CN1896192A - Two-way combined process of wax-oil hydrogenation treatment and catalytic cracking - Google Patents
Two-way combined process of wax-oil hydrogenation treatment and catalytic cracking Download PDFInfo
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Abstract
A two-way combined process of wax oil hydro-process and catalytic crack is carried out by entering wax oil, catalytic cracking re-circulating oil and catalytic cracking diesel oil into hydro-processor, hydrogenation reacting under existence of hydrogen and hydrogenation catalyst, separating for reactant to obtain gas, hydrogenation naphtha oil, hydrogenation diesel oil and hydrogenation tail oil, entering hydrogenation tail oil into catalytic cracker, crack reacting under existence of catalytic cracking agent, separating to obtain dry gas, liquefied gas, catalytic cracking gasoline, catalytic cracking diesel oil and catalytic cracking re-circulating oil and oil slurry, and circulating for catalytic cracking diesel oil and catalytic cracking re-circulating oil to hydro-processor. It has higher recovery rate and cetyl value, less sulfur content, arene content and coke output.
Description
Technical field
The invention belongs to the combined technical method of handling hydrocarbon ils with other step of converting of a hydroprocessing technique process and, more particularly, is a kind of wax oil hydrogenation the processing and the method for two kinds of processing methodes combinations of catalytic cracking.
Background technology
At present the world is being faced with crude oil and becomes and heavily become bad trend, and people gradually reduce the demand of heavy fuel oil (HFO), and the demand of lightweight oil is then significantly increased.Therefore, how to utilize limited petroleum resources maximum to produce light-end products, the heavy oil lighting is one of gordian technique.The main technique of heavy oil lighting comprises hydrocracking, catalytic cracking and coking, and wherein hydrocracking is restricted its application because of investing factors such as height, process cost height and difficult processing vacuum residuum; Factors such as coking process is low because of liquid yield, poor product quality, not environmental protection of production process, application also is restricted; And catalytic cracking can be processed decompressed wax oil, vacuum residuum, and lightweight light-end products yield height, thereby obtains than widespread use.
But along with the enhancing of people's environmental consciousness, countries in the world have all proposed more strict requirement to the motor spirit specification.Wherein the gasoline products major requirement further reduces sulphur content and olefin(e) centent, simultaneously aromatic hydrocarbons and benzene content is limited; Diesel product then requires further to reduce sulphur content and aromaticity content, improves cetane value simultaneously.The catalytic cracking process product gasoline has high sulphur content and olefin(e) centent, and product diesel oil has high sulphur content and aromaticity content height, and cetane value is low, makes that directly satisfying dispatching from the factory of product requires to become more and more difficult.In order to solve the problem of catalytic gasoline and catalytic diesel oil quality, developed a lot of catalyzer, auxiliary agent and Technology, wherein catalytically cracked material hydrogenation preconditioning technique is a problem that solves the catalytic gasoline sulphur content preferably.Its aromaticity content, sulphur nitrogen content are minimized after the pre-treatment of catalytically cracked material hydrogenation, thereby improved the catalytic cracking transformation efficiency, can voluminous light-end products and reduced coke yield, quality product is improved significantly simultaneously, and the wherein reduction significantly of the sulphur content in the gasoline products, content of olefin in gasoline and diesel cetane-number all make moderate progress.Therefore, the technology as catalytically cracked material after wax oil hydrogenation is handled obtains more and more general application.
In the whole bag of tricks of decompressed wax oil lighting, wax oil hydrogenation-catalytic cracking combined technique is a kind of good method.Wax oil removes impurity such as most sulphur, nitrogen after hydrotreatment, and saturated part aromatic hydrocarbons, improved hydrogen richness, reduce aromaticity content and sulphur nitrogen content, thereby improved catalytic cracking transformation efficiency, voluminous light-end products, produced coke less, and quality product is improved, and the sulphur content in the gasoline products reduces significantly, and content of olefin in gasoline and diesel cetane-number all make moderate progress.Simultaneously, the low-sulfur diesel-oil of by-product about 15% has improved the diesel and gasoline ratio of full factory in the wax oil hydrogenation treating processes.Therefore, the technology as catalytically cracked material after wax oil hydrogenation is handled obtains more and more general application.
Conventional wax oil hydrogenation processings-catalytic cracking process is that heavy cycle oil is circulated to further processing in the catalytic cracking unit, and catalytic diesel oil goes out behind the device independent or be mixed into diesel hydrotreating unit with straight-run diesel oil and further handle.Because heavy cycle oil mainly is made up of polycyclic aromatic hydrocarbons, its sulphur of while, nitrogen content higher (exceeding more than a times than raw material approximately), after catalytic cracking, produce 1/3rd gas, 1/3rd gasoline and diesel oil, 1/3rd coke approximately, the green coke amount is big, increase the revivifier load, reduced the treatment capacity and the economic benefit of oily catalytic cracking unit.Catalytic diesel oil aromaticity content height generally more than 50%, even reaches 80%, and cetane value is low, stability is poor, sulphur content height, colour-difference, is difficult to directly dispatch from the factory, and needs through further hydrotreatment.
US6,565,739 disclose the combination process of a kind of two-stage catalytic cracking and hydrotreatment.This method be the heavy cycle oil of first stage catalytic cracking after hydrotreatment, enter the second stage catalytic cracking device and carry out cracking, two-stage catalytic cracking adopts dissimilar catalyzer at different material.But this method need be with the independent hydrotreatment of heavy cycle oil, and it is a lot of to increase plant investment, and only solves the high problem of catalytic cracking unit coke yield, little to the quality product increase rate.
US6,123,830 disclose the combination process of a kind of two-stage catalytic cracking and two hydrotreatments.Stock oil obtains first hydrogenation tail oil at first through first hydrotreater; First hydrogenation tail oil enters first catalytic cracking unit, obtains petroleum naphtha, diesel oil and heavy oil; First catalysis heavy oil enters second hydrotreater and carries out hydrogenation (its hydrogen dividing potential drop will be higher than first hydrogenation unit), obtains second hydrogenation tail oil, and the part tail oil is delivered to first hydrotreater again and carried out hydrogenation; Second hydrogenation tail oil to the second catalytic cracking unit carried out cracking.This combination process is comparatively complicated, comprises two hydrotreaters and two catalytic cracking unit, and long flow path, complicated operation are invested too high.
US5,770,044 disclose the combination process of a kind of catalytic cracking and hydrotreatment.This method is: fresh feed separates obtaining gas, petroleum naphtha and heavier product (comprising diesel oil and heavy cycle oil) after catalytic cracking; After heavier product enters a hydrotreater, separate obtaining petroleum naphtha, diesel oil and hydrogenation tail oil; Catalytic cracking unit is returned in hydrogenation tail oil recirculation.This combination process has solved the problem of coke yield height, diesel quality difference preferably, but need set up hydrogenation unit separately, and does not solve the high problem of catalytic gasoline sulphur content.
US4,713,221 disclose the combination process of a kind of residual hydrogenation and catalytic cracking.This method is: fresh feed separates obtaining gas, light-end products and heavier product (comprising decompressed wax oil and vacuum residuum) after hydrotreatment; Decompressed wax oil and vacuum residuum separately or mix and enter two cover catalytic cracking unit respectively, the heavy cycle oil recirculation of two cover catalytic cracking unit are returned hydrotreater and are carried out hydrogenation.The advantage of this method is that heavy catalytic cycle oil has been carried out hydrotreatment, has improved the product distribution, has reduced coke yield.But this method is not handled catalytic diesel oil.
CN1119397C has disclosed a kind of hydrogenation and catalystic cracking combined process for residual oil, and in this method, residual oil and clarified oil enter the residual hydrocracking device together, carry out hydrogenation reaction in the presence of hydrogen and hydrogenation catalyst; The hydrogenated residue of reaction gained enters catalytic cracking unit, carries out cracking reaction in the presence of cracking catalyst, and heavy cycle oil circulates in catalytic cracking unit inside; The slurry oil of reaction gained obtains clarified oil through the separator separation, is back to hydrogenation unit.But slurry oil enters the residual hydrocracking device, and the easy green coke thing in the slurry oil will increase the carbon deposit of hydrogenation catalyst, has reduced the activity and the operational cycle of hydrogenation catalyst, and heavy cycle oil is at the catalytic cracking unit internal recycle.Therefore, this method is quite limited to reducing coke yield, improving the quality of products.
Summary of the invention
The objective of the invention is on the prior art basis, to provide a kind of wax oil hydrogenation to handle and the catalytic cracking two-way combined process.
Method provided by the invention comprises:
Wax oil and heavy catalytic cycle oil, catalytic cracking diesel oil enter hydrotreater together, carry out hydrogenation reaction in the presence of hydrogen and hydrogenation catalyst, and reaction product isolated obtains gas, hydrotreated naphtha, hydrogenated diesel oil and hydrogenation tail oil; Wherein hydrogenation tail oil enters catalytic cracking unit, in the presence of catalytic cracking catalyst, carry out cracking reaction, obtain dry gas, liquefied gas, catalytically cracked gasoline, catalytic cracking diesel oil, heavy catalytic cycle oil and slurry oil after separating, wherein catalytic cracking diesel oil and heavy catalytic cycle oil are circulated to hydrotreater.
Method provided by the invention improves the yield of light oil, reduces the sulphur content in the gasoline, reduces the aromaticity content of diesel oil and improves its cetane value.
Description of drawings
Accompanying drawing is that wax oil hydrogenation provided by the invention is handled and catalytic cracking two-way combined process synoptic diagram.
Embodiment
Respectively hydrotreatment and two steps of catalytic cracking are launched respectively to describe below.
(1), hydrotreatment
Wax oil of the present invention is the straight run decompressed wax oil or/and wax tailings, and its boiling spread is 350 ℃～540 ℃.
Typical wax oil hydrogenation processing condition are: hydrogen dividing potential drop 3.0～12.0MPa, 330～450 ℃ of temperature of reaction, volume space velocity 0.1～3.0 hour
-1, hydrogen and stock oil volume ratio (hereinafter to be referred as hydrogen-oil ratio) 350～2000.The stock oil here is meant decompressed wax oil, heavy catalytic cycle oil and catalytic cracking diesel oil, and wherein heavy catalytic cycle oil accounts for 3～30 heavy % of Wax Oil Hydrogenation Unit combined feed total feed, and catalytic cracking diesel oil accounts for 3～30 heavy % of hydrogenation unit combined feed total feed.
Described hydrogenation catalyst can be the strong hydrogenation catalyst of a kind of aromatic hydrocarbons saturability, and its active metal component is nickel-tungsten or nickel-molybdenum, and carrier is aluminum oxide, silicon-dioxide or amorphous aluminum silicide, and wherein aluminum oxide is the most frequently used carrier.If have higher metal content or carbon residue higher or the coking precursor amounts is higher in the raw material; in order to protect Primary Catalysts and to prolong running period; can be before Primary Catalysts contacts raw material the placement part guard catalyst, its ratio is 10～30 volume % of Primary Catalysts.
The wax oil hydrogenation type of reactor is a fixed bed, and hydrogenation unit comprises a reactor and a separation column at least.Gas in the hydrotreatment products can be used as hydrogen feedstock or sneaks in the refinery gas, hydrotreated naphtha can be used as reformer feed, hydrogenated diesel oil is ideal low-sulfur, high hexadecane value diesel product or blending component, the boiling spread of hydrogenation wax oil is＞370 ℃, can be all as the charging of catalytic cracking unit.
(2), catalytic cracking
Catalytic cracking unit can be that every covering device should comprise a reactor, a revivifier and a separation column at least more than a cover or overlapped.
Described catalytic cracking catalyst is REY, REHY, ZSM-5 molecular sieve catalyst or mixture, processing condition are: the weight ratio (hereinafter to be referred as agent-oil ratio) 3～10 of 470～570 ℃ of temperature of reaction, 0.5～5 second reaction times, catalyzer and stock oil, 650～800 ℃ of regeneration temperatures, the stock oil here is meant hydrogenation tail oil (be called for short HT-VGO), its boiling spread is＞and 370 ℃.
Gasoline in the catalytic cracking production is ideal low-sulfur, high octane gasoline products or blending component, and its olefin(e) centent is also than low about 10 percentage points of conventional catalytically cracked gasoline; Catalytic cracking diesel oil and heavy catalytic cycle oil are put circulation and are entered Wax Oil Hydrogenation Unit and further handle.
Heavy catalytic cycle oil aromaticity content height, and mainly be polycyclic aromatic hydrocarbons, its sulphur content and nitrogen content also double above than catalytic cracking unit charging, but its boiling range scope and decompressed wax oil are basic identical.If the heavy catalytic cycle oil deep hydrogenation is saturated, need higher pressure, and need to consume a large amount of hydrogen, but increase few to the raising of catalytic cracking transformation efficiency and the improvement of quality product after the advanced treatment.Decompressed wax oil and heavy catalytic cycle oil hydrotreatment are to the polycyclic aromatic hydrocarbons fractional saturation, rather than the degree of depth is saturated to naphthenic hydrocarbon, and such operation scheme helps reducing plant investment and process cost.Catalytic cracking diesel oil also has high aromaticity content, generally weighs more than the % 50, even reaches 80 heavy %, and the composition of its aromatic hydrocarbons mainly is a di pah, secondly is mononuclear aromatics, and three rings or the aromatic hydrocarbons more than three rings are seldom.If reduce aromatic hydrocarbons significantly and improve cetane value, need higher hydrogen dividing potential drop just can meet the demands, but catalytic cracking diesel oil is relative and decompressed wax oil cut boiling range is lighter, and aromatic hydrocarbons mainly is monocycle and two rings by hydrotreatment.Therefore, decompressed wax oil, heavy catalytic cycle oil and catalytic cracking diesel oil are mixed, under the catalyst treatment of elevated pressures and the saturated performance of high aromatic hydrocarbons (base metal), the aromatic hydrocarbons that can reach the diesel oil distillate higher degree is saturated, the purpose of raising cetane value, decompressed wax oil reaches (comprising heavy cycle oil) the polycyclic aromatic hydrocarbons fractional saturation of higher degree, the purpose of reduction polycyclic aromatic hydrocarbon content simultaneously, thereby obtains high-quality diesel oil and low-sulfur, low nitrogen and the higher catalytically cracked material of aromatic hydrocarbons degree of saturation.
Below in conjunction with accompanying drawing method provided by the present invention is further detailed, but does not therefore limit the present invention.
Accompanying drawing is that wax oil hydrogenation provided by the invention is handled and catalytic cracking two-way combined process synoptic diagram, has omitted the equipment of many necessity among the figure, as process furnace, pump etc.
Flow process is described in detail as follows:
Wax oil through pipeline 1 and from the catalytic cracking diesel oil of pipeline 23 with the mixture of heavy catalytic cycle oil after feedstock pump boosts to reaction pressure, mix with hydrogen-rich gas from pipeline 2, enter hydrotreating reactor 4, by contacting with the hydrotreating catalyst bed, remove impurity such as metal in the stock oil, sulphur and nitrogen, in desulfurization, denitrogenation, generation aromatic hydrocarbons is saturated, alkene is saturated and mild cracking.Because hydrotreatment is a strong exothermal reaction, need in the middle of reactor bed, to introduce cold hydrogen, control reaction temperature and temperature rise through pipeline 3.Hydrotreating reactor 4 outlet effluents enter high-pressure separator 6 through pipeline 5 to be separated, isolated gaseous stream enters that recycle compressor 9 boosts after pipeline 2 is recycled to the hydrotreating reactor inlet, isolated liquid phase stream arrives light pressure separator 7 more further to be separated, isolated liquid phase stream enters the separation column 10 of hydrotreater through pipeline 8, isolate gas at separation column, petroleum naphtha, diesel oil and hydrogenation tail oil, gas wherein, petroleum naphtha, diesel oil is respectively through pipeline 11,12,13 caterpillars, hydrogenation tail oil then enter the reactive system 15 of catalytic cracking unit through pipeline 14.
Enter the reactive system 15 of catalytic cracking unit from the hydrogenation tail oil of pipeline 14, on catalytic cracking catalyst, react, reacted oil gas logistics enters the separation column 17 of catalytic unit through pipeline 16, isolate gas, catalytically cracked gasoline, catalytic cracking diesel oil, heavy catalytic cycle oil and slurry oil, gas wherein, catalytically cracked gasoline, slurry oil is respectively through pipeline 18,19,22 draw, the slurry oil amount seldom, and contain more solid particulate, go out catalytic cracking unit or loop back catalytic cracking unit and all can, catalytic cracking diesel oil, heavy catalytic cycle oil is respectively through pipeline 20,21 draw mixing after, be recycled to hydrotreating reactor through pipeline 23.
The invention has the advantages that:
1, at the decompressed wax oil hydrotreater with catalytic cracking unit catalytic diesel oil and heavy cycle oil combination treatment, after the high hydrotreating catalyst of middle pressure and the saturated performance of aromatic hydrocarbons is handled, can reduce the aromaticity content of catalytic diesel oil significantly, improve cetane value, produce fine low-sulfur, high hexadecane value diesel oil or blend component, with the polycyclic aromatic hydrocarbons fractional saturation of decompressed wax oil (comprising heavy cycle oil), reduce the sulphur nitrogen content simultaneously, produce the fine catalytically cracked material;
2, decompressed wax oil and heavy cycle oil can reduce sulphur content behind hydrogenation, thereby can reduce the sulphur content in the catalytically cracked gasoline, satisfy sulfur in gasoline content and are strict with; Can increase its saturation ratio and hydrogen richness behind decompressed wax oil and the heavy cycle oil hydrogenation, reduce nitrogen content, effectively improve the yield (the yield sum that refers to liquefied gas, gasoline and diesel oil) of catalytic cracking unit light oil; Reduce simultaneously the green coke amount significantly, improve the treatment capacity of catalytic cracking unit;
3, there is certain hydrocracking reaction in the hydrotreatment process, increased diesel yield, reduced the inlet amount of catalytic cracking unit, improved the diesel and gasoline ratio of full factory;
4, the reduction significantly of sulphur content in the catalytically cracked material has reduced the corrosion of catalytic cracking unit, has reduced the SOx discharging, and the reduction of green coke amount has also reduced CO
2Discharging, reduced environmental pollution.
The following examples will give further instruction to method provided by the invention, but not thereby limiting the invention.Employed stock oil is the straight run decompressed wax oil in embodiment and the Comparative Examples, and its character is listed in table 1.The decompressed wax oil hydropyrolysis experiment carries out in reactor, filling hydrogenation protecting agent and hydrotreating catalyst, the two ratio is 10: 90, the trade names of wherein hydrogenation protecting agent, hydrotreating catalyst are respectively RG-1 and RN-2, produce by Changling Refinery Chemical Industry Co., Ltd. of China Petrochemical Industry catalyst plant; Embodiment is identical with employed cracking catalyst in the Comparative Examples, is the catalyst plant production of Lanzhou branch office of group of CNPC, and trade names are LV-23.
Comparative Examples
This Comparative Examples adopts conventional wax oil hydrogenation processing-catalyst cracking method, i.e. the raw material of hydrotreatment is the straight run decompressed wax oil, and the raw material of catalytic cracking is the hydrogenation wax oil, and heavy catalytic cycle oil is handled at the catalytic cracking unit internal recycle.Table 2～table 4 is respectively processing condition, product distributes and main products character.
Embodiment
This embodiment adopts wax oil hydrogenation provided by the invention to handle and the catalytic cracking two-way combined process, and catalytic cracking diesel oil and heavy catalytic cycle oil are circulated to further processing in the hydrotreater.Table 2,3,5 is respectively processing condition, product distributes and main products character.
Comparing result shows, after catalytic cracking diesel oil and heavy catalytic cycle oil and the processing of straight run decompressed wax oil mixed hydrogenation, two covering devices add up to can increase by 0.8 percentage point in gasoline (comprising hydrotreated naphtha), diesel yield increases by 5.3 percentage points, gas reduces by 0.6 percentage point, liquefied gas reduces by 2.0 percentage points, coke reduces nearly 3 percentage points, improved the product distribution significantly, the quality product of catalytic cracking diesel oil increases substantially simultaneously, satisfy the requirement of low-sulfur, high hexadecane value, catalysis catalytic gasoline sulphur content further reduces.
Table 1, stock oil character
| Density (20 ℃), g/cm 3 | 0.9235 |
| S，m％ | 3.1 |
| N，ppm | 898 |
| Carbon residue, m% | 0.23 |
| Boiling range (D-1160), ℃ | |
| 10％/50％ | 379/446 |
| 95%/do | 528/553 |
Table 2, hydrotreatment and catalytic cracking process condition
| Comparative Examples | Embodiment | |
| The hydroprocessing technique condition | ||
| Raw material | Fresh feed | Fresh feed+heavy cycle oil+urge bavin |
| The hydrogen dividing potential drop, MPa | 8.0 | 8.0 |
| Temperature of reaction, ℃ | 380 | 380 |
| *Volume space velocity, h -1 | 1.0 | 1.0 |
| Hydrogen-oil ratio | 500 | 500 |
| The catalytic cracking process condition | ||
| Raw material | The hydrogenation wax oil | Hydrogenation wax oil+hydrogenation heavy cycle oil |
| Temperature of reaction, ℃ | 500 | 500 |
| *Agent-oil ratio | 5 | 5 |
*Calculate with the device inlet amount.
Table 3, product distribute
| Comparative Examples | Embodiment | |
| *The hydrotreatment product distributes: m% | ||
| Chemistry hydrogen consumption | 0.72 | 1.02 |
| Gas | 3.84 | 3.36 |
| Petroleum naphtha | 1.45 | 1.66 |
| Diesel oil | 18.25 | 29.98 |
| Hydrogenation tail oil | 77.18 | 66.10 |
| *The catalytic cracking product distributes: m% | ||
| Dry gas | 2.40 | 1.35 |
| Liquefied gas | 19.10 | 16.3 |
| Gasoline | 57.03 | 56.39 |
| Diesel oil | 15.50 | 12.55 |
| Heavy cycle oil | 0 | 11.3 |
| Coke | 5.97 | 2.11 |
| **Two covering devices add up to, m% | ||
| Chemistry hydrogen consumption | 0.72 | 1.21 |
| Dry gas | 5.65 | 5.04 |
| Liquefied gas | 14.75 | 12.75 |
| Gasoline (comprising hydrotreated naphtha) | 45.49 | 46.24 |
| Diesel oil | 30.22 | 35.53 |
| Coke | 4.61 | 1.65 |
*With the device inlet amount is 100% calculating,
*With fresh feed is 100% calculating.
Table 4, conventional wax oil hydrogenation-catalytic cracking main products character
*
| The hydrotreatment part | The catalytic cracking part | ||||
| Product | Diesel oil | Wax oil | Gasoline | Diesel oil | Heavy cycle oil |
| Density, g/cm 3 | 0.870 | 0.881 | 0.739 | 0.952 | 1.004 |
| S，ppm | 200 | 500 | 30 | 1000 | 2500 |
| Condensation point, ℃ | -2 | 35 | / | ＜-35 | -12 |
| Aromatic hydrocarbons, w% | 35 | / | 22 | 82 | / |
| Cetane value | 49 | / | / | 23 | / |
| RON/MON | / | / | 90/80 | / | / |
*Wherein hydrogenation wax oil, heavy catalytic cycle oil are intermediates.
Table 5, main products character of the present invention
*
| The hydrotreatment part | The catalytic cracking part | ||||
| Product | Diesel oil | Wax oil | Gasoline | Diesel oil | Heavy cycle oil |
| Density, g/cm 3 | 0.873 | 0.885 | 0.737 | 0.948 | 0.975 |
| S，ppm | 150 | 430 | 27 | 850 | 2000 |
| Condensation point, ℃ | -2 | 33 | / | ＜-35 | -6 |
| Aromatic hydrocarbons, w% | 38 | / | 20 | 78 | / |
| Cetane value | 47 | / | / | 25 | / |
| RON/MON | / | / | 90/80 | / | / |
*Wherein hydrogenation wax oil, catalytic cracking diesel oil and heavy catalytic cycle oil are intermediates.
Claims (7)
1, a kind of wax oil hydrogenation is handled and the catalytic cracking two-way combined process, it is characterized in that wax oil and heavy catalytic cycle oil, catalytic cracking diesel oil enter hydrotreater together, carry out hydrogenation reaction in the presence of hydrogen and hydrogenation catalyst, reaction product isolated obtains gas, hydrotreated naphtha, hydrogenated diesel oil and hydrogenation tail oil; Wherein hydrogenation tail oil enters catalytic cracking unit, in the presence of catalytic cracking catalyst, carry out cracking reaction, obtain dry gas, liquefied gas, catalytically cracked gasoline, catalytic cracking diesel oil, heavy catalytic cycle oil and slurry oil after separating, wherein catalytic cracking diesel oil and heavy catalytic cycle oil are circulated to hydrotreater.
2, according to the method for claim 1, it is characterized in that described wax oil is the straight run decompressed wax oil or/and wax tailings, its boiling spread is 350 ℃～540 ℃.
3, according to the method for claim 1, it is characterized in that the wax oil hydrogenation processing condition are: hydrogen dividing potential drop 3.0～12.0MPa, 330～450 ℃ of temperature of reaction, volume space velocity 0.1～3.0 hour
-1, hydrogen and stock oil volume ratio 350～2000.
4, according to the method for claim 1, the stock oil that it is characterized in that wax oil hydrogenation is meant decompressed wax oil, heavy catalytic cycle oil and catalytic cracking diesel oil, wherein heavy catalytic cycle oil accounts for 3～30 heavy % of Wax Oil Hydrogenation Unit combined feed total feed, and catalytic cracking diesel oil accounts for 3～30 heavy % of hydrogenation unit combined feed total feed.
5, according to the method for claim 1, it is characterized in that described activity of hydrocatalyst metal component is nickel-tungsten or nickel-molybdenum, carrier is aluminum oxide, silicon-dioxide or amorphous aluminum silicide.
6,, it is characterized in that described catalytic cracking catalyst is REY, REHY, ZSM-5 molecular sieve catalyst or mixture according to the method for claim 1.
7, according to the method for claim 1, it is characterized in that the catalytic cracking process condition is: the weight ratio 3～10 of 470～570 ℃ of temperature of reaction, 0.5～5 second reaction times, catalyzer and stock oil, 650～800 ℃ of regeneration temperatures.
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