TW201024400A - A combination process for improved hydrotreating and catalytic cracking of hydrocarbon oils - Google Patents

Abstract

Disclosed is a combination process for improved hydrotreating and catalytic cracking of hydrocarbon oils, including: contacting residual oil, catalytic cracking cycle oil, and optional distillate oil with a hydrotreating catalyst under hydrotreating conditions in the presence of hydrogen followed by separation of the reaction products to obtain gas, hydrogenated naphtha, hydrogenated diesel oil, and hydrogenated tail oil; contacting the hydrogenated tail oil and optional normal catalytic cracking feedstock oil with a cracking catalyst under catalytic cracking conditions followed by separation of the reaction products to obtain dry gas, hydrogenated naphtha, liquefied petroleum gas, catalytic cracked gasoline, catalytic cracked diesel oil, and catalytic cracking cycle oil; wherein the hydrogenated tail oil and/or normal catalytic cracking feedstock oil are separated into at least two fractions, the light and the heavy fractions or normal catalytic cracking heavy feedstock oil and normal catalytic cracking light feedstock oil, prior to contacting the hydrogenated tail oil and/or normal catalytic cracking feedstock oil with the cracking catalyst. The process according to the present invention is especially suitable for conversion of hydrocarbon oils to produce more products of gasoline or diesel oil.

Description

201024400 VI. INSTRUCTIONS: The invention belongs to the invention. The invention relates to a method for converting tobacco oil by a combination process of a hydrogenation treatment process and a catalytic cracking process. Previous technologies have witnessed the world's tendency to become heavier and worse, and the demand for heavy fuel oil has gradually decreased, and the demand for light oil has increased significantly. Therefore, refining companies are pursuing the largest conversion of residual oil into gasoline, diesel and liquefied petroleum gas. Hydrogenation treatment can reduce the content of impurities such as sulfur, nitrogen, metals and residual carbon in inferior, heavy oil or residual oil, and achieve the raw material requirements for normal processing of catalytic cracking equipment. It is an effective method to achieve the above objectives. US 4,713,221 discloses the recycling of catalytic cracking (including ant oil catalytic cracking and heavy oil catalysis cleavage) & heavy cycle oil (HCO) to a oil sinter hydrogenation unit on the basis of conventional residue hydrogenation and catalytic cracking σ. After being mixed with the residue and hydrogenated, it is added to a catalytic cracking unit (mainly a wax oil catalytic cracking unit) for processing. This technical improvement has resulted in a large variation in product distribution in the catalytic cracking unit's own rework mode of operation, as compared to conventional residuary hydrogenation to provide feedstock for the catalytic cracking unit. From the example given in the patent, 'when the main operating parameters are basically similar, after the new combined processing technology, the total conversion rate of the catalytic cracking unit is increased by 3 volume percent, and the mass yield of liquefied petroleum gas is increased by 25.7%. The gasoline mass yield increased by 1.07%, the diesel mass yield decreased by 3.97%, the heavy cycle oil quality 4 201024400 yield decreased by 15.61%, and the coke quality yield decreased by 5.56%. CN1382776 discloses a combined method of residue hydrotreating and heavy oil catalytic cracking. The patented method proposes mixing the heavy cycle oil produced by the catalytic cracking device and the clarified oil in the slurry together as part of the feed of the residue device, and the hydrogenation is reformed and then returned to the catalytic cracking process together with other feeds. Increase the yield of gasoline and diesel in catalytic crackers.

❹ CN1422327A discloses a method for increasing the production of small molecule olefins and gasoline by subjecting Hc oxime produced by a catalytic cracking unit to hydrogenation treatment or after mixing with naphtha and then performing external independent catalytic cracking. This method proposes that the re-cracking of the circulating oil in the external second riser catalytic cracking reactor can inhibit the undesired hydrogen transfer reaction that occurs when a single riser reactor is reacted with other feeds. This is advantageous for further improving the yield of light olefins. China Patent CN1423689A also proposes on the basis of the above patents that the use of a ZSM_5 structured sieve catalytic cracking catalyst in an externally independent second catalytic cracking reactor can further increase the yield of light olefins. China Special 2 CN1425055A is based on the Chinese patent CN1422327A, using different hydrogenation catalyst combinations in the hydrotreating reactor and using a combination of different unit cell size molecular sieve catalytic cracking catalysts in the external = independent second catalytic cracking reactor. A method of light olefin yield. CN1262306A discloses a residue hydrotreating-catalytic cracking combined process, which comprises introducing a residue and a clarified oil into a residue hydrotreating device, performing a hydrogenation reaction in the presence of hydrogen and a hydrogenation catalyst; and the hydrogenated residue obtained by the reaction enters the catalytic process. The cracking device performs a cracking reaction in the presence of a cracking catalyst, and the heavy cycle oil is circulated inside the catalytic cracking device; the oil slurry of the reaction 201024400 is separated by a separator, and returned to the hydrogenation device. By re-circulating the catalytic cracking product heavy oil (including heavy cycle oil, clarified oil or ψΓην^ 慝 into the catalytic cracking unit, it can further improve the vehicle ^ ^ ^ σ early use of several oils 'diesel and liquefied petroleum = production The yield of ° °. However, the existing methods generally have the problem that the distribution of the product and the selectivity of the gasoline or diesel in the product distribution are poor. The invention solves the technical problem that the product distribution in the prior art is adjustable. Disadvantages of poor selectivity of gasoline or diesel in product distribution and product providing an improved combination of hydrotreating and catalytic cracking of hydrocarbon oils. The present invention provides an improved combination of hydrotreating and catalytic cracking of hydrocarbon oils, including: in the presence of hydrogen And reacting the residue, the catalytic cracking back to the refinery oil and the optional distillate oil together with the hydrotreating catalyst crucible under hydrotreating reaction conditions, separating the reaction product to obtain a gas, hydrogenated naphtha, hydrogenated diesel oil and hydrogenated tail oil; Hydrogenation tail oil and/or conventional catalytic cracking f feedstock together with catalytic cracking under catalytic cracking conditions The catalyst contacts the reaction, and the reaction product is separated to obtain dry gas, liquefied petroleum gas, catalytic pyrolysis gasoline, catalytic cracking diesel oil, and catalytic cracking back to the refinery; wherein the contact reaction with the catalytic cracking catalyst includes at least two in a flow direction along the reactant. In the reactors of reaction zones I and π, 6 201024400, before the weathering tail oil and / / he is used to contact the catalytic catalyst The step of distilling the tailing oil and/or the conventional catalytic cracking feedstock oil into at least two light portions and weighing the two crane portions, wherein the (4) cracking catalyst contact reaction is to lightly crush the hydrogenated tail oil and the hydrogenated tail oil heavy fraction. An optional oil, private gas, ground and uncut hydrogenated tail sling gauge catalytic cracking feedstock oil and / or conventional catalytic cracking heavy feedstock oil, often light feedstock oil is added to reaction zone 1, and the hydrogenation is carried out Tail oil 10 ginseng sulphate and hydrogenated tail oil heavyweights - J force species optionally with uncut, oil, conventional catalytic cracking feedstock oil and / or conventional catalytic cracking heavy feedstock oil, conventional catalytic cracking Light feedstock oil is added to the reaction zone π, or the feedstock is mixed with the pure feedstock (4). (4) Conventional urging, one of the heavy feedstock oil and the conventional catalytic cracking light feedstock oil is optionally combined with uncut (tetra) hydrogenated tail oil, conventional catalysis. Pyrolysis feedstock oil and/or hydrogenation tail oil light (iv) 'chlorinated tail oil weight (four) is added to reaction zone 1' and another of the conventional catalytic cracking heavy feedstock oil and conventional catalytic cracking light feedstock oil is optionally combined with The cut hydrogenated tail oil, the conventional catalytic cracking feedstock oil and/or the hydrogenated tail oil Ik cut, the hydrogenated tail oil heavy fraction is added to the reaction zone, and the light and heavy two oils are optionally combined with the hydrogenated tail oil and/or Or in the mixed feed of the hydrogenated tail oil light fraction and the hydrogenated tail oil heavy fraction, the content of the hydrogenated tail oil is not zero at the same time. According to the method provided by the invention, the hydrogenated tail oil refers to the boiling range. Part of the 'hydrogenated diesel' case, the boiling point is higher than the 35th generation of the museum. The ° is preferably such that the light library accounts for 1 〇 _ 8 〇 of the total amount of the hydrogenated tail oil. /. It is preferably from 20 to 70% by weight, more preferably from 30 to 60% by weight. 7 201024400 according to the method provided by the present invention, when the conventional catalytic cracking light feedstock oil is mixed with the hydrogenated tail oil, the content of the hydrogenated tail oil is within 5 〇 wt%, preferably within 40 wt%; When the catalytic cracking heavy feedstock oil is mixed with the hydrogenated tail oil, the content of the hydrogenated tail oil is within 9% by weight, preferably within 80% by weight. The conventional catalytic cracking feedstock oil is well known to those skilled in the art, for example, a reduced pressure wax oil, an atmospheric residue, a vacuum depressurized oil blended partially depressurized > oil or other secondary enhanced hydrocarbons oil. The hydrocarbon oil obtained by the secondary processing is one or more of a coking wax oil, a deasphalted oil, and a furfural refined raffinate oil. The light feedstock oil and heavy feedstock oil may be isolated by (iv) or several prior art techniques. For example, it is separated by a method of atmospheric pressure and/or reduced pressure evaporation. The conventional catalytic cracking heavy feedstock oil is a hydrocarbon oil having a boiling point of more than 50 (TC or more, and the conventional catalytic cracking light feedstock oil is a hydrocarbon oil having a distillation range of 35 〇·5 〇〇. The catalytic cracking back to the refining oil may be off In addition to catalytically cracking catalyst particles of heavy cycle oil, clarified oil or separation of catalytic cracking of the diesel pyrolysis cracking cracking heavy oil in the species or several. The hydrogenation tail oil and / or when the recruitment of several columns. The method for catalyzing the cracking of the raw material oil into two or two can be any method for separating the light and heavy fractions in the prior art. For example, in the dust reduction steaming or the sudden boiling separation, for example, a combination of a species or a combination of several In a preferred embodiment, a preferred method of hydrogen hydride method is used in the method of steaming the sulphuric acid in the method of oxidizing the raw material of the yttrium/yield/y/y. The obtained reheating is the smoky oil with a monument greater than 500t, and the light remainder is a hydrocarbon oil with a museum schedule of 8 201024400 3 5 0 - 5 0 〇 ° C. As a common knowledge well known in the art, when entering a fixed bed hydrogenation reaction Particulate matter of solid impurities contained in the raw material oil When less than 25μΓη, it can pass through the residue of the residue hydrogenation catalyst without forming a pressure drop (improvement of the feed of the residue hydrogenation unit) [Mu Haitao, Sun Zhenguang, Refining Design, Vol. 31, No. 5 '2001) Therefore, the particle size of the particles which normally control the solid impurities contained in the residue during the conventional residue hydrotreating reaction is less than @25μϊη. However, the inventors of the present invention found that when introduced into the feedstock oil of the hydrotreating reactor The situation with catalytic cracking back to the refinery is not exactly the same. Studies have shown that when the feedstock oil introduced into the hydrotreating reactor contains catalytic cracking back to the refinery, the amount of solids in the refinery is catalytically cracked back to the solid particles. The particle size is both stable to the operation of the hydrotreating reactor. Thus, in a preferred embodiment, the heavy cycle oil, the decant oil or the total catalytic cracking cracking product heavy solids in the heavy oil of the catalytic cracking catalyst particles are removed. The content is less than 3〇wtppm, and the particle diameter of the solid particles is less than 10, and the content of the particles is less than 15 wtppm, and the particle size is less than 5 μppm. More preferably, it contains less than 5 wtppm and the particle size is less than 2 μm. The particle size of the particles is determined by a laser scattering particle size analyzer. The particle size of the solid particles is distributed within a certain particle size range, and the particle size described herein. It means that the particle size of 90 〇 / 〇 (volume) of solid particles in the distribution is less than the value. The content of the solid particles is determined by carbonization and burning weighing method, that is, weighing in a quartz cup The weight of the catalytic cracking back to the refinery sample, the sample is in the incinerator at 6 〇〇. The following carbonization (nitrogen protection), then air ashing, and then nitrogen protection cooling, take out the amount of 201024400 residual solid particles 'calculated The difference between the results of the repeatability test of the solid particle content in the catalytic cracking back to the refining oil is not more than 0 02 〇 / 〇. The method for removing solid impurity particles from the catalytic cracking cycle oil may be any method in the prior art that can separate oil from solid particles, for example, the method may be filtration, centrifugation, distillation or ablation separation. One or several combinations. A preferred method of removing catalytic cracking catalyst particles from the catalytic cracking cycle oil in the preferred embodiment is a filtration process. As an example of a filter in the form of solid-liquid separation, the separation can achieve the desired filtration accuracy by selecting the filter pore size of the filter cartridge. Wherein, the filter element may be a metal powder sintered plate, a wire sintered mesh or prepared by any prior art. In order to improve the efficiency of filtration, in a more preferred embodiment, the filtration temperature is 100 to 350 ° C, more preferably 200 to 32 (rc. The residue of the contact reaction with the hydrogenation catalyst is a vacuum residue and/or an atmospheric residue, the distillate oil in contact with the hydrogenation catalyst is one selected from the group consisting of coker gas oil, deasphalted oil, vacuum gas oil or solvent refined oil. According to the method provided by the present invention, there is no limitation on the mixing ratio of the catalytic cracking back to the refining oil and the residual oil in the hydrotreated feedstock oil, and depending on the processing capacity of the reaction device and the source of the raw materials, it is generally preferred to catalytically crack the refining oil into hydrogenation. The apparatus has a total hydrocarbon oil feed amount of 5 to 40% by weight, more preferably 6 to 3 % by weight, and still more preferably 8 to 25% by weight. The apparatus for the amination treatment is a conventional residue hydrotreating reaction apparatus. The deuteration reactor is usually a fixed bed reactor, and may also be a shifting 201024400 moving bed reactor or an ebullated bed reactor. The residue hydrotreating reaction conditions are: hydrogen partial pressure 5 -22 MPa, reaction temperature 330 - 450 ° C, volumetric space velocity 0.1-3 hours -1, hydrogen oil volume ratio 350-2000 Nm3 / m3. The hydrogenation treatment catalyst is a catalyst or catalyst combination conventionally used in the art, for example, the active metal component is selected from the a Group VIB metal and/or a Group VIII non-noble metal, the carrier being selected from one or more of the group consisting of alumina, cerium oxide, amorphous quartz, and aluminum. The metal component is preferably nickel-tungsten, nickel-tungsten. a combination of cobalt, nickel-molybdenum or cobalt-molybdenum. Regarding the residue processing technology and the catalysts used therein are CN1626625A, CN1648215A, CN1400285A, CN1400288A,

The descriptions of .CN12623〇6A, CN1382776A, CN1690172A, and CN1782031A are respectively referred to, and are hereby incorporated by reference. The gas in the residue hydrotreating reaction product can be used as a hydrogen producing raw material or a refinery gas, and the hydrogenated naphtha can be used as a raw material for a catalytic recombination device or a steam cracking ethidium dilute device, and the hydrogenated diesel oil is an ideal diesel product blending component. The hydrogenated tail oil has a range of >35〇t, which can be used as a feed to the catalytic cracker. According to the method provided by the present invention, the catalytic cracking reaction device is an H-domain If the catalytic cracking device described by 'for example' may be heavy oil fluidized pure cracking (RFCC) or may be catalytic (4) ((10), lifting: And a combination of a helium phase bed reactor), a prolific isoparaffin catalytic cracking 'combination of a riser series fast bed reactor," or any set of devices. The present invention preferably optimizes the catalytic cracking unit of the riser reaction II and the MIP reactor 11 201024400 (reactor described in Chinese Patent No. 99105903.4). Preferably, the reactor in the catalytic cracking unit is a riser reactor which comprises at least two reaction zones I and π from bottom to top in the vertical direction. In a further preferred catalytic cracking unit, a regenerated catalyst conveying device is disposed between the reaction zone π of the reactor and the catalytic cracking catalyst regenerator. The high temperature regenerant is introduced or not introduced into the reaction zone by means of the apparatus, thereby achieving control of the operational severity of the reaction zone II (including reaction temperature and agent to oil ratio, etc.) to further satisfy the regulation of the distribution of the final product. In addition, the reaction pressures described herein refer to gauge pressure unless otherwise specified. The reaction temperature of the reaction zone I of the catalytic cracking unit is 55 〇 7 〇〇. 〇, the ratio of the agent to the oil is 4-50 'reaction time is 〇.5_〗 〇 seconds, the atomized water vapor accounts for 2-5 〇 wt% of the feed amount, the reaction pressure is atmospheric pressure · 3 〇〇 kPa, preferably the reaction The temperature is 560-650. Hey, the ratio of the agent to the oil is 7_2 〇, the reaction time is ^ seconds, and the fog is owed? ,, ru accounted for 5_1〇% by weight of the feed amount, and the reaction pressure was loo-πο千帕0 ❹ The reaction temperature of the reaction zone of the catalytic cracking unit was 5GG-600°C, and the ratio of the two oils was 3-50'. The reaction time is 〇2_8 seconds. 'Atomized water vapor accounts for 2_2 〇 〇 〇 〇 / , = from the reaction pressure to atmospheric pressure -300 kPa, preferably the reaction temperature is 510-560 ° C, #丨丨, The ratio is 5-40, the reaction time is 〇.5-1.5 seconds, the atomized water vapor accounts for 4-8 wt% of the feed feed amount, and the reaction pressure is 100-300 kPa. The catalytic cracking catalyst of the agent 2 is a combination of one or more of the following. The catalytic cracking provided by the prior art is usually an inorganic oxide and optionally (iv) soil, and the content of each component is 12 201024400: 5 to 50% by weight of zeolite, and ~70 by weight of inorganic oxide. /. . %weight. /. , the soil of the dry soil 0 as an active component, selected from the group ... ..., 曰 hole, feldspar and optionally medium pore zeolite, macroporous / vermiculite accounted for 25~ soil θ n / of the active component $ ® % is preferably 50 to 100 weight I / 〇, and the medium pore zeolite accounts for 〇 to % by weight of the active component. Heavy *〇/(四)0~50 The large hole Buddha stone is selected from γ type Buddha stone, rare earth γι^ stone (rey), _ rare earth hydrogen γ type stone (REHY), ultra stable γ type buddha (usy), rare earth One or a mixture of two or more of ultra-stable Y-type stagnation stones (REUSY). The mesoporous fossil is selected from the ZSM series zeolite and/or the zeolitic zeolite, and can also modify the non-metallic elements such as the above-mentioned mesofoss (four) and/or the transition metal elements such as iron, the beginning and the recording, and the ZSM series of stagnant stones. From MM. ZSM-11 ^ ZSM-12 > ZSM-23 > ZSM-35 ^ 2SM-38 > A mixture of any one or any of ZSM-48 and other similarly structured zeolites. The inorganic oxide is used as a binder and is selected from the group consisting of cerium oxide (si〇2) and/or aluminum oxide (ai2o3). The clay acts as a substrate, i.e., a carrier, selected from the group consisting of kaolin and/or hydrous kaolin. The catalytic cracking process and the catalysts employed therein are described in USP 6,495,028, CN110116, CN110116C, CN1072032C, CN1814705, CN1814707, CN1854251, and CN1854254, respectively, which are incorporated herein by reference. According to the method provided by the present invention, the separation oil formed by the hydrotreatment reaction or the oil formed by the catalytic cracking reaction can be separated by distillation 13 201024400 to obtain the hydrogenated naphtha and hydrogen wood. And hydrogenated tail oil or liquefied petroleum gas, catalytic cracking gasoline, catalytic cracking diesel catalyzed cracking back to refinery and other products. The method of distillation is well known in the art. Typically, one or more of the operations of the ablation, atmospheric distillation and vacuum distillation may be included to complete the desired separation. ', to be reflected in, distillate oil? Incorporating the adjustment of the operating conditions, thereby obtaining the advantages of the present invention, compared with the prior art, the main effect of the invention, by cutting the hydrogenated tail oil into light distillate oil and different reaction zones of the heavy cracking unit and different reactions The zone is integrated to control the distribution of the desired product in the cracking reaction of the hydrogenated hydrocarbon oil. For example, the heavy portion of the oil alone or with other extraneous heavy hydrocarbons, together with the introduction of the catalytic cracking reaction zone, while using a larger ratio of oil to oil, 7-16) and higher oil contact temperature (for example, 58 〇 _ 65〇.〇In order to increase the cracking depth of heavy oil', it is beneficial to increase the light oil in the catalytic cracking product; the light distillate oil is cut into the catalytic cracking reaction zone alone or together with other external light hydrocarbon oils. The cracking reaction occurs under the action of the catalytic cracking catalyst mixed with the material rising from the first reaction zone, and the catalytic cracking catalyst is first reacted with the heavy oil fraction in the first reaction zone to generate a quantitative amount on the catalyst. Coke to purify the catalyst. These will reduce the cracking conversion depth of the oil, which is beneficial to improve the yield of gasoline, diesel and low gas products. 2. Hydrogenated tail oil and other light or heavy oils After the feed is effectively combined, the bottom-up of at least two reaction zones of the catalytic cracking unit reactor is introduced into the octane 11 to control the cracking reaction of the hydrocarbon oil, thereby obtaining the rationality 14 201024 400. The α-mouth knife cloth is produced. For example, the hydrogenated Μ ^ ^ ^ hair / is introduced into the catalytic cracking reaction zone together with other heavy catalytic cracking crude oil, and is made 1 due to the hydrogenation The tail oil 1* first has the effect of diluting heavy oil. At the same time, because the oxidation tail oil contains catalytic cracking cycle oil modified by hydrogen, its higher aromaticity can further strengthen the asphalt f and aromatic hydrocarbons in heavy hydrocarbons. The dissociation phase of the micelle can significantly improve the efficiency of the contact reaction between the oil and the catalyst, while using a larger agent oil ratio (for example, 5-12) and a higher agent oil contact temperature (for example, 58 〇 _65 〇. 〇), ❹ The reaction residence time is controlled at Μ5 seconds to increase the cracking depth of heavy oil, which is beneficial to the improvement of light oil yield in catalytic cracking products; then the light hydrocarbon oil is introduced into the catalytic cracking reaction zone. , the cracking reaction occurs under the action of the catalytic cracking catalyst mixed with the material rising from the first reaction zone, wherein the reaction temperature of the reaction is preferably 510-54 (TC' ratio of oil to oil is 9_4 〇, reaction Time stop time is controlled at 1.0-1.8 Since the catalytic cracking catalyst in the first reaction zone is first contacted with the heavy oil fraction, a certain amount of coke is formed on the catalyst to passivate the catalyst. These will reduce the cracking conversion depth of the light distillate oil, and improve the gasoline. The diesel yield and the yield of the reduced gas product are favorable. 3. By introducing a regenerated catalyst delivery device between the reaction zone of the reactor and the catalytic cracking catalyst regenerator, a reaction can be introduced in the reaction zone II of the reactor. A new high-temperature regenerant to adjust the severity of the reaction, while the reaction zone I adopts a relatively mild reaction condition, which can effectively reduce the dry gas yield and increase the yield of high-value products. For example, the heavy oil alone The catalytic cracking reaction zone I is introduced with a larger agent to oil ratio (for example, 1 〇 _ 18), a moderate agent oil contact temperature (for example, 550-600 ° C), and a reaction residence time control of 15 201024400 at 0.9-1.3 seconds. Increasing the depth of cracking conversion of heavy oil can reduce the dry gas yield; then the hydrogenated tail oil is mixed with other external light hydrocarbon oils and then introduced into the catalytic cracking reaction zone. The cleavage reaction occurs by mixing with the material rising from the first reaction zone and under the action of the catalytic cracking catalyst therein. Since the catalytic cracking catalyst is first reacted with the heavy oil fraction in the first reaction zone, a "quantitative line-money catalyst passivation" is formed on the catalyst but the reaction is carried out due to the regenerated catalyst newly introduced from the regenerator. The conversion capacity of the catalyst in the zone II system is enhanced, preferably the reaction temperature A 520-58 (TC 'agent oil ratio is 9-18), the reaction time residence time is controlled at i.3-2.0 seconds, which can enhance the conversion of heavy oil while improving gasoline. The yield of two value products, such as diesel yield, inhibits dry gas yield.

The process provided by the present invention is particularly useful for the conversion of hydrocarbon oils to produce light oil products such as flakes, diesel, and the like. The method of the present invention is to add the hydrogenated tail oil heavy fraction and the optional uncut & tailing oil to the reaction zone 1 according to the present invention. And the hydrogenated tail oil is taken into the zone II. The light fraction accounts for 1〇_5〇% by weight of the total amount of the hydrogenated tail oil; the cutting causes the light fraction to account for 20_45% by weight of the total amount of the hydrogenated tail oil, and the cut is made to make the light fraction account for the total amount of the hydrogenated tail oil. The reaction conditions of the 25_35 heavy ^% excellent first reaction zone include: the reaction temperature is 55 〇 _7 〇 generation, the ratio of the agent to the oil is 5.2 〇, the reaction time is G 5_1 G sec, and the amount of the atomized water is 2 _ 5 °. % by weight, the reaction pressure is kPa at the normal pressure side; preferably, the ratio of oil to oil of 7-16, the ratio of the oil is 7-16, and the reaction conditions of the zone include: the temperature is 56 〇 _65 〇t, the reaction The time A 1-2 seconds, the atomized water vapor accounts for the feed amount, and the reaction pressure is 100-300 kPa. The reaction conditions of the third reaction zone include: _ 旰 栝 脉 脉 脉 脉 脉 脉 rc rc rc rc rc rc rc rc rc rc rc rc rc rc rc rc rc rc rc rc rc rc rc rc rc rc rc rc rc rc rc rc rc rc rc rc rc rc Thousand kPa; preferably the first reaction conditions include: the temperature is 51G_56 (rc, the ratio of the agent to the oil is ΐ (Μ8'^

The time should be 0.5 - 1.5 seconds, the atomization of the Taijie, Shishang, the female hydrating water π accounted for 4-8 wt% of the feed amount, the reaction pressure is 100-300 kPa. According to an embodiment of the present invention, the contact reaction with the catalytic cracking catalyst is to add the hydrogenated tail oil light fraction to the reverse bank, and to distill the halogenated tail oil and optionally Uncut hydrogenated tail oil is added to reaction zone II. The light fraction accounts for 丨〇_5〇% by weight of the total amount of the hydrogenated tail oil; preferably, the cleavage makes the light fraction account for 20_45 by weight of the total amount of the hydrogenated tail oil = the cut is selected so that the light fraction accounts for the total hydrogenated tail oil 25_35 wt% of the amount. In this embodiment, the first! The reaction conditions of the reaction zone include a reaction temperature of 550 to 700. (:, the ratio of agent to oil is 5_2 〇, the reaction time is 〇5_1 〇 seconds, the atomized water vapor accounts for 2-50% by weight of the feed amount, and the reaction pressure is atmospheric pressure _% 〇 kPa; preferably, the reaction temperature of reaction zone I is 56〇_65〇〇c, the ratio of the agent to the oil is 7-16, the reaction time is ^.5 seconds, and the atomized water vapor accounts for the weight % of the feed amount. The reaction pressure is 100-300 kPa. In this embodiment The reaction conditions of the second reaction zone include: the temperature is 500-60 (TC, the ratio of the agent to the oil is 7-20, the reaction time is 〇2_8 seconds, the atomized water vapor accounts for 2-20% by weight of the feed amount, and the reaction pressure is constant Pressure _3〇〇 thousand 17 201024400 Pa; preferably the reaction temperature of the second reaction zone is 52〇-56 (TC, the ratio of agent to oil is 10-18, the reaction time is 1-2 seconds, and the atomized water vapor accounts for the feed amount. 4_8 wt% 'reaction pressure is 100-300 kPa. The regenerated catalyst can be decomposed in the reaction zone π 3. According to an embodiment of the invention, the contact reaction with the catalytic cracking catalyst is the hydrogenation tail oil The heavy fraction and optional uncut pets and/or conventional catalytic cracking feedstock oil are added to reaction zone I, and the hydrogenation is described The oil light fraction is added to the reaction zone II. The light fraction accounts for 10 to 50% by weight of the total amount of the hydrogenation tail; preferably the cleavage is such that the light fraction accounts for 20 to 45% by weight of the total amount of the hydrogenated tail oil; more preferably The cutting causes the light fraction to account for 25-35 wt% of the total amount of the hydrogenated tail oil. In this embodiment, the reaction conditions of the 'first reaction zone include: the reaction temperature is 550-700 ° C. The ratio of the agent to the oil is 5- 20 'reaction time is 5.5_1 〇 seconds, atomized water vapor accounts for 2-50% by weight of the feed amount, and the reaction pressure is atmospheric pressure _3 〇〇 kPa; preferably, the reaction conditions of the first reaction zone include: temperature is _ 560_650 ° C, the ratio of agent to oil is 7-16, the reaction time is 1-2 seconds, the atomized water vapor accounts for 5-10% by weight of the feed amount, and the reaction pressure is ι〇〇_3〇〇 kPa. In this embodiment, the reaction conditions of the second reaction zone include: the temperature is 500-600 ° C, the ratio of the agent to the oil is 3-20, and the reaction time is 〇.2_8 seconds. The atomized water vapor accounts for 2-20 of the feed amount. % by weight, the reaction pressure is atmospheric pressure _3 〇〇 kPa; preferably, the reaction conditions of the second ruthenium reaction zone include: temperature of 51 〇 _ 56 〇 < t, ratio of agent to oil of 6-14, reaction time of 0.54.5 second The atomized water vapor accounts for 4-8 wt% of the feed amount, and the reaction pressure is 1 〇〇 3 〇〇 kPa. According to an embodiment of the present invention, the contact reaction with the catalytic cracking catalyst 18 201024400 is The hydrogenated tail oil light fraction and optionally the conventional catalytic cracking feedstock oil are added to reaction zone I, and the hydrogenated tailstock heavy fraction and optional uncut hydrogenated tail oil are added to reaction zone π. Light ends Between 10 and 50% by weight of the total amount of hydrogenated tail oil; preferably, the cleavage makes the light fraction account for 20-45% by weight of the total amount of the hydrogenated tail oil; more preferably, the cleavage makes the light fraction account for the total amount of hydrogenated tail oil 2 5 - 3 5 wt%. In this embodiment, the reaction conditions of the first reaction zone include: the reaction enthalpy temperature is 550-70 (TC, the ratio of the agent to the oil is 5-2 Torr, the reaction time is 0·5_1 〇 seconds, and the atomized water vapor accounts for the feed. 2_50% by weight of the amount, the reaction pressure is atmospheric pressure _3 〇〇 kPa; preferably, the reaction temperature of the reaction zone I is 560_65 (rc, the ratio of the agent to the oil is 7-16, the reaction time is seconds, and the atomized water vapor accounts for the feed. The weight % of the amount 'reaction pressure is 1 〇〇 3 〇〇 kPa. In this embodiment, the reaction conditions of the ruthenium reaction zone include: the temperature is 500-600. (:, the ratio of the agent to the oil is 7_2 〇 'reaction The time is _2_8 seconds, the atomized water vapor accounts for 2_2〇% by weight of the feed amount, and the reaction pressure is atmospheric pressure _3〇〇千❹帕; preferably, the reaction temperature of the π reaction zone is 520·56〇χ: The oil ratio is W - 18, the reaction time is 1-2 seconds, the atomized water vapor accounts for the weight % of the feed amount, and the reaction pressure is 100 - 300 kPa. In the reaction zone u, a regenerated catalyst can be introduced. In one embodiment, the contact reaction with the catalytic cracking catalyst is to recycle the hydrogenated tail oil heavy fraction, conventional catalytic cracking heavy And optionally the uncut hydrogenated tail oil is added to the reaction zone 4, and the light tailing of the = tailing oil and the conventional catalytic cracking light feedstock are added to the reaction zone ^. The light library accounts for the total amount of hydrogenated tail oil The weight of 1〇_5〇 is preferably such that the cut 19 201024400 cuts the light fraction to 20_45% by weight of the total amount of the hydrogenated tail oil; more preferably, the cut causes the light fraction to account for 25_35 wt% of the total amount of the hydrogenated tail oil. In this embodiment, the reaction conditions of the first reaction zone include: the reaction temperature is 550-700. The ratio of the tanning agent oil is 4-20', the reaction time is 〇5_1〇 seconds, and the atomized water vapor accounts for 2-50% by weight of the feed amount. The reaction pressure is atmospheric pressure _3 〇〇 kPa; preferably, the reaction conditions of the first reaction zone include: temperature of 560-650 ° C, ratio of agent to oil of 5 _ 16 , reaction time of 1-2 seconds, steaming of atomized water The reaction charge is 5-1 〇〇 kPa, and the reaction pressure is 1 〇〇 3 〇〇 kPa. In this embodiment, the reaction conditions of the second reaction zone include: a temperature of 5 〇〇 -60 (TC, The ratio of agent to oil is 3_2〇, the reaction time is 〇2_8 seconds, the atomized water vapor accounts for 2_2〇% by weight of the feed amount, and the reaction pressure is atmospheric pressure _3〇〇 kPa. Preferably, the reaction conditions of the second reaction zone include: a temperature of 51 〇 _ 56 〇, a ratio of the agent to the oil of 6-14, a reaction time of 〇·5_15 seconds, and an atomized water vapor of 4-8 by weight in the feed. 〇, the reaction pressure is 1〇〇3〇〇 kPa. According to an embodiment of the present invention, the contact reaction with the catalytic cracking catalyst is a light fraction of the hydrogenated tail oil and a conventional catalytic cracking heavy raw material, and The selected uncut hydrogenated tail oil is added to the reaction zone, and the hydrogenated tail oil heavy fraction and the conventional catalytic cracking light feedstock oil are added to the reaction zone. The light crane fraction accounts for 1% of the total amount of the hydrogenated tail oil. 5 重量% by weight; preferably the cleavage is such that the lighter occupies 2% to 45% by weight of the total amount of the hydrogenated tail oil; more preferably, the cleavage causes the light fraction to account for 25-35% by weight of the total amount of the hydrogenated tail oil. The gasification tail, the proportion of participation by light fraction is at least greater than zero, and there is no maximum ratio. / In this embodiment, the reaction conditions of the '帛1 reaction zone include: the reaction temperature is 55〇-7〇〇t:, the ratio of the agent to the oil is 5-20, and the reaction time is 5.5_1〇 second, 20 201024400 atomized water The steam accounts for 2-50% by weight of the feed amount, and the reaction pressure is atmospheric pressure _3卯 kPa; preferably, the reaction temperature of the reaction zone I is 560_65 (rc, the ratio of the agent to the oil is 7-16, the reaction time is i_15 seconds, the atomized water The steam accounts for the weight % of the feed amount, and the reaction pressure is 1〇0_3〇〇 kPa. In this embodiment, the reaction conditions of the second reaction zone include: the temperature is 500-600 ° C, and the ratio of the agent to the oil is 7-50. The reaction time is 〇2_8 seconds, the mist = water vapor accounts for 2-20% by weight of the feed amount, the reaction pressure is atmospheric pressure _3〇〇 ❹pa; preferably, the reaction temperature of the second reaction zone is 520_560〇c, and the ratio of the agent to the oil is 8-40, the reaction time is 1-2 seconds, the atomized water vapor accounts for the weight % of the feed amount, and the reaction pressure is 100-300 kPa. In the reaction zone, the regenerated catalyst can be introduced. According to an embodiment of the present invention, The contact reaction with the catalytic cracking catalyst is to conventionally catalyze the cracking of the heavy feedstock oil and the uncut hydrogenated tail. The oil is added to the reaction zone I, and the conventional catalytic cracking light feedstock oil is added to the reaction zone II. The conventional catalytic cracking of the heavy feedstock oil and the hydrogenation tail oil is mixed, and the content of the hydrogenated tail oil is within 90% by weight. Preferably, the content of the hydrogenated tail oil is within 80% by weight. In this embodiment, the reaction conditions of the first reaction zone include: the reaction temperature is 550-700. (:, the ratio of the agent to the oil is 4-20, and the reaction time is 〇 5_1 〇 second, the atomized water vapor accounts for 2-50% by weight of the feed amount, and the reaction pressure is atmospheric pressure _3 〇〇 kPa; preferably, the reaction conditions of the first reaction zone include: temperature 560-650 ° C, the agent oil The ratio is 5_16, the reaction time is 1-2 seconds, the atomized water vapor accounts for 5-10% by weight of the feed amount, and the reaction pressure is ι〇〇_3〇〇 kPa. In this embodiment, the third reaction zone The reaction conditions include: temperature 21 201024400 is 500-600 ° C, the ratio of agent to oil is 7-50, the reaction time is 〇.2_8 seconds, the atomized water vapor accounts for 2-20% by weight of the feed amount, and the reaction pressure is constant. Pressure _3 〇〇 kPa; preferably the reaction conditions of the third reaction zone include: temperature 510_56 (Γ (:, ratio of agent to oil is 8 _ 40, the reaction time is 0.5-1.5 seconds, the atomized water vapor accounts for 4-8 wt% of the feed amount, and the reaction pressure is 100-300 kPa. The contact reaction with the catalytic cracking catalyst according to an embodiment of the present invention The conventional catalytically cracked heavy feedstock oil and optionally conventional rhodium-catalyzed cracked feedstock oil are added to reaction zone I, and the conventional catalytically cracked light feedstock oil and uncut hydrogenated tailstock oil are added to reaction zone π. In the mixed feed of the conventional catalytic cracking light feedstock oil and hydrogenated tail oil, the gasification tail is contained within a content of 50% by weight, preferably the hydrogenated tail oil is within 4%'%. In this embodiment, the reaction conditions of the first reaction zone include a reaction temperature of 550 to 700. (:, the ratio of the agent to oil is 4-20, the reaction time is 〇5_1 〇 seconds, the atomized water vapor accounts for 2-50% by weight of the feed amount, and the reaction pressure is atmospheric pressure _3 〇〇〇 kPa; preferably the reaction zone The reaction temperature of I is 560-650. The ratio of the ratio of the agent to the oil is 5, the reaction time is 丨_丨.5 seconds, the atomized water vapor accounts for $ _ 1 〇% by weight of the feed amount, and the reaction pressure is 1〇〇. In this embodiment, the reaction conditions of the second reaction zone include: the temperature is 500-600t, the ratio of the agent to the oil is 7_5 〇, the reaction time is 〇2_8 seconds, and the mist Z water vapor accounts for the feed amount. 0 2_2〇% by weight, the reaction pressure is normal pressure (10) kPa, preferably the reaction temperature of the π reaction zone is 52〇_56 (rc, the ratio of the agent to oil is =40 'reaction time is _2 seconds), and the atomized water vapor accounts for The weight of the feed amount is 5% by weight, and the reaction pressure is (10) kPa. In the reaction zone, 22 201024400 regenerated catalyst can be introduced. According to the procedure shown in Fig. 1, hydrogen gas introduced from 8 horses by 8 is mixed with residual oil and The device 2 for removing catalytic cracking of the solid particles back to the refining oil 1 is contacted with the hydrogenation catalyst, and the reaction product is introduced to the product separation device 30 Separation, the obtained gas is passed through ^1 naphtha by 12, hydrogenated diesel oil is led out by 13, hydrogenated tail oil ^8 or all by hydrazine into the hydrogenated tail oil branch tower 4 to separate into light and heavy two: φ parts, The separation is such that the light fraction accounts for 10 to 80% by weight, preferably 20 to 70% by weight, more preferably 3 to 6% by weight, based on the total amount of the hydrogenated tail oil. 16 The hydrogenated tail oil, which is cut separately or in combination with other external cracking feedstocks 4 and/or which has not entered the hydrogenated tailings fractionation column 4, is mixed into the catalytic cracking reaction zone I to participate in the reaction; the light distillate oil is passed through 15 alone or with The other cracked feedstock oil 40 and/or the hydrogenated tail oil not cut into the hydrogenation tail oil fractionator 4 are mixed and then enter the catalytic cracking reaction zone η to participate in the reaction. The catalytic cracking reaction product is separated from the catalyst crucible after the catalytic cracking reactor 5 is separated from the catalyst. After being separated into the catalytic cracking product separation device 3 through 18, the obtained gas is passed through 19, the catalytic gasoline is passed through 20, the catalytic diesel oil is passed through a 21 take-out device, and the catalytic cracking is returned to the refining oil partially or completely by 22 into the catalytic cracking back to the refining oil filter 1 for filtration. Over The content of solid particles in the catalytic cracking back to the refinery through 10 into the hydrotreating reaction device 2 is less than 30 wtppm, the particle size of the solid particles is less than 1 Ομηι, more preferably less than 15 wtppm, and the particle size is less than 5 μηη. When partially catalyzed by cracking back to the refining oil After filtering and entering the hydrogenation unit for hydrogenation and subsequent reaction, the remaining part is taken out by 23 and can be used as a raw material for producing fuel oil, acicular petroleum coke and carbon black. In the catalytic crack 23 201024400, the reaction settler 5 is separated from the cracked product. The latter catalyst is regenerated through the catalyst regenerator 7 via 24, and the regenerated catalyst is reacted through the 25 cycles into the catalytic cracking reactor 6. 〃 Follow the map! The flow shown is to change the ratio of the light and heavy two fractions obtained by vacuum separation of the hydrogenated tail oil by changing the amount of the catalytic cracking back oil to be introduced into the nitriding treatment device, and changing the proportion of the light oil to the oil Gufen oil flat 16 in the catalytic cracking reactor on the feed position and operating conditions and other factors, it is easy to control the distribution of the product of the cracking reaction, to ensure the full conversion of cracking raw materials while achieving the goal of producing more gasoline and diesel. According to the procedure shown in Fig. 2, the hydrogen introduced by 8, the introduced residual oil and the optional distillate oil, and the catalytic cracking of the solid particles obtained by the removal of the solid particles are introduced into the hydrogenation unit and the hydrogenation treatment catalyst. Contact reaction, the reaction product is led to the product separation device 3〇 for separation, and the obtained gas is passed through 11. The hydrogenated naphtha is passed through 12, the argonized diesel oil is passed through a 13-out device, and the hydrogenated tail oil is introduced into the heavy product through 14 and 16 The feedstock oil enters the catalytic cracking reaction zone I and the catalytic cracking catalyst contact reaction, and the light cracking feedstock oil 15 enters the catalytic cracking reaction zone II to contact with the catalytic cracking catalyst. The catalytic cracking reaction product is separated from the catalyst by the catalytic cracking reactor 5 and separated into 18 by the catalytic cracking product separation device 3, and the obtained gas is subjected to i9, the catalytic oil is passed through 20, the catalytic diesel oil is filtered through the 2 1 extraction device, and the catalytic cracking is carried out. Part or all of the refinery (including heavy-cycle oil, clarified oil or one or more of the total catalytic cracking cracked heavy oil remaining after the catalytic cracking of the diesel oil) is partially or completely introduced into the refinery solid particulate separator 1 to separate the solid particles therein. . The separation is such that the amount of solid particulate matter in the catalytic cracking back to the refinery via 10 into the hydrotreating reactor 2 is less than 30 wtppm, the particle size of the solid particulates is less than 1 Ομηη, more preferably less than i 5 wtppm, and the particle size is less than 5 μηη. When the partially catalyzed cracked refinery oil is filtered and then introduced into the chlorination treatment unit for hydrogenation and subsequent reaction, the remaining portion is taken up by 23, and can be used as a raw material for producing fuel oil, acicular petroleum coke and carbon black. After the separation of the catalytic cracking reactor settler 5 and the cracked product, the catalyst is passed through 24

The regenerant 7 is regenerated, and the regenerated catalyst is reacted through the catalytic cracking reactor 6 through 25 cycles. Except as given in the scheme shown in Figure 2, the hydrogenated tail oil is passed through a feed mode in which the catalytic cracking reaction zone I is contacted with the catalytic cracking catalyst via a heavy feedstock oil introduced via 16 and the hydrogenation tail is passed. The oil enthalpy can also optionally be mixed with the conventional catalytic cracking feedstock oil in two other ways and then enter the catalytic cracking reaction zone to contact with the catalytic cracking catalyst: 〇 and the 15 bow! The incoming light cracked feedstock oil enters the feed mode of the catalytic cracking reaction zone and the catalytic cracking catalyst contact reaction; 2) the hydrogenated tail oil can be cut into two strands, one of which is a heavy fraction or a light fraction of the hydrogenated tail oil In combination with the light cracking feedstock oil introduced by 15 into the catalytic cracking reaction zone η and the catalytic cracking catalyst contact reaction, while the hydrogenated tail oil money or light library in the other stocks and 16 intensive heavy feedstock oil A feed mode in which a catalytic cracking reaction zone I is contacted with a catalytic cracking catalyst. Fig. 3 is a schematic flow chart showing a combination method provided by the present invention. The difference between the hydrogenation treatment of the hydrocarbon oil and the catalytic cracking group W 3 and FIG. 2 is that 26 of the temperature-regenerating agent is introduced from the regenerator to the reaction zone I!, and the hydrogenated tail oil is passed through 14 and the light source of 15 is introduced. 25 201024400 The feedstock enters the catalytic cracking reaction zone π to contact with the catalyst, and the heavy feedstock oil 16 enters the catalytic cracking reaction zone I to contact the catalyst. Among them, the position of the high-temperature regenerant 26 introduced in the reaction zone η should satisfy the residence time of the hydrocarbon in the reaction zone 不 not less than 〇·2 seconds, and the preferential residence time is not less than 1 second. By introducing a high-temperature regenerated catalyst from the regenerator into the reaction zone II in the reactor 6, the reaction temperature and operation of the reaction zone π can be flexibly modulated.

The ratio of agent to oil and reaction time, etc., can better modulate the distribution of cracked products to meet different needs. After the .... (4), the nipple first" Tianli 丄 丄 15 15 introduced by the light feedstock oil - into a catalytic cracking reaction zone of the vertical fish catalytic cracking catalyst contact reaction of a feed mode, hydrogenated tail oil can also be 14 The other two ways are mixed with the f-catalyzed cracking feedstock oil and then contacted with the catalytic cracking catalyst in the catalytic cracking reaction zone: f human heavy cracking feedstock oil 4 enters the catalytic cracking reaction zone! The feed mode of the contact reaction with the catalytic cracking catalyst; 2) the hydrazine hydrogenated tail oil is cut into two strands, wherein the hydrogenated tail oil weighs / 31 from one of the heavy fraction or the light fraction and the light cracked feedstock oil Catalytic cracking reaction zone: Catalyst contact reaction, and the feed mode of the gasification tail oil and the heavy feedstock oil sheep introduced by 16 and the catalytic cracking catalyst contact reaction Although the implementation of the present invention has been described in the drawings and the accompanying drawings, it is not intended to be in the spirit and scope of the corresponding embodiments:::r: package improvements, and equivalents. 26 201024400 The following examples will further illustrate the invention, but are not intended to limit the invention. The feedstock oil is processed by the process shown in Fig. 1, wherein the raw material of the hydrogenation unit is mixed by crushing oil and catalytic cracking back to refinery oil (i.e., dilution oil) according to different ratios.

The raw materials A and B, the raw oils and B properties are listed in Table iQ. The hydrotreating reaction is carried out on a reactor comprising three fixed beds, wherein the first reactor is an upflow fixed bed reactor (UFR). The reactor is read up to the top and the RUiM and ruf_2 catalysts are charged in a ratio of 1:2, the catalyst accounts for 44% of the total packed volume of the hydrogenation unit catalyst, and the second reactor and the third reactor are the downflow fixed bed reactor. The second reactor is loaded with the demetallization catalyst RDM_2 'The loading of the catalyst in the second reactor accounts for 12% of the total loading volume of the hydrogenation unit catalyst: the third reactor is charged with the desulfurization catalyst RMS - the loading of the catalyst in the third reactor The amount accounts for 44% of the total packed volume of the nitriding device catalyst (the above catalysts are all products of Sinopec Changling Catalyst Factory). The catalytic cracking reaction is carried out in a riser reactor comprising two reaction zones, RMS_8 (product of Sinopec Qilu Catalyst Factory). The solid particles in the catalytic cracking back to the refining oil (for the catalytic cracking of the heavy-cycle oil and the clarified oil) are filtered and removed by a filtering device, wherein the filter filter and the transition pore diameter of the core are 〇. The particle size and content of the solid particles in the filtered catalytic cracking cycle oil were 5 micrometers and the filtration temperature was 250 C. 27 201024400 Embodiment 1 This embodiment illustrates the effect of providing a method. The raw material oil introduced into the hydrotreating reaction apparatus was the raw material oil A, and the hydrogenation treatment reaction conditions and the product distribution of the hydrogenation-treated oil were shown in Table 2. The hydrogenated tail oil light library (55% by weight of the total gasification tail oil) and the hydrogenated tail oil heavy fraction (45% by weight of the total hydrogenated tail oil of the bottom heavy oil) were obtained by steam distillation. The oil properties of the oils are listed in Table 3. The hydrogenated tail oil heavy distillate oil is introduced into the catalytic cracking reaction zone I, respectively. The nitriding tail oil® light distillate oil is introduced into the catalytic cracking reaction zone and is contacted with the catalyst cracking catalyst. The reaction, catalytic cracking reaction conditions and results are shown in Table 4. Comparative Example 1 The raw material oil, the catalyst used and the operating conditions processed in this comparative example were the same as in Example 1, except that the hydrogenated tail oil was directly introduced into the catalytic cracking reaction zone without being separated, and the catalytic cracking catalyst was contacted. The nitrogen-treated tail oil properties are listed in Table 3. The catalytic cracking reaction conditions and results are shown in Table 4. Example 2 This example illustrates the effect of providing the process. Among them, the feedstock oil introduced into the hydrotreating reaction apparatus is the feedstock oil B, and the hydrogenation treatment reaction conditions and the hydrogenation treatment are not listed in Table 2. The hydrogenated tail oil light fraction (39% by weight of the total hydrogenated tail oil) and the hydrogenated tail oil recycled portion (61% of the total hydrogenated tail oil 28 201024400% by weight of the bottom heavy oil) were obtained by distillation under reduced pressure. 'The properties of the two distillate oils are listed in Table 3. The hydrogenated tail oil heavy distillate oil is separately introduced into the catalytic cracking reaction zone I, the gasification tail is introduced into the catalytic cracking reaction zone by light distillate oil, and the catalyst cracking catalyst is contacted with the reaction. The catalytic cracking reaction conditions and results are listed in Table 4. Comparative Example 2 The raw material oil, the catalyst used and the operation bar processed in this comparative example were the same as in Example 2, except that the hydrogenated tail oil was directly introduced into the catalytic cracking reaction zone 1 without contact with the catalytic cracking catalyst. The reaction, hydrogenation tail oil properties are listed in Table 3, catalytic cracking reaction conditions and results are listed in Table 4. 29 CQ 80% 20% Hydrogenated mixed feedstock 0.9789 49.23 9.33 85.90/ 10.93 2.66/0.40 15.8/34.1 8.6/0.6/1.5 30.3/ 45.5 21.4/2.8 49.9 Residue 0.9795 68.19 11.30 85.44/11.02 3.00/0.44 19.8/42.6 10.7/ 0.7/1.9 27.5/45.1 23.9/3.5 62.4 ! JP cleavage back to refining oil 0.9764 8.396 1.44 87.76/10.58 1.3/0.26 41.7/47.0 11.4/C0.1 ο U") < 90% 10% Hydrogenated mixed raw material 0.9783 55.69 11.00 85.67 /10.98 2.83/0.42 17.8/38.3 9.6/0.6/1.7 28.1/46.8 22.7/2.4 56.2 Residue 0.9795 68.19 11.30 85.44/11.02 3.00/0.44 19.8/42.6 10.7/0.7/1.9 27.5/45.1 23.9/3.5 62.4 Catalytic cracking back to refinery __ 丨8.396 1.44 87.76/10.58 1.30/0.26 41.7/47.0 11.4/<0.1 ο Raw oil composition of raw material oil, wt% Residue catalyzed cracking back to refining property density (20 〇' g/cm3 viscosity (100 〇, Mm2/s CCR,m% Elemental composition,% by weight C/HS/N Metal content, wtppm Ni/V/ Fe/Ca/Na Four components, wt% Saturated hydrocarbons/aromatics! Colloidal/asphaltene (C7 insolubles) 1 Ni+V 5 wtppm solid content, wtppm particle size _. blade) 201024400 2 Hydrogenation unit feed feed A feed B upper bed reactor hydrogen mixed, Nm3/m3 21026 21930 lower bed reactor mix, Nm3/m3 19627 19720 Ph2 * MPa 15.1 15.1 reaction temperature, °C upper bed reactor 393.5 393.8 Downflow bed reactor 394. 0 394.2 Item material name Feed, wt% oil break 90 80 Catalytic cracking back to refinery 10 20 Pure hydrogen 1.30 1.35 Total 101.30 101.35 Discharge, wt% Hydrogen sulfide 2.18 2.14 Gas 1.14 1.12 Hydrogenated naphtha 3.34 3.35 Hydrogenated Diesel 11.37 11.86 Hydrogenated tail oil 83.08 82.67 Ammonia 0.20 0.21 Total 101.30 101.35 31 201024400 Feed Β Comparative Example 2 Hydrogenated tail oil 253 0.9253 3.71 87.37/ 12.18 0.39/0.25 1 1.83/2.75 58.76 32.64 7.87 0.77 Example 2 Hydrogenation Tail oil heavy distillate oil 0.9351 5.76 87.22/12.04 0.5/0.3 3.00/4.50 52.4 35.8 10.6 CN Hydrogenated tail oil light distillate oil Os m 0.9103 m 〇87.61/12.39 0.21/0.17 68.7 27.7 cn 〇 Feed A Comparative Example 1 Hydrogenation Treatment of tail oil ο 1-Η 0.9315 4.43 86.94/12.08 0.77/0.24 1.53/3.15 60.56 33.45 5.68 0.37 Example 1 Hydrogenated tail oil weight Oil 0.9367 8.02 87.47/11.90 0.47/0.29 3.40 /7.00 51.7 37.3 10.3 argonized tail oil light oil ηη 0.9152 in 87.59/12.21 0.18/0.19 67.8 30.3 Ο) r-4 Hydrogenation unit feed example logistics name Total feed ratio, wt% ΓΠ BP balance carbon, weight % element composition, weight % C/HS/N metal content, wtppm Ni/V four components, wt% saturated hydrocarbon 辁 asphaltene (C7 insoluble) - 201024400 Table 4 Hydrogenation unit feed feed A feed B Example Example 1 Comparative Example 1 Example 2 Comparative Example 2 Reaction zone Π Working conditions Reaction temperature, °c (initial contact mixing) 550.5 540 Reaction time, seconds 1.3 0.8 Oil ratio * 12.7 15.4 Reaction zone I Working condition Reaction temperature, °c (initial contact mixing) 620 621 Difference 580 582 Difference reaction time, second 1.5 3 1.6 2.6 Agent oil ratio * 15.6 9.8 Regeneration temperature 713 713 713 713 Regeneration pressure (G), KPa 229.9 230.3 229.9 230.3 Total reaction time 2.8 3 2.4 2.6 Total agent to oil ratio * 7 7 6 6 Product distribution, weight % Acid gas 0.55 0. 51 0.04 0.50 0.51 -0.01 Dry gas 4.26 4.33 -0.07 4.00 4.10 -0.10 Liquefied petroleum gas 15.84 15.45 0.39 15.00 14.80 0.20 Stabilized gasoline 31.48 27.51 3.97 31.20 30.00 1.20 Diesel 34.17 34.35 -0.18 36.10 34.00 2.10 Oil crowd 3.46 7.29 -3.83 4.00 7.09 - 3.09 Coke 9.54 9.68 -0.14 8.70 9.00 -0.30 Loss 0.70 0.88 0.50 0.50 Total 100.00 100.00 100.00 100.00 Conversion, f 62.37 58.36 4.01 59.90 58.91 0.99 Light oil yield, 65.65 61.86 3.79 67.30 64.00 3.30 Total liquid yield, #1 % 81.49 77.31 4.18 82.30 78.80 3.50 Propylene yield, # 4.66 4.51 0.15 4.50 4.40 0.10 *Note: The ratio of the agent to the oil is the ratio of the catalyst participating in the reaction to the mass of the hydrocarbon oil. 33 201024400

Ο The results given in Table 4 clearly demonstrate that the selectivity of gasoline and diesel in the product distribution obtained by the process of the present invention is significantly improved compared to the direct conversion of hydrogenated tailstock to a catalytic cracking reactor. For example, implement 5 cases 1 and a control! The processing feedstock oil was the same, except that in Example i, the chlorinated tail oil was separated by light pressure and two fractions, and the two different reaction zones for catalytic cracking were respectively subjected to a hydrazine reaction. Comparing the results obtained by two different processing methods, the conversion rate of Example i increased by about 4 percentage points, the gasoline yield increased by 3.97 percentage points, the coke yield decreased by 〇·_ percentage points, and the total liquid volume increased by 1〇. 4.18 percentage points. Example 2 was the same as Comparative Example 2 processing stock oil, and the results obtained by two different processing methods were compared, wherein the conversion rate of Example 2 was increased by about 1%, the diesel oil yield was increased by 210%, and the gasoline yield was increased by 1.2. Percentage points, coke yield decreased by 〇·3 percentage points, and total liquid collection increased by 3.5 percentage points. 15 20 The deuteration treatment feeds of Example 1 and Example 2, the ratio of light, (four) parts of oil and the conditions of catalytic cracking reaction obtained by deuteration of deuterated tail oil under reduced pressure are not seen from the reaction results. The distribution is different. Among them, the conversion rate of the Example! is increased, and the cracked product is more lighter, and the diesel yield in Example 2? Significantly improved. This indicates that the amount of the catalytic cracking cycle in the feed by changing the hydrogenation treatment (feedstock A and feedstock B) 'changes the hydrogenation tail oil to a lighter, _ part oil ratio and catalytic cracking reaction conditions, etc. 'On the premise of the comparative conversion rate, the distribution of the product in the produced oil can be woven. ^ 34 201024400 Example 3 This example illustrates the effect of the processing according to the flow shown in Fig. 2. Wherein, the feedstock oil introduced into the hydrotreating reaction device is the feedstock oil A, the hydrogenation treatment reaction conditions and the product distribution of the hydrotreated oil to be produced are listed in Table 2, and the hydrogenated tail oil formed in 5 is named as hydrogenated tail oil c, and the feed e Yes - a commonly used catalytic cracking feed. Hydrogenated tail oil c and feed E accounted for % and (10) weight percent of total feed, respectively. Feed E is steamed under reduced pressure (4). (4) Catalytic cracking of light feedstock Η (distillation range 350_5〇〇t:, weight of feed E. 乂) and catalytic cracking of heavy feedstock oil G (hecheng is higher than 500t) , accounting for % by weight of feed ^), various feed properties of ω are listed in Table 5, the catalytic cracking heavy feedstock oil G and chlorine = tail oil C - the core catalytic cracking reaction zone! The catalytic cracking light crude oil is introduced into the catalytic cracking reaction zone π to react with the catalyst cracking catalyst, wherein the weight ratio of the hydrogenated tail oil c to the catalytic cracking heavy feed oil (IV) in the reaction zone is 3U. Catalytic cleavage reaction conditions and results are listed in Table 61. © Comparative Example 3 The stock oil processed in this comparative example, the catalyst used and the operating conditions: The same as in Example 3: hydrogenated tail oil. And the feed price also accounts for 2% by weight and 8% by weight, respectively. The difference is that the feed is not separated and the hydrazine and the hydrogenated tail oil C-starting catalysis (4) anti-consumption and the catalytic cracking catalyst contact reaction 'various feed properties are listed in Table 5_ conditions and results are listed in Table 6-1. Embodiment 4 35 20 201024400 This embodiment illustrates the effect of processing according to the flow shown in FIG. 2. Wherein, the feedstock oil introduced into the argon treatment reaction device is the feedstock oil B, and the hydrogenation treatment reaction conditions and the product distribution of the hydrotreated oil to be produced are listed in Table 2, wherein the hydrogenated tail oil produced is named as hydrogenated tail oil D, and the feed E is A commonly used 5 catalytic cracking feed (same as in Example 3). Hydrogenated tail oil D and feedstock accounted for 70% and 3% by weight of the total feed. Feed E was subjected to vacuum distillation to obtain catalytic cracking light feedstock H (distillation range of 35 〇 _5 〇〇〇 c, accounting for % by weight of feed e) and catalytic cracking of heavy feedstock oil G (distillation range was higher than 5〇〇.〇, accounting for 56% by weight of feed E), various feed properties are listed in Table 5-1. Introducing the catalytic 1〇 cracking heavy feedstock oil G and the hydrogenated tailing oil D into the catalytic cracking reaction zone I′, the catalytic cracking light feedstock oil H is introduced into the catalytic cracking reaction zone π and the catalyst cracking catalyst contact reaction, wherein the reaction zone I The weight ratio of hydrogenated tail oil D to catalytically cracked heavy feedstock oil G was 81:19. Catalytic cracking conditions and results are listed in Table 6-1. 15 Comparative Example 4 The raw material oil, the catalyst used and the operating conditions used in this comparative example were the same as in Example 4, in which the weathered tail oil d· and the feed £ were also too 2 〇 _ material '(4) and 30 weight respectively. %. The difference is that the feed is not ^ = 疋 directly introduced into the catalytic cracking reaction zone together with the deuterated tailings c. The catalytic cracking reaction is combined with the catalytic cracking. The various feed properties are listed in Table 5-1. Catalytic cracking reaction conditions and results are listed in Table 6-1. Embodiment 5 36 201024400 This embodiment illustrates the effect of processing according to the flow shown in FIG. Among them, the feedstock oil introduced into the deuteration treatment reaction device is the feedstock oil A, the hydrogenation treatment reaction conditions and the product distribution of the hydrotreated oil to be produced are listed in Table 2, and the weathered tail oil formed in the = is named hydrogenated tail oil C, and the feed jge One German ♦ '5 catalytic cracking feed for the T (same as in Example 3). Hydrogenated tail oil c and feed 2 accounted for 20% and 80% by weight of the total feed. Feed E was distilled under reduced pressure = catalytic cracking light feedstock enthalpy (distillation range 350_50 (rc, 44% by weight of feed E) and catalytic cracking of heavy feedstock G (column range higher than 5) 〇 (rc, accounting for 56% by weight of feed E), various feed properties are listed in Table 5-2. The catalytic-1 〇 cracked heavy feedstock oil G is separately introduced into the catalytic cracking reaction zone 1, the catalytic cracking light feedstock oil The hydrazine and hydrogenated tail oil c are introduced into the catalytic cracking reaction zone π to contact with the catalyst cracking catalyst, wherein the weight ratio of the hydrogenated tail oil c in the reaction zone π to the catalytic cracking light feedstock is 34: 66. The catalytic cracking reaction conditions and results are listed. Table 6-2. 15 Comparative Example 5 The raw material oil, the catalyst used and the operating conditions of the comparative example were the same as in Example 5, wherein the hydrogenated tail oil C and the feed enthalpy also accounted for 2 respectively. The material is 20% by weight and 8% by weight. The difference is that the feed ε is directly separated from the hydrogenated tail oil c into the catalytic cracking reaction zone without separation, and the catalytic cracking catalyst is contacted. Various feed properties are listed in the table. The cleavage reaction conditions and results are listed in Table 0-2. Example 6 37 201024400 The examples illustrate the effects of the process according to the flow shown in Fig. 3. 5 wherein the feedstock oil introduced into the hydrotreating reaction set is the feedstock oil 3, the nitriding treatment reaction conditions and the product distribution of the hydrotreated oil to form the oil are listed in Table 2, wherein The resulting hydrogenated tail oil is named hydrogenated tail oil D. Feed ε is a commonly used heavy oil catalytic cracking feed. Hydrogenated tail oil D and feed enthalpy account for % of total feed enthalpy and 7 G weight %, respectively. The steam cracking was carried out to obtain the catalytic cracking light feed oil mash (Gu Cheng is 35G province c, accounting for 44% by weight of the feed mash) and the catalytic cracking heavy feedstock oil G (the library is higher than 鸠.c, accounting for the feed (4) % by weight), various feed properties f are listed in Table 5-2. The catalytic cracking heavy feedstock oil G is separately introduced into the catalytic cracking reaction zone 1, and the catalytic cracking light feedstock oil and hydrazine tail oil D are introduced. The catalytic cracking reaction zone is contacted with the catalyst cracking catalyst, wherein the weight ratio of the hydrogenated tail oil D to the catalytic cracking light feed oil η in the reaction zone is 49:51. The catalytic cracking reaction conditions and results are shown in Table 6_2. 6 The original oyster sauce of JF's jfcL, _l " The catalyst and operating conditions used were the same as in Example 6, in which 1 g n J of the deuterated tailing oil D and the feed E were also separately occupied. The difference was that the feed E was not separated and the tail oil D was introduced into the catalyst. The cracking reaction zone is contacted with the catalytic cracking catalyst, and various feed properties are listed in Table 2. The catalyzed cleavage reaction conditions and results are shown in Table 6-2. The effect of the process of the process shown in Example 7. 38 This example According to Fig. 20 201024400, the feedstock oil introduced into the hydrotreating reaction device is the feedstock oil B. The hydrogenation treatment reaction conditions and the product distribution of the oil produced by the deuteration treatment are listed in Table 2, wherein the produced deuterated tailings oil is named as hydrogenated tail oil. D, feedstock is a commonly used heavy oil catalytic cracking feed. Hydrogenated tail oil D and feed E accounted for 5% and 70% by weight of the total feed, respectively. Feed E and hydrogenated tail oil D were subjected to vacuum distillation to obtain a catalytic cracking light feed oil enthalpy (distillation range 350_50 (rc, 44% by weight of feed e) and hydrogenated tail oil D light distillate oil (occupied Hydrogenated tailing oil D 39 parts by weight / 〇 and catalytic cracking heavy feed oil G (distillation range higher than 50 (rc, 56% by weight of feed E), hydrogenated tail oil D heavy distillate (accounting for -10 61% by weight of hydrogenated tail oil d), various feed properties are listed in Table 5-3. The catalytically cracked heavy feedstock oil G and hydrogenated tail oil D heavy fraction oil are introduced into the catalytic cracking reaction zone I The light-distilled oil of the catalytic cracking light feed oil H and the hydrogenated tail oil D is introduced into the catalytic cracking reaction zone and the catalyst cracking catalyst is contacted. The catalytic cracking reaction conditions and results are shown in Table 6_3. 15 ~ Comparative Example 7 The raw material oil, the catalyst used and the operating conditions were the same as in Example 7, and the hydrogenated tail oil D and the feed E also accounted for 30% by weight and 70% by weight, respectively, of the total feed, respectively. The material e and the hydrogenated tail oil 〇2〇 are separated from the light and heavy fractions, but are directly mixed and introduced into the catalytic cracking reaction zone I and the catalytic cracking. Catalyst reaction, various feed properties are listed in Table 5-3. Catalytic cracking reaction conditions and results are shown in Table 6_3 ^ 39201024400

Feed B Comparative Example 4 Reaction zone I Hydrogenated tail oil D 70.0 0.9253 ! 3.71 87.37 I 12.18 0.39 0.25 1.83 2.75 58.8 32.6 Ο) 00 d 4.58 Feed E 30.0 1 0.9351 1 5.07 87.22 12.04 0.50 0.24 4.70 5.70 52.4 35.8 10.6 1 ( Ν 10.40 Example 4 I-Reaction zone I Catalytic cracking of heavy feedstock G 16.8 0.9580 9.76 87.68 ! 11.64 0.74 0.27 8.80 j 10.80 38.7 43.3 15.9 Η 19.60 Hydrogenated tail oil 70.0 0.9253 1 3.71 87.37 12,18 0.39 0.25 m 00 2.75 58.8 32.6 Ο) 00 d 4.58 1 Reaction zone 催化 Catalytic cracking light feedstock Η 13.2 0.9103 (N Ο 87.61 I 12.39 0.21 0.17 Feed A Comparative Example 3 Reaction zone I Hydrogenated tail oil C 20.0 0.9315 4.43 86.94 1 12.08 0.77 0.27 1.53 cn 60.6 j 33.5 卜trt inch 4.68 Feed Ε 80.0 0.9351 :5.07 87.22 1 12.04 0.50 0.24 4.70 5.70 52.4 35.8 10.6 1 (Ν 10.40 Example 3 Reaction zone I Catalytic cracking of heavy feedstock G 44.8 0.9580 9.76 87.68 11.64 0.74 0.27 8.80 10.80 38.7 43.3 15.9 (Ν 19.60 Hydrogenated tail oil C 20.0 0.9315 4.43 86.94 1 12.08 0.77 0.27 1.53 3.15 60.6 33.5 Bu inch Ο 4.68 Reaction zone Π Chemical cracking light feedstock Η 35.2 0.9103 (Ν Ο 87.61 12.39 0.21 '0.17 Hydrogenation unit feed example catalytic cracking reaction zone feed stream name to total feed ratio, weight % density (20 ° C), g / cm3 carbon residue ,% by weight Elemental composition, % by weight 〇C/l Z Metal content, ppm > Four components, wt% Saturated hydrocarbon asphaltenes (C7 insolubles) Ni+V, ppm ° inch 201024400

's^ Feed B Comparative Example 6 Reaction zone I Hydrogenated tail oil D 30.0 0.9253 3.71 87.37 12.18 I 0.39 0.25 00 2.75 58.8 32.6 Ο) 00 〇 4.58 Feed E 70.0 0.9351 5.07 87,22 12.04 1 0.50 0.24 4.70 1- 5.70 52.4 35.8 10.6 <N 10.40 Example 6 Reaction zone I Catalytic cracking of heavy feedstock G 39.2 0.9580 9.76 87.68 11.64 0.74 0.27 8.80 , 10.80 38.7 43.3 15.9 1 Η 19.60 Reaction zone 氢化 Hydrogenated tail oil D 30.0 0.9253 3.71 87.37 12.18 0.39 0.25 1.83 2.75 58.8 32.6 Ο) Bu ^ 00 ο 4.58 Catalytic cracking light feedstock Η 30.8 0.9103 (N d 87.61 12.39 1 0.21 0.17 Feed A Comparative Example 5 Reaction zone I Hydrogenated tail oil C 20.0 0.9315 4.43 86.94 12.08 1 0.77 0.27 1.53 3.15 60.6 33.5 Bu ο 4.68 Feed Ε 80.0 0.9351 . 5.07 87.22 12.04 1 0.50 0.24 4.70 5.70 52.4 35.8 10.6 10.40 Example 5 Reaction zone I Catalytic cracking of heavy feedstock oil G 44.8 0.9580 9.76 87.68 11.64 1 0.74 0.27 8.80 10.80 38.7 43.3 15.9 19.60 Reaction District Π Hydrogenated tail oil C 20.0 0.9315 4.43 86.94 12.08 1 0.77 0.27 1.53 3.15 60.6 33.5 Bu inch Ο 4.68 Catalytic cracking Solution light feedstock Η 35.2 0.9103 〇87.61 12.39 1 0.21 0.17 Hydrogenation unit feed example catalytic cracking reaction zone feed stream name to total feed ratio, wt% density (20 ° C), g/cm3 residual carbon, wt% Elemental composition, wt% UX metal content, ppm 2 > Four components, wt% saturated hydrocarbon asphaltene (C7 unpainted) Ni+V, ppm one inch 201024400

G Feed B Comparative Example 7 Reaction zone I Hydrogenated tail oil D 30.0 ! 0.9253 3.71 , 87.37 12.18 0.39 0.25 ro 00 2.75 58.8 32.6 Ο) 〇〇〇 4.58 Feed E 70.0 0.9351 5.07 , 87.22 1- 12.04 0.50 0.24 4.70 5.70 52.4 35.8 10.6 10.40 Example 7 Reaction zone I Catalytic cracking of heavy feedstock G 39.2 | 0.9580 9.76 87.68 11.64 0.74 0.27 8.80 10.80 38.7 43.3 15.9 19.60 ; Heavy fraction of hydrogenated tailing oil D 18.3 0.9351 5.76 87.22 12.04 0.50 0.30 3.00 4.50 52.4 35.8 10.6 <N 7.50 reaction zone 轻 Light oil of hydrogenated tail oil D 11.7 0.9103 CN Ο __ 12.39 0.21 0. Π 68.7 27.7 r〇1—^ Catalytic cracking light feedstock Η 30.8 ; 0.9103 (Ν Ο 1_^_ 12.39 0.21 0.17 • Hydrogenation unit feed example catalytic cracking reaction zone feed stream name to total feed ratio, wt% density (2°C), g/cm3 carbon residue, wt% elemental composition, wt% bismuth metal content, Ppm % > Four components, wt% saturated hydrocarbon asphaltenes (C7 insolubles) Ni+V, ppm 201024400 Table 6_1

Hydrogenation unit feed feed A feed B Example Example 3 Comparative Example 3 Example 4 Comparative Example 4 Reaction zone Π Working conditions Reaction temperature, °c 550 540 (initial contact mixing) Reaction time, seconds 1.8 1.0 Operating agent oil Ratio 19.9 37.9 Reaction zone I Working conditions Reaction temperature, °c 640 640 580 582 (initial contact mixing) Difference difference Reaction time, seconds 1.1 3 1.5 2.6 Operating agent oil ratio * 10.8 5.8 Regeneration temperature, °c 713 713 713 713 Regeneration pressure (G), KPa 229.9 230.3 229.9 230.3 Total apparent refining ratio * 0.12 0.12 0.24 0.24 Total reaction time * 2.9 3 2.4 2.6 Total oil ratio* 7 7 5 5 Product distribution, weight % Acid gas 0.55 0.51 0.04 0.50 0.51 -0.01 dry gas 4.26 4.33 -0.07 4.00 4.10 -0.10 LPG 15.84 15.45 0.39 15.00 14.80 0.20 Stabilized gasoline 38.60 36.83 1.77 34.20 33.00 1.20 Diesel 27.85 27.50 0.35 33.10 31.00 2.10 Slurry 3.00 5.20 -2.20 4.00 7.09 -3.09 Coke 9.40 9.68 -0.28 8.70 9.00 -0.30 Loss 0.50 0.50 0.50 0.50 Total 100.00 100.00 100.00 100.00 Conversion rate, 1#% 69.15 67.30 1.85 62.90 61.91 0.99 Light oil yield, 66.45 64.33 2.12 67.30 64.00 3.30 Total liquid yield, f#% 82.29 79.78 2.51 82.30 78.80 3.50 Propylene yield, 4.80 4.50 0.30 4.50 4.30 0.20 *Note The operating agent oil ratio is the ratio of the mass of the catalyst to the feedstock oil in the specific reaction zone; the total agent oil ratio is the ratio of the catalyst of the entire reactor to the mass of the total feedstock oil; the total apparent refining ratio is the refining oil participating in the reaction. The ratio of (HCO) to the fresh catalytic cracking feed mass; the total reaction time is the sum of the reaction zone I and the helium time of the hydrocarbon oil in the riser reactor. 43 201024400 Table 6-2 Hydrogenation unit feed feed A feed B Example Example 5 Comparative Example 5 Example 6 Comparative Example 6 Reaction zone Π Working conditions Reaction temperature, °c 570 540 (initial contact mixing) Reaction time, Second 1.7 1.4 Operating agent oil ratio 13.2 9.9 Reaction zone I Working condition reaction temperature, °c 580 600 560 580 (initial contact mixing) Difference difference Reaction time, second 1 2.9 1.2 2.6 Operating agent oil ratio 15.6 15.3 Regeneration temperature, t 713 713 713 713 Regeneration pressure (G), KPa 229.9 230.3 229.9 230.3 Total apparent refining ratio 0.12 0.12 0.24 0.24 Total reaction time 2.7 2.9 2.6 2.6 Total oil ratio 7 7 6 6 Product distribution, weight % Acid gas 0.45 0.40 0.05 0.43 0.39 0.04 Dry gas 3.50 4.20 -0.70 3.10 3.90 -0.80 Liquefied petroleum gas 14.50 14.30 0.20 14.30 13.80 0.50 Stabilized gasoline 37.50 34.80 2.70 35.50 34.31 1.19 Diesel 31.05 31.00 0.05 33.10 31.00 2.10 Slurry 3.80 5.80 -2.00 4.50 7.40 -2.90 Coke 8.70 9.00 -0.30 8.57 8.70 -0.13 Loss 0.50 0.50 0.50 0.50 Sum 100.00 100.00 100.00 100.00 Conversion, wt% 65.15 63.20 1.95 62.40 61.60 0.80 Light oil yield, wt% 68.55 65.80 2.75 68.60 65.31 3.29 Total liquid yield, wt% 83.05 80.10 2.95 82.90 79.11 3.79 Propylene yield, wt% 4.20 4.00 0.20 4.00 3.70 0.30 44 201024400 Table 6-3 Hydrogenation unit feed feed B Example Example 7 Comparative Example 7 Reaction zone Π Working conditions Reaction temperature, °c 545 (initial contact mixing) Reaction time, seconds 1.4 Operating agent oil ratio 14 Reaction zone I working condition reaction temperature, °c 585 585 (initial contact mixing) difference reaction time, second 1.5 3 operating agent oil ratio 10.4 regeneration temperature, t 713 713 regeneration pressure (G), KPa 229.9 230.3 total apparent refinery Ratio 0.24 0.24 Total reaction time 2.9 3 Total oil ratio 6 6 Product distribution, weight % Acid gas 0.51 0.51 Dry gas 4.40 4.30 0.10 Liquefied petroleum gas 15.50 15.10 0.40 Stabilized gasoline 37.00 34.50 2.50 Diesel 30.00 29.00 1.00 Slurry 3.20 6.79 -3.59 Coke 8.89 9.30 -0.41 loss 0.50 0.50 sum 100.00 100.00 conversion rate, %% 66.80 64.21 2.59 Light oil yield, wt% 67.00 63.50 3.50 Total liquid yield, wt% 82.50 78.60 3.90 Propylene yield, wt% 4.70 4.35 0.35 45 201024400 The results given in Table 6-1 can be clearly stated The selectivity of gasoline and diesel in the product distribution obtained by the method provided by the invention is significantly improved compared to the direct introduction of hydrocarbon oil into the catalytic cracking reactor for conversion. For example, in Example 3 and Comparative Example 3, the raw material oil phase is the same, except that in Example 3, the smoke oil is separated by light pressure and two fractions, wherein the heavy fraction and the hydrogenated tail are separated under reduced pressure.

After the oil combination, the two different reaction zones of the catalytic cracking are respectively reacted. Comparing the results obtained by two different processing methods, the conversion rate of Example 3 increased by about 1.85 percentage points, the gasoline + diesel yield increased by 212 percentage points, the coke yield decreased by 0.28 percentage points, and the total liquid volume increased by 2.51. Percentage points. The slurry yield dropped by 2.20 percentage points, indicating that the heavy oil conversion capacity was significantly improved. Example 4 was the same as Comparative Example 4 processing stock oil, and the results obtained by two different processing methods were compared, wherein the conversion rate of Example 4 was increased by about 1%, the diesel yield was increased by 2.10%, and the gasoline yield was increased. 2 percentage points, coke yield decreased by 0.3 percentage points' total liquid volume increased by 35 percentage points. The results given in Table 6-2 clearly show that, compared with the direct introduction of hydrocarbon oil into the catalytic cracking reactor for conversion, the method for enhancing the conditioning of the second reaction zone provided by the present invention (introducing a high-temperature regenerant) is obtained. The selectivity of the product distribution in gasoline and diesel is significantly improved, while reducing the low-value product 'especially the reduction in dry gas yield' further increases the efficiency of catalytic cracking. For example, 'Example 5 is the same as the processing material oil of Comparative Example 5'. In Example 5, the hydrocarbon oil is separated by light pressure and light weight, and two of them are combined, and the light (four) is combined with the hydrogenated tail oil to respectively catalyze the cracking. The reaction is carried out in different reaction zones. Comparing the results obtained by two different methods of reinforcement, 46 201024400, wherein the conversion yield of Example 5 was increased by 2.75 hundred: the mouth was about "5 percentage points" gasoline + diesel point, and the total liquid volume was increased by 2_95 carbon yield. Reduced G.30 percentage points, dry gas yield decreased by 5%, product distribution benefit. Processing raw material oil is the same, compared with the results obtained by the same method in Example 6 and Comparative Example 6 It has a percentage point, =::: percentage points' diesel oil yield increase Ο m rate decreased by 0.U percentage points, H r19 percentage points, coke production" total liquid collection increased by 3.79 percentage points, dry gas yield decreased 〇.8(M@*' _, the knife pulp slurry yield decreased by 2.90 knife points' (IV) The heavy oil conversion capacity was obviously improved. The results given in Table 6-3 can be clearly stated, and the smoke will be directly Compared with the introduction of oil into catalytic cracking and anti-riding, the selectivity of gasoline and diesel in the product distribution obtained at a lower reaction temperature is significantly improved by using the method provided by the present invention. For example, Example 7 and Comparative Example 7 process feedstock oil. Same, different It is Example 7 Jiang Zugu, 丄1 J. All hydrocarbon oils are fractionally distilled into two fractions, light and heavy, under reduced pressure. Accordingly, the light and heavy fractions are respectively reacted in two different reaction zones of catalytic cracking. Comparing the results obtained by two different processing methods, the conversion rate of Example 7 in the pot increased by about 2.59 percentage points, the gasoline + diesel yield increased by 3.50 percentage points, the coke yield decreased by 41%, and the total liquid volume increased. 3.90 percentage points. The slurry yield decreased by 3. 2 percentage points, indicating that the heavy oil conversion capacity and gasoline yield were significantly improved. The hydrogenation treatment feed of Example 3 and Example 4, the hydrogenation tail oil accounted for the total feed ratio Different and catalytic cracking reaction conditions are different, and their product distributions are different from the reaction results*. Among them, the conversion rate of Example 3 is increased, 47 201024400 cracking products are more lighter, and the diesel oil yield of Example 4 is Significantly improved. This shows the change in the amount of catalytic cracking cycle oil (feedstock A and feedstock B) by varying the amount of hydrogenated tail oil to heavy fraction oil and the catalytic cracking reaction. In order to ensure the higher conversion rate of the feedstock oil, the product distribution in the produced oil can be modulated. Examples 5 and 6 are compared with the examples 3 and 4, and it is found that the catalyst participates in the reaction mode by adjusting the catalyst. In order to strengthen the operating conditions of different reaction zones, the yield of low-value products can be further reduced, and the conversion efficiency of the catalytic cracking device can be improved. Various changes and improvements can be made to the above embodiments. All such improvements and changes are desired to be included in the present invention. BRIEF DESCRIPTION OF THE DRAWINGS Figure 1 is a schematic flow diagram of an improved combination process for hydrocarbon oil hydrotreating and catalytic hydrazine cracking provided by the present invention. Figure 2 is a modified hydrocarbon provided by the present invention. Schematic diagram of the combined process of oil hydrotreating and catalytic cracking ^ /, Catalyst Figure 3 is a schematic flow diagram of a more flexible combination of hydrolyzed hydrocarbon oil hydrolyzed rhodium catalytic cracking provided by the present invention. "Car to component symbol description 1.. Filter; 2.. device; 3 · · separation, ^ ^ knife away from the device; 4 · · fractionation tower; 5. • settler; 6. Reactor; · Regenerator. ^ Dan Yi, 1〇·. Back to refinery; U• gas passage; 12·. Hydrogenated naphtha; &, 'Weathered diesel oil; Μ·. Hydrogenated tail oil; 48, 23. · 201024400 丨经; 15.. light distillate oil; 16. heavy distillate oil; 18, 22 19. gas; 20. catalytic gasoline; 21. catalytic diesel 5 24, 25 ·. Catalyst; 26.. regenerant; 31.. pipeline 40, 41.. feedstock oil

49

Claims (1)

201024400 VII. Scope of application: 1 · A modified combination of hydrocarbon oil deuteration treatment and catalytic cracking, including: Residue, catalytic cracking back to refinery and optional pavilions in the presence of hydrogen and hydrotreating conditions The oil is contacted with a hydrogenation catalyst to separate the reaction product to obtain a gas, hydrogenated naphtha, hydrogenated diesel oil and hydrogenated tail oil; e 纟 catalytic cracking reaction conditions, hydrazine hydrogenated tail oil and/or conventional catalytic crack = raw material, Contacting with a catalytic cracking catalyst, separating the reaction product to obtain dry gas, liquefied petroleum gas, catalytic pyrolysis gasoline, catalytic cracking diesel oil, and catalytic cracking back to refinery; characterized in that the contact reaction with the catalytic cracking catalyst is in the flow direction along the reactant In a reactor comprising at least two reaction zones ^ and π, Before contacting the hydrogenated tail oil and/or the conventional catalytic cracking feedstock oil with the catalyzing catalyst, the XI _ _ 虱 虱 虱 虱 虱 和 和 和 和 和 和 和 和 和 和 和 和 和 和 和 和 和 和 和 和 和 和 和 和 和Part of the step, ', the contact reaction with the catalytic cracking catalyst is to treat the hydrogenated tail oil> 知 _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ Optionally, the uncut hydrogenated tail oil, the conventional catalytic cracking feedstock oil, and/or the conventional catalytic cracking heavy feedstock oil, the second cracked light feedstock oil, are added to the reaction, and the hydrogenated tail is: :: another from the heavy library Optionally, with uncut hydrogenation tailings = chemical cracking feedstock oil and / or often · cracking heavy feedstock oil,: catalytic cracking light feedstock oil is added to the reaction zone π, often 50 201024400 or the catalytic cracking _ cleavage of heavy feedstock oil and conventional catalytic system: should - the conventional cleavage of chlorinated tail oil, conventional catalytic cracking feedstock oil: two optional and unparticulated, hydrogenated tail oil heavy library added to the reaction zone! Or hydrogenated tail oil light distillate 裂解 cracking heavy feedstock oil and conventional catalytic cracking light source, the conventional catalytic and uncut hydrogenated tail oil, conventional catalytic cracking raw material, optionally light library, hydrogenated tail oil heavy library added to the reaction Area ", in the tail oil raw material oil and the hydrogenation tail: the mixing of the two tail oil heavy parts, the hydrogen == parts, hydrogenation zero. ^ When the content of the tailing oil is different, it is 2, such as the application area No. 1 and the catalytic cracking catalyst re-feeding device. The method of the present invention, wherein the method of claim 2, wherein the regenerated catalyst delivery device is disposed at a position on the reaction zone π, is provided. The residence time of the hydrocarbon oil in the reaction zone 11 is not less than 0.2 seconds. 4. The method of claim 3, wherein the regenerated catalyst delivery device is disposed at a position on the reaction zone π such that the residence time of the hydrocarbon oil in the reaction zone 11 is not less than 1 second. 5. The method of claim 1, wherein the method 51 201024400 includes a step of removing catalytic cracking catalyst particles from the catalytic cracking back to the refinery, the step of catalytically cracking back into the refinery to catalytically crack the catalyst particles. The content is less than 30 wtppm and the particle size is less than 1 〇μπι. 6. The method of claim 5, wherein the catalytic cracking catalyst refining oil has a catalytic cracking catalyst particulate matter content of less than 15 wtppm and a particle size of less than 5 μιη. 7. The method of claim 5, wherein the method of removing catalytic cracking catalyst particles from the catalytic cracking back to the refinery is steaming and/or transitioning. 8. The method of claim 7, wherein the operating temperature in the filtering method is from 100 to 350. Hey. 9. The method of claim 8, wherein the operating temperature in the filtering method is from 2 〇〇 to 320. Hey. The method of claim 1, wherein the catalytic cracking back to the refining oil is one or a mixture of two or more of a heavy cycle oil, a decant oil or a total catalytic cracking cracking product heavy oil. 11. The method of claim 1, wherein the virtual hydrogenation catalyst is in contact with the reaction oil, catalytic cracking back to the refinery oil, and optionally 52 201024400 distillate oil to 'catalyze cracking back to the refined oil content It is 5-40 weight. /❶, preferably 6-30% by weight' more preferably 8-25% by weight. 12. The method according to claim 1, wherein the reaction zone I has a reaction temperature of 550-700 ° C, a ratio of the agent to the oil of 4 to 50, a reaction time of 0.5 to 10 seconds, and atomization. The water vapor accounts for 2-50% by weight of the feed amount, and the reaction pressure is atmospheric pressure - 300 kPa. Preferably, the reaction temperature of the reaction zone I is 560-650. 〇, Lu agent oil ratio of 7 - 2 0 'reaction time is 1-2 seconds, atomized water vapor accounts for 5-10% by weight of the feed amount, and the reaction pressure is 100-300 kPa. 13. The method of claim 1, wherein the reaction enthalpy has a reaction temperature of 500 to 600 ° C, a ratio of the agent to the oil of 3 to 50, and a reaction time of 0.2 to 8 seconds. The steam accounts for 2-20 parts by weight of the feed. /. The reaction pressure is atmospheric pressure -3 00 kPa, preferably the reaction temperature of the reaction zone is 5 1 〇-560, the ratio of the agent to the oil is 5-40, the reaction time is 0.5-1.5 seconds, and the atomized water vapor accounts for the feed β. The amount is 4-8 wt% and the reaction pressure is 100-300 kPa. 14. The method of claim 1, wherein the contacting reaction with the catalytic cracking catalyst is to add the nitriding tail oil heavy fraction and optionally uncut hydrogenated tail oil to reaction zone I. The hydrogenated tail oil is added to the reaction zone in a light portion. 15. The method of claim 14, wherein the light library comprises 丨〇_5〇% by weight of the total amount of hydrogenated tail oil; preferably the cutting causes the 53 201024400 light fraction to account for hydrogenation tail 20_45 weight of the total amount of oil. /. More preferably, the cutting is such that the portion of the lubricant accounts for 25 to 35 wt% of the total amount of the hydrogenated tail oil. 16. The method of claim 1, wherein the reaction conditions of the first reaction zone comprise: a reaction temperature of 550-70 (rc, a ratio of the agent to the oil of 5-20' is 〇5-1 〇 seconds, The atomized water vapor accounts for 2-50 parts of the feed amount, and the reaction pressure is atmospheric pressure _3 〇〇 kPa; preferably, the reverse φ condition of the first reaction zone includes: the temperature is 560-650. (3, the ratio of the agent to the oil is 7-16, The reaction time is 1 _2 seconds. The atomized water vapor accounts for 5-10% by weight of the feed amount, and the reaction pressure is 100-300 kPa. 17. The method according to claim 14, wherein The reaction conditions of the first reaction zone include: the temperature is 5〇〇_6〇〇. (:, the ratio of the agent to the oil is 7-20, and the reaction time is 0.2-8 seconds. 'Atomized water vapor accounts for 2_2〇 of the feed amount. % by weight, the reaction pressure is atmospheric pressure -300 kPa; preferably, the reaction conditions of the π-th reaction zone include: temperature 510-56 (TC, ratio of agent to oil 10-18, reaction time 〇5-1 5 seconds, atomized water The steam accounts for 4-8 wt% of the feed amount, and the reaction pressure is 1 〇〇 3 〇〇 kPa. 18. The method according to claim 2, wherein the catalytic cracking catalysis The contact reaction is carried out by adding the hydrogenated tail oil light fraction to reaction zone I, and adding the hydrogenated tail oil heavy fraction and optionally uncut hydrogenated tail oil to reaction zone π. 54 201024400 19. The method of claim 18, wherein the light injury accounts for 1 〇 _ 5 〇 by weight of the total amount of hydrazine tail oil; preferably, the cutting causes the light fraction to account for the total amount of hydrogenated tail oil. 20_45重量%; more preferably, the cleavage makes the light collateral account for 2 5 - 3 5 wt% of the total amount of the hydrogenated tail oil. 20. The method of claim 18, wherein the first reaction zone The reaction conditions include: the reaction temperature is 550-700. (:, the ratio of the agent to the oil is φ 5-20, the reaction time is 〇 5_1 〇 seconds, the atomized water vapor accounts for 2_5 〇 weight / 〇 of the feed amount, and the reaction pressure is The atmospheric pressure is _3〇〇 kPa; preferably, the reaction temperature of the reaction zone j is 560-6503⁄4, the ratio of the agent to the oil is 7_16, the reaction time is 5 seconds, and the atomized water vapor accounts for 5-10% by weight of the feed amount. The reaction pressure is 1〇〇_3〇〇 kPa. 21. The method according to claim 18, wherein the reaction of the first reaction zone The conditions include: the temperature is 500_600. 〇, the ratio of the agent to the oil is 7_2 〇, the reaction time is 0.2-8 seconds, the atomized water vapor accounts for 2_2 〇% by weight of the feed amount, and the reaction pressure is atmospheric pressure - 300 kPa; The reaction temperature in the π reaction zone is 52〇-5 60 C, the ratio of the agent to the oil is 1 〇-1, the reaction time is 1 _2 seconds, and the atomized water vapor accounts for 4-8 wt% of the feed amount. 22. The method of claim 18, wherein the regenerated catalyst is introduced in the reaction zone II. 23. The method of claim 1, wherein the contact reaction with the catalyzed 55 201024400 is to recycle the gasified tail oil and optionally the unhydrogenated tail oil and / or conventional catalytic cracking feedstock oil is added to reaction zone I' and the hydrogenated tail oil light fraction is added to reaction zone II. The method of claim 23, wherein the light (four) accounts for 1 G_5 Gwt% of the total amount of the hydrogenated tail oil; preferably, the cutting causes the boxing injury to account for 2q_45 wt% of the total amount of the hydrogenated tail oil; More preferably, the cutting is such that the hydrazine portion comprises from 25 to 35 parts by weight based on the total amount of the hydrogenated tail oil. /. . 25. The method of claim 23, wherein the reaction conditions of the reaction zone include: a reaction temperature of 550-70 (TC, a ratio of agent to oil of 5-20, a reaction time of 〇5_1 〇 seconds, fog) The steam content accounts for 25% by weight of the feed amount. The reaction pressure is atmospheric pressure _3 〇〇 kPa; preferably, the reaction conditions of the first reaction zone include: the temperature is 56 〇 _65 〇〇 c, and the ratio of the agent to the oil is 7_16, the reaction time is 1 _2 seconds 'the atomized water vapor accounts for 5-10% by weight of the feed amount, and the reaction pressure ❹ is 100-300 kPa. 26. The method according to claim 23, wherein the method The reaction conditions of the π reaction zone include: the temperature is 5〇〇-600° C., the ratio of the agent to the oil is 3-20, the reaction time is 0.2-8 seconds, and the atomized water vapor accounts for 2-20% by weight of the feed amount. The pressure is _3〇〇 kPa at normal pressure; preferably, the reaction conditions of the πth reaction zone include: temperature is 510-560. (:, ratio of agent to oil is 6-14, reaction time is 0.5-1.5 seconds) The method according to the fourth aspect of the invention, wherein the blood pressure is 4-8 wt% of the feed amount, and the reaction pressure is 100-300 kPa. The pyrolysis catalyst contact reaction is to add the hydrogenated tail oil to the reaction zone in the reaction zone of the hydrogenation tail oil and the catalytic cracking feedstock, and add the hydrogenated tail oil to the hydrogenation tail oil and optionally the unhydrogenated tail oil of the (four) The method of claim 27, wherein the method of claim 27, wherein the light salt injury accounts for 1 〇 5 〇 of the total amount of sputum tail oil, preferably the cutting makes the light The portion accounts for 2〇_45% by weight of the total amount of the hydrogenated tail oil; more preferably, the cutting is such that the light fraction accounts for 25-35 parts by weight of the total amount of the hydrogenated tail oil. The method wherein the reaction conditions of the reaction zone include: a reaction temperature of 55 〇 7 〇〇 〇, a ratio of the agent to the oil of 5, a reaction time of 0.5 〇 〇, and an atomized water vapor occupies the feed amount. 2_5〇 weight & pressure should be normal pressure _ kPa; preferably reaction zone ^ reactivity is 560 650 C, ratio of agent to oil is 7-16 'reaction time is 1-1.5 seconds, atomized water steaming π accounted for feed The amount of 5_1 〇% by weight, the reaction pressure is just - (10) kPa. The method described in Item 27, wherein the ηth temperature is 500-600 ° C, and the ratio of the agent to the oil is 7- 20, the atomized water vapor accounts for 2-20% by weight of the feed amount, 30. The reaction conditions of the patent application zone include: the reaction time is 0.2-8 seconds, and the reaction pressure is atmospheric pressure _3 〇〇. kPa; 520-560 C ' the ratio of oil to oil is ι〇_18. The reaction temperature of the first reaction zone is 'reaction time is 1 _2 seconds, atomized water 57 201024400 steam accounts for 1 2 3 4_8% by weight of feed amount, reaction pressure It is 100-300 kPa. The method of claim 27, wherein the regenerated catalyst is introduced in the reaction zone II. The method of claim 1, wherein the contacting reaction with the catalyzed catalyst is to recycle the hydrogenated tail oil, conventional hydrazine & cracking heavy feedstock oil and optionally uncut. The hydrogenated tail oil is added to the reaction zone! The hydrogenated tail oil light fraction and the conventional catalytic cracking light feedstock oil are added to the reaction zone II _ ^ 33. The method of claim 32, wherein the light fraction accounts for total hydrogenated tail oil. The amount of 1〇_5〇% by weight; preferably the cutting is such that the light fraction accounts for 2〇_45% by weight of the total amount of the hydrogenated tail oil; more preferably, the cutting causes the light fraction to account for the total hydrogenated tail oil The amount of 25_3 5 weight 〇乂. The method of claim 32, wherein the conventional catalytic cracking heavy feedstock oil is a hydrocarbon oil having a boiling point greater than 5 〇〇〇c, and the conventional catalytic cracking light feedstock oil has a distillation range of 3 5 〇. _ 5 〇〇 its hydrocarbon oil. 58 1 5. The method of claim 32, wherein the reaction conditions of the first anti-2 reaction zone comprise: a reaction temperature of 55 〇 7 〇 (rc, a ratio of the agent to the oil of 3 4-20, % of reaction) The ratio is 〇5_1〇 second, the atomized water vapor accounts for 2 5〇4% by weight of the feed amount, and the reaction pressure is atmospheric pressure _300 kPa; preferably the reverse reaction of the first reaction zone I 201024400 The conditions include: temperature 560_650° C, the ratio of the agent to the oil is 5_16, the reaction time is 1-2 seconds, 'the atomized water vapor accounts for 5_丨〇% by weight of the feed amount, and the reaction pressure is 100·300 kPa. 36. For the scope of claim 32 The method wherein the reaction conditions of the first reaction zone include: a temperature of 500_6〇〇t:, a ratio of the agent to the oil of 3_2〇, and a reaction time of 0.2-8 seconds. The atomized water vapor accounts for 2_2〇 of the feed amount. % , ❹ The reaction pressure is _30〇 kPa at normal pressure; preferably the reaction conditions in the third reaction zone include: temperature 510-56〇t:, ratio of agent to oil is 6-14, reaction time is 0.5-1.5 - sec' The atomized water vapor accounts for 12 to 8% by weight of the feed amount, and the reaction pressure is 100 to 300 kPa. 37. The method according to claim 1, The contact reaction with the catalytic cracking catalyst is carried out by adding the hydrogenated tail oil light column, conventional catalytic cracking heavy feed oil and optionally uncut hydrogenated tail oil to the reaction zone I' and the argonized tail oil The heavy fraction and the conventional catalytically cracked light feedstock oil are added to the reaction zone II. 59. The method of claim 37, wherein the light fraction accounts for 丨〇_5 of the total amount of the hydrogenated tail oil. % by weight; preferably the cutting is such that the 2 light parts account for 2% to 45% by weight of the total amount of the hydrogenated tail oil: more preferably the cutting is such that the portion of the hydrogenated tail oil is 25-33% by weight The proportion of the light-duty portion of the hydrogenated tail oil is at least greater than zero, and there is no maximum ratio. 201024400 39. The method described in claim 37 of the patent scope, the conventional catalytic cracking heavy feedstock oil described in I is greater than For hydrocarbon oils above C, the conventional catalytic cracking light feedstock oil is a hydrocarbon oil having a distillation range of 35 〇 5 〇 (rc). 4 〇 · The method described in claim 37, in the first reaction zone The reaction conditions include: the reaction temperature is 55 〇 _7 〇 (rc / ratio of oil to oil is 5-20, The time should be 5.5_1 〇 seconds 'Atomized steam accounts for 2 5 〇❿ 4 $ % of the feed amount. The reaction pressure is atmospheric pressure · kPa; preferably the reaction temperature of the reaction zone is 560-650 ° C, the agent The oil ratio is 7_16, the reaction time is 丨15 seconds, the atomized water vapor accounts for 510% by weight of the feed amount, and the reaction pressure is 100-300 kPa. 41. As described in claim 37 The method of the reaction zone of the 11th reaction zone comprises: a temperature of 500_6 〇 (rc, a ratio of the agent to the oil of 7 to 50, and a reaction time of 0.2 to 8 seconds). The atomized water vapor accounts for 2_2 〇 weight 〇/0 of the feed amount. The reaction reaction Lili is usually a thousand Pa; preferably, the reaction temperature of the third reaction zone is 520-560 ° C, the ratio of the agent to the oil is 8-40, the reaction time is 1_2 seconds, and the atomized water vapor accounts for 4 - 4 8 wt% 'reaction pressure is ι〇〇_3〇〇 kPa. 42. The method of claim 37, wherein the regenerated catalyst is introduced in the reaction zone II. 43. The method of claim 1, wherein the contacting with the catalytic cracking catalyst comprises adding a conventional catalytic cracking heavy feedstock oil and an uncut 60 201024400 cut hydrogenated tail oil to the reaction zone i, The conventional catalytic cracking light feedstock oil is added to the reaction zone. 44. The method of claim 43, wherein in the mixed feed of the conventional catalytically cracked heavy feedstock oil and hydrogenated tailstock, the hydrogenated tail oil is contained within 9 wt%, preferably hydrogenated tail The oil content is within 8 〇 weight%. 45. The method of claim 43, wherein the conventional catalytic cracking heavy feedstock oil is a hydrocarbon oil having a boiling point greater than 5 〇 (rc or more, and the conventional catalytic cracking light feedstock oil has a distillation range of 350-500 °c) The method of claim 43 wherein the reaction conditions of the first reaction zone comprise: a reaction temperature of 550-700. (:, the ratio of the agent to the oil is one sec. The atomized water vapor accounts for 22% by weight 'reaction pressure is normal pressure _ then kPa; preferably the reaction conditions of the first reaction zone include · · temperature is 5 teams 65 (rc, ratio of agent to oil is 5_16, reaction time is 1- 2 shifting 'atomized water vapor accounted for 5_ι% by weight of the feed amount, and the reaction pressure is 100-300 kPa. 47. The method described in claim 43, wherein the reaction conditions of the second reaction zone include ·, θ by or, including. The dish is 500-60 (rc, the ratio of the agent to the oil is 7_5 〇, the reaction time is 0.2 - 8 seconds, Lin Zuo ★ poor νίτ μ ^ I accounted for steam 2-20% by weight of the feed amount, the reaction dust force is atmospheric pressure _3 〇〇 kPa; the optimal reaction time is preferably the reaction condition of the third reaction zone. 201024400 Included. Temperature is 510-560 〇C 'The ratio of agent to oil is 8-40, the reaction time is 0.5-1.5 private, the atomized water vapor accounts for 4-8 wt% of the feed amount, and the reaction pressure is i〇〇_3〇〇 The method of claim 2, wherein the contacting with the catalytic cracking catalyst is carried out by adding the conventional catalytic cracking heavy feedstock oil and optionally a conventional catalytic cracking feedstock oil to the reaction zone! And the conventional catalytic cracking light feedstock oil is added to the reaction zone π, wherein the conventional catalytic cracking light feedstock oil and the uncut hydrogenated tail oil are added to the reaction zone π. In the mixed feed with the hydrogenated tail oil, the content of the hydrogenated tail oil is within 50% by weight, preferably the content of the hydrogenated tail oil is within 4% by weight. 50. The method of claim 48, wherein The conventional catalytic cracking heavy feedstock oil is a hydrocarbon oil having a boiling point of more than 5 〇〇〇c, and the conventional catalytic cracking light feedstock oil is a hydrocarbon oil having a distillation range of 35 〇 5 〇〇. 〇. The method described in the item, wherein the first The reaction conditions of the zone include: the reaction temperature is 55 〇 _7 〇〇 < t, the ratio of the agent to the oil is 4-20, the reaction time is 5. 5_1 〇 seconds, and the atomized water vapor accounts for the weight of the feed amount. The reaction pressure is atmospheric pressure _ then kPa; preferably, the reaction temperature of the reaction zone ι is 560-65 (TC' ratio of oil to oil is 5-16, reaction time is 丨$ second, 62 201024400 atomized water vapor accounts for 5 of the feed amount) -10% by weight, the reaction pressure is 100-300 kPa. 52. The method of claim 48, wherein the reaction conditions of the second reaction zone include: a temperature of 500-6001, a ratio of the agent to the oil of 7- 50, the reaction time is 〇·2-8 seconds, the atomized water vapor accounts for 2-20% by weight of the feed amount, the reaction pressure is atmospheric pressure _3〇〇 kPa; preferably the reaction temperature of the η reaction zone is Φ 520 -56 ° ° C, the ratio of agent to oil is 8_4 Torr, the reaction time is 1-2 seconds, the atomized water vapor accounts for 4-8 wt% of the feed amount, and the reaction pressure is $ kPa. ^ Method, in which, for example, A, please introduce the regenerative catalyst in the reaction zone II. ❹ 63