located at riser
The top of section, and the first catalytic cracking catalyst entrance is located at the top of the fluid bed section, it is described
Second catalytic cracking catalyst entrance is located at the top of the lifting pipeline section, and the catalytic cracking catalyst goes out
Mouth is located at the bottom of the lifting pipeline section.
15. system of processing according to claim 10, wherein, the fluid bed faces hydrogen adsorption zone
(I) 0.5-5 times of the diameter of a diameter of riser cracking area (II), the fluid bed faces hydrogen absorption
The length in area (I) is the 1-30% of the length of riser cracking area (II).
16. system of processing according to claim 10, wherein, the fluid bed section is provided with cold
But medium inlet, the cooling medium entrance faces hydrogen adsorption zone (I) directly fluid with the fluid bed and connected
Heat collector (17) that is logical or facing with being arranged on the fluid bed in hydrogen adsorption zone (I) is in fluid communication.
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