CN102453509B - Catalytic conversion method for hydrocarbon oil - Google Patents
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Abstract
The invention discloses a catalytic conversion method for hydrocarbon oil. The method comprises the following steps of: introducing a preheated heavy hydrocarbon oil raw material into a first lifting pipe reactor from a bottom; undergoing a contact reaction with a catalyst, making a reaction product flow upwards; introducing reaction oil gas and a spent catalyst into an oil-agent separating system from an upper outlet for separating; stripping the separated spent catalyst, regenerating and returning to the reactor for recycling; introducing separated reaction oil gas into a main fractionating tower; extracting a part of circulating oil on the top of the main fractionating tower, and introducing into a second lifting pipe for freshening; and mixing reaction oil gas separated from the outlet of a second lifting pipe reactor with reaction oil gas of the first lifting pipe reactor, and entering a subsequent separating system for further separating to obtain a product. Due to the adoption of the method provided by the invention, the yield of petroleum can be increased by 3-10 percent, the yield of liquefied gas is increased by 0.5-3 percent, the olefin content of petroleum is lowered by 5-20 percent, the RON (Research Octane Number) of petroleum is increased by 0.2-2 units, and the yield of low-quality catalyzed diesel oil is lowered.
Description
Technical field
The present invention relates to the method for the catalyzed conversion of hydrocarbon ils under the condition that does not have hydrogen, more particularly, is the catalysis conversion method of a kind of hydrocarbon ils on duo-lift tube reactor.
Background technology
Along with the growth of Chinese national economy and increasing sharply of automobile pollution, recent year Oil Product Market significantly promotes the demand of gasoline and the demand of diesel oil is declined to some extent, increases gasoline output and has become one of matter of utmost importance that oil refining enterprise faces.Simultaneously, the problem that cleans of gasoline products has also become one of important environmental protection index in oil refining enterprise, the EU Council of Ministers had been promoted Euro V emissions within the scope of European Union last year, respective gasoline product sulphur content should be controlled in 10ppm, olefin(e) centent is less than 18 volume %, and within the scope of European Union in 2014, promotes more strict Europe VI emission standard; Within domestic 2007, play the state III emission standard of popularizing in an all-round way with reference to EUROIII Emission Standard, and the experimental cities such as Beijing, Shanghai, Guangzhou have started to promote state IV emission standard.
Catalytic cracking is one of important technical of heavy oil lighting, and domestic plant catalytic stable gasoline proportion in product gasoline pond surpasses 70%, and catalytic diesel oil also surpasses 20% to the contribution of product diesel oil.Therefore, to the optimization of the structure of catalytic cracking unit and operation be adjust vapour bavin and liquefied gas product structure and improve one of main method of gasoline octane rating.
For new demands such as Oil Product Market product structure and gasoline cleaning indexs, adopt double lifting leg to carry out the technical development of hydrocarbon oil catalytic conversion very fast.General, on main riser tube, carry out the catalytic cracking of heavy hydrocarbon oil; On another riser tube, carry out the freshening of gasoline upgrading and conversion or various diesel oil distillates.
CN1069054A discloses a kind of adaptable multieffect catalyst cracking method (FDFCC), and the light benzine cut hydrocarbon ils such as the first riser tube processing catalysis raw gasline, coker gasoline and reforming raffinate oil carry out passivation to the metal pollutant on catalyzer simultaneously; The second riser tube processing heavy hydrocarbon oil.The method can be increased production C
2-C
4alkene, metal pollutant on the regenerated catalyst of passivation simultaneously.But owing to relating to the again cracking reaction of each gasoline fraction in riser reactor, total gasoline yield is subject to suitable impact.
CN1302843A discloses a kind of two-stage riser fluid catalytic cracking technology (TSRFCC), raw material and catalyzer carry out short period of time catalytic cracking reaction in the first riser tube, oil gas enters the second riser tube after separation, half reclaimable catalyst enters revivifier coke burning regeneration, regenerated catalyst after regeneration contacts and carries out catalytic cracking reaction at the second riser tube with the isolated oil gas of the first riser tube, isolates spent agent and enters revivifier regeneration.The method realizes the object of oil gas series connection, catalyzer relay, segmentation reaction, Reaction time shorten and raising catalyzer average behaviour, reaches reduction alkene, increases isoparaffin and aromatic hydrocarbons, improves gasoline octane rating texts.But the related scrap build of the method is more complicated, actually operating stability needs to be investigated; Because the first riser tube does not have complete stripping sedimentation structure, the incomplete steam stripped oil gas of part enters revivifier, and in addition, catalyst recirculation amount increases, the phenomenon that causes coke yield to raise on apparent, and plant energy consumption integral body increases to some extent.
CN1458227A discloses a kind of gasoline subsidiary riser and has fallen olefin process, in the original conventional condensing cooling system of separation column, set up B-grade condensation cooling system, for separating of the lighting end that goes out raw gasline, and it is carried out to olefine reducing modification in auxiliary upgrading lifting gear, reach the environmental requirement that reduces alkene in gasoline.But the method relates to two kinds of different catalysts systems, operation relative complex; Due to part raw gasline is carried out to freshening upgrading, gasoline yield is subject to corresponding impact; Because olefin(e) centent in product gasoline declines, without corresponding octane value recovering measure, gasoline octane rating can be subject to certain influence.
In prior art, duo-lift tube reactor hydrocarbon oil catalytic conversion technology is mainly carried out freshening and the upgrading of the light hydrocarbon oils such as gasoline fraction in auxiliary (second) riser tube, all can reduce to a certain extent catalytic unit yield of gasoline; And olefin(e) centent reduction may cause degradation problem under gasoline octane rating in product gasoline.How when improving yield of gasoline, to reduce content of olefin in gasoline, and improve gasoline octane rating, become one of Important Problems of those skilled in the art's care.
Summary of the invention
The technical problem to be solved in the present invention is on prior art basis, a kind of raising yield of gasoline is provided, reduces content of olefin in gasoline, does not lose the catalytic conversion method of hydrocarbon oil of gasoline octane rating simultaneously.
A kind of catalytic conversion method of hydrocarbon oil, catalytic cracking unit comprises the first riser reactor and the second riser reactor, heavy hydrocarbon oil raw material after preheating is introduced to the first riser reactor by bottom, contact with the high-temperature regenerated catalyst coming from revivifier, under catalytic cracking reaction condition, react and make progress and flow, it is separated that reaction oil gas and reclaimable catalyst enter finish separation system by the outlet of riser reactor top, isolated reclaimable catalyst is through stripping, after regeneration, Returning reactor recycles, isolated reaction oil gas is introduced main fractionating tower, a part for main fractionating tower top turning oil is extracted out, by bottom, introduce and in the second riser reactor, carry out freshening, the logistics that the second riser reactor outlet is discharged is separated through finish separation system, isolated reclaimable catalyst is through stripping, after regeneration, Returning reactor recycles, the reaction oil gas of isolated reaction oil gas and the first riser reactor enters the further separated product that obtains of subsequent separation system after mixing.
In method provided by the invention, catalyticing conversioning condition described in the first riser reactor is: temperature of reaction is 450-650 ℃, preferred 480-550 ℃, reaction pressure is 100-450kPa, preferred 100-300kPa, catalyzer and stock oil mass ratio are (2-20): 1, preferably (3-10): 1, and reaction time is 0.1-30 second, preferred 0.1-10 second.
Catalytic conversion reaction condition described in the second riser tube is: temperature of reaction is 400-560 ℃, preferred 450-550 ℃, reaction pressure is 100-450kPa, preferred 100-300kPa, catalyzer and stock oil mass ratio are (2-20): 1, preferably (3-10): 1, and reaction time is 0.1-30 second, preferred 0.1-5 second.
In method provided by the invention, described heavy hydrocarbon oil raw material is the petroleum hydrocarbon cut that initial boiling point is greater than 250 ℃, is selected from one or more the mixture in long residuum, decompressed wax oil cut, vacuum residue fraction, vacuum residuum solvent-deasphalted oils, hydro-cracking of vacuum residue tail oil, vacuum residuum hydrotreatment oil.
In method provided by the invention, described catalyzer is for containing or do not contain the acidic catalyst cracking catalyst of molecular sieve.Described molecular screening self-contained or not containing the Y of rare earth or HY type zeolite, containing or containing ultrastable Y－type zeolite, the ZSM-5 series zeolite of rare earth or have in the supersiliceous zeolite, β zeolite, ferrierite of five-membered ring structure a kind of, two or more, described catalyzer for the acidic catalyst cracking catalyst containing molecular sieve be not amorphous silicon aluminium catalyzer.
In method provided by the invention, described top cycle oil fraction raw material is the part of the top turning oil of separation system separation column, and boiling range is 80 ℃-270 ℃.
The beneficial effect of method provided by the invention is:
Partially catalyzed separation system fractionation tower top turning oil is entered to the second riser tube as top cycle oil fraction raw material and carry out catalytic cracking reaction, gasoline yield is improved, in gasoline, olefin(e) centent reduces, and liquefied gas yield improves.Because aromaticity content in the turning oil raw material of top is high, therefore make aromaticity content in gasoline products raise, so gasoline octane rating improve.
Present method operates separately owing to having increased by the second riser tube, and turndown ratio is large.The second riser tube adopts high severity operational condition, can increase gasoline yield, gasoline octane rating and liquefied gas yield; The second riser tube adopts low severity operational condition, can significantly reduce content of olefin in gasoline, increases isoparaffin content, and catalytic gasoline octane value increases to some extent.
From embodiment and comparative example, adopt method provided by the invention, gasoline yield improves 3-10 percentage point, and liquefied gas yield improves 0.5-3 percentage point, and content of olefin in gasoline reduces 5-20 percentage point, and in gasoline, (RON) improves 0.2-2 unit.And relatively inferior catalytic diesel oil productive rate can decline to some extent;
Accompanying drawing explanation
Accompanying drawing is the schematic flow sheet of catalytic conversion method of hydrocarbon oil provided by the invention.
Embodiment
Below in conjunction with accompanying drawing, illustrate the embodiment of catalytic conversion method of hydrocarbon oil provided by the invention, but therefore the present invention is not restricted.
Catalytic conversion method of hydrocarbon oil provided by the invention, the method comprises two riser reactors, two settling vessel, stripping section and revivifiers that riser reactor is shared.
Specifically comprise the following steps:
By pre-lift medium through pipeline 3, heavy hydrocarbon oil raw material is introduced in the first riser reactor 2 by bottom through pipeline 1, with through regenerator sloped tube 4, the high-temperature regenerated catalyst from revivifier 21 contacts, under catalytic cracking condition, react, catalytic cracking condition described in the first riser reactor is: temperature of reaction is 450-650 ℃, preferred 480-550 ℃, reaction pressure is 100-450kPa, preferred 100-300kPa, catalyzer and stock oil mass ratio are (2-20): 1, preferably (3-10): 1, and reaction time is 0.1-30 second, preferred 0.1-10 second.Catalyzer with coke after the oil gas generating and reaction upwards enters the finish disengaging zone 6 in settling vessel 5.
In the top pump around circuit pipeline 15 of main fractionating tower 10, extract part top turning oil out and introduce the second riser reactor 18 through pipeline 17, all the other top turning oils draw back main fractionating tower as pump around circuit through pipeline 16, the pre-lift medium of introducing through pipeline 19 contacts with the top cycle oil fraction of introducing through pipeline 17 with the high-temperature regenerated catalyst of introducing through regenerator sloped tube 20, catalytic cracking reaction condition described in the second riser reactor is: temperature of reaction is 400-560 ℃, preferred 450-550 ℃, reaction pressure is 100-450kPa, preferred 100-300kPa, catalyzer and stock oil mass ratio are (2-20): 1, preferably (3-10): 1, reaction time is 0.1-30 second, preferred 0.1-5 second.The oil gas and the reacted catalyzer that generate upwards enter the finish disengaging zone 21 in settling vessel 5.
Wherein, in the first riser reactor and the second riser reactor, stock oil sprays in riser reactor through atomising unit together with atomized water steam, in the first riser reactor, the mass ratio of water vapour and stock oil is (0.01-0.5): 1, be preferably (0.02-0.3): 1.In the second riser reactor, the mass ratio of water vapour and stock oil is (0.01-0.5): 1, preferred (0.02-0.5): 1.
In finish disengaging zone, 6,21 isolated reaction oil gas are introduced the separation system separating reaction products such as main fractionating tower 10 through main gas pipeline 9, fractionator overhead cut is introduced gas-liquid separation in condensing cooling and oil-water-gas separating tank 12 through pipeline 11, and the liquefied gas separating is through pipeline 13 caterpillars; Isolated naphtha fraction is through pipeline 14 caterpillars; Catalyzer obtains reclaimable catalyst after stripping stage 7 strippings, and reclaimable catalyst is introduced in revivifier 21 and carried out coke burning regeneration activity recovery through inclined tube 8 to be generated, obtains regenerated catalyst, regenerated catalyst is returned to riser reactor and recycle.
In method provided by the invention, described pre-lift medium is various pre-lift medium well known to those skilled in the art, as one or more in water vapor, refinery dry gas, light paraffins, light olefin.The effect of pre-lift medium is to make catalyzer accelerate to rise, and forms the catalyst activity plug flow of even density in riser reactor bottom.The consumption of pre-lift medium is well known for the person skilled in the art, and in general, the consumption of pre-lift medium accounts for 1～30wt% of hydrocarbon ils total amount, preferably 2～15wt%.
In method provided by the invention, the top cycle oil fraction raw material that the second described riser reactor is introduced is a part for the top turning oil of separation system separation column.The top cycle oil fraction of described introducing the second riser reactor is the 1-50% of fractionation tower top turning oil total amount.
In method provided by the invention, the weight ratio of the heavy hydrocarbon oil raw material that introduce the top cycle oil fraction raw material that introduce the second described riser reactor bottom and the first riser reactor bottom is (0.015-0.8): 1.
In method provided by the invention, described catalyzer is that described catalyzer is the acidic catalyst cracking catalyst that contains or do not contain molecular sieve.Consisting of of catalytic cracking catalyst is conventionally known to one of skill in the art, and the present invention is not limited in this respect.Described molecular screening self-contained or not containing the Y of rare earth or HY type zeolite, containing or containing ultrastable Y－type zeolite, the ZSM-5 series zeolite of rare earth or have in the supersiliceous zeolite, β zeolite, ferrierite of five-membered ring structure a kind of, two or more.The described acidic catalyst cracking catalyst that does not contain molecular sieve is amorphous silicon aluminium catalyzer.Wherein preferably contain the catalytic cracking catalyst of molecular sieve.
In method provided by the invention, the first riser reactor of introducing heavy hydrocarbon oil raw material is 1 with the volume ratio of introducing the second riser reactor of top turning oil raw material: (0.1～1), be preferably 1: (0.2～0.5).Two riser reactor diameters can be identical, also can be different, when the diameter of riser reactor is identical, the aspect ratio of the first riser reactor and the second riser reactor is volume ratio, therefore, when riser reactor diameter is identical, the aspect ratio of the first riser reactor and the second riser reactor is 1: (0.1～1), be preferably 1: 0.2～0.5.
In method provided by the invention, described reclaimable catalyst is the catalyzer after stripping stage stripping after catalytic conversion reaction completes, and reclaimable catalyst carbon content is about 0.5～1.2wt%.Regenerated catalyst is the catalyzer of holomorphosis, and this coke on regenerated catalyst is about 0.01～0.05wt%.
In method provided by the invention, adopt water vapor to carry out stripping in stripper, its effect is that the oil gas that is full of between granules of catalyst and in particle hole is cemented out, and improves oil product productive rate.Amount for steam stripped water vapor is well known for the person skilled in the art.In general, for steam stripped water vapor amount, account for 0.1～0.8wt% of catalyst recirculation amount, preferred 0.2～0.4wt%.
In method provided by the invention, in described revivifier, introduce oxygen-containing gas, air for example, under the condition of 550-750 ℃, with the charcoal coke burning regeneration on the reclaimable catalyst of charcoal, activity recovery.Operational condition in revivifier is known to the skilled person, and the present invention is not limited in this respect.
By comparative example and embodiment, the present invention is further described below, but therefore the present invention is not restricted.
In comparative example and embodiment, the catalytic cracking catalyst trade mark used is MLC-500, by Shandong catalyzer branch office of China Petroleum Chemicals Corporation, is produced, and character is listed in table 1;
Heavy hydrocarbon oil raw material long residuum used, tower top cycle oil fraction, naphtha fraction and diesel oil distillate are all taken from China PetroChemical Corporation's Gaoqiao Petrochemical Company, and character is listed in table 2-table 5.
Comparative example 1
Comparative example 1 explanation returns to naphtha fraction to the reaction effect that subsidiary riser carries out the double lifting leg reactive system of freshening.
Adopt medium-sized duo-lift tube reactor, the first riser reactor is that total height is 10 meters, and internal diameter is the cylindrical structure of 2.5 centimetres, and this riser tube foot is pre lift zone.The second riser reactor 5 for total height be 8 meters, internal diameter is the cylindrical structure of 2.5 centimetres, this riser tube foot is pre lift zone.Catalyzer is MLC500, and heavy hydrocarbon oil raw material is long residuum, and character is in Table 3.
Concrete implementation step is: the long residuum that is preheating to 200 ℃ is introduced the first riser reactor bottom, with the regenerated catalyst hybrid reaction promoting through pre-lift medium, reaction oil gas and catalyzer upwards enter settling vessel along riser tube to riser reactor outlet, through cyclonic separator separating catalyst and reaction product, reaction product enters subsequent separation system by gas pipeline and isolates product, catalyzer obtains reclaimable catalyst through stripping, and reclaimable catalyst enters after revivifier burns activity recovery and recycles through pipeline to be generated.Naphtha fraction is introduced to the second riser reactor bottom, with the regenerated catalyst hybrid reaction through pre-lift, reaction oil gas and catalyzer mix along riser tube reaction oil gas and reclaimable catalyst that upwards and the first riser reactor outlet rear to riser reactor outlet discharged, enter together subsequent separation system.
Main operational condition and product distribution results are listed in table 4, and the gasoline products obtaining forms and character is listed in table 5.
Comparative example 2
Comparative example 2 explanations return to diesel oil distillate to the reaction effect that subsidiary riser carries out the double lifting leg reactive system of freshening.
Adopt the medium-sized double lifting leg reactive system in comparative example 1.Catalyzer is MLC-500, and heavy hydrocarbon oil raw material is long residuum, and character is in Table 3.The raw material of the second riser tube is diesel oil distillate, character in Table.
Concrete implementation step is with comparative example 1, and difference is diesel oil distillate to be introduced to the second riser reactor bottom react.Main operational condition and product distribution results are listed in table 4, and gasoline forms and character is listed in table 5.
Embodiment 1
Embodiment 1 explanation is provided by the invention returns to tower top cycle oil fraction to the reaction effect that subsidiary riser carries out the double lifting leg reactive system of freshening.
Adopt the medium-sized double lifting leg reactive system in comparative example 1.Catalyzer is MLC-500, and heavy hydrocarbon oil raw material is long residuum, and character is in Table 3.The raw material of the second riser tube is tower top cycle oil fraction, and character is in Table 2.
Concrete implementation step is with comparative example 1, and difference is the top cycle oil fraction raw material of catalytic cracking main fractionating tower to be introduced to the second riser reactor bottom react.Wherein, top cycle oil fraction raw material and long residue feed weight ratio are 1: 12.Main operational condition and product distribution results are listed in table 4, and gasoline forms and character is listed in table 5.
Adopt the medium-sized double lifting leg reactive system in comparative example 1.Catalyzer is MLC500, and heavy hydrocarbon oil raw material is long residuum, and character is in Table 3.The raw material of the second riser tube is tower top cycle oil fraction, and character is in Table 2.
Concrete implementation step is with embodiment 1, and difference is that described top cycle oil fraction raw material and long residue feed weight ratio are 1: 8.Main operational condition and product distribution results are listed in table 4, and gasoline forms and character is listed in table 5.
Table 1 catalyst property
| Project | MLC-500 |
| Chemical constitution, % | |
| RE 2O 3 | 3.0 |
| AL 2O 3 | 54.6 |
| Na 2O | 0.13 |
| Fe | 0.245 |
| Ca | 0.107 |
| Physical properties | |
| Specific surface area, m 2/g | 124 |
| Pore volume cm 3/g | 0.161 |
| Micro-activity | 64 |
Table 2 long residuum character
| Project | Long residuum |
| Density, g/cm3 | 0.8972 |
| Condensation point, ℃ | 49 |
| Carbon residue, wt% | 4.7 |
| Sulphur content, wt% | 0.61 |
| Nitrogen content, wt% | 0.08 |
| Nickel content, ppm | 6.7 |
| Content of vanadium, ppm | 3.2 |
| Boiling range, ℃ | |
| Initial boiling point | 258 |
| 10％ | 363 |
| 30％ | 415 |
| 50％ | 467 |
Table 3 top cycle oil fraction character
| Project | Top turning oil |
| Density, g/cm 3 | 0.8143 |
| Cetane value | 25.4 |
| 20 ℃ of specific refractory poweres | 1.4624 |
| Boiling range, ℃ | |
| Initial boiling point | 83.5 |
| 10％ | 152.9 |
| 30％ | 169.7 |
| 50％ | 186.3 |
| 70％ | 199.5 |
| 90％ | 222.4 |
| Final boiling point, ℃ | 270 |
| 20 ℃ of viscosity, mm 2/s | 1.285 |
| Carbon residue, wt% | ＜0.05 |
| Carbon content, wt% | 87.29 |
| Hydrogen richness, wt% | 12.61 |
| Group composition, quality % | |
| Normal paraffin | 10.2 |
| Isoparaffin | 23.57 |
| Alkene | 10.32 |
| Naphthenic hydrocarbon | 3.15 |
| Aromatic hydrocarbons | 52.76 |
Table 4 naphtha fraction character
Table 5 diesel oil distillate character
| Project | Diesel oil |
| Density, g/cm 3 | 0.8833 |
| Cetane value | 36.6 |
| 20 ℃ of specific refractory poweres | 1.5072 |
| Boiling range, ℃ | |
| Initial boiling point | 179.6 |
| 10％ | 227.3 |
| 30％ | 250.5 |
| 50％ | 276.0 |
| 70％ | 309.3 |
| 90％ | 355.9 |
| Final boiling point, ℃ point | 345 |
| 20 ℃ of viscosity, mm 2/s | 4.776 |
| Carbon residue, wt% | 0.18 |
| Carbon content, wt% | 87.88 |
| Hydrogen richness, wt% | 11.95 |
Table 6 reaction conditions and result
| Example | Comparative example 1 | Comparative example 2 | Embodiment 1 | |
| The first riser reactor | ||||
| Pressure, kPa | 140 | 140 | 140 | 140 |
| Temperature out, ℃ | 502 | 502 | 502 | 502 |
| Agent- |
6 | 6 | 6 | 6 |
| Reaction time, second | 4 | 4 | 4 | 4 |
| Atomizing steam amount, % | 5 | 5 | 5 | 5 |
| The second riser reactor | ||||
| Pressure, kPa | 140 | 140 | 140 | 140 |
| Temperature out, ℃ | 505 | 505 | 505 | 495 |
| Raw material weight ratio, the second/the first | 1∶12 | 1∶12 | 1∶12 | 1∶8 |
| Regenerator temperature, ℃ | 670 | 670 | 670 | 670 |
| Product distributes: wt% | ||||
| Dry gas | 3.9 | 3.9 | 3.9 | 3.9 |
| Liquefied gas | 14.2 | 15.2 | 14.4 | 14.0 |
| Gasoline | 42.3 | 44.3 | 49.5 | 46.7 |
| Diesel oil | 24.1 | 20.0 | 19.0 | 20.4 |
| Heavy oil | 8.6 | 9.6 | 6.2 | 8.0 |
| Coke | 6.9 | 7.0 | 7.0 | 7.0 |
| Gasoline family forms: wt% | ||||
| Normal paraffin | 8.2 | 9.2 | 7.2 | 7.6 |
| Isoparaffin | 21.6 | 21.1 | 22.4 | 28.1 |
| Alkene | 42.1 | 40.1 | 37.1 | 31.7 |
| Naphthenic hydrocarbon | 7.5 | 7.7 | 7.1 | 6.7 |
| Aromatic hydrocarbons | 20.6 | 21.9 | 26.2 | 25.9 |
| Gasoline octane rating | 90.2 | 90.5 | 91.1 | 91.0 |
As can be seen from Table 6, comparative example 1,2 and embodiment 1 contrast are visible, adopt method provided by the invention, and gasoline yield increases 5-7 percentage point, and diesel yield reduces 1-5 percentage point, and gasoline octane rating improves 0.6-0.9 unit.
From embodiment 1 and embodiment 2 contrasts, adopt method provided by the invention, the second outlet temperature of riser is controlled as a little more than the first outlet temperature of riser, can significantly increase gasoline and liquefied gas yield, gasoline yield improves 2.8 percentage points, and liquefied gas yield can improve 0.4 percentage point; And the catalytic diesel oil productive rate that quality is lower relatively reduces by 1.4 percentage points.Aromatic Hydrocarbon in Gasoline content increases by 0.3 percentage point, and meanwhile, product gasoline octane value significantly increases, and RON can improve 0.1Ge unit.
Present method operates separately owing to having increased by the second riser tube, and turndown ratio is large.The second riser tube adopts high severity operational condition, can increase gasoline yield, gasoline octane rating and liquefied gas yield; The second riser tube adopts low severity operational condition, can significantly reduce content of olefin in gasoline, increases isoparaffin content, and catalytic gasoline octane value increases to some extent.
Claims (8)
1. the method for a hydrocarbon oil catalytic conversion, it is characterized in that, catalytic cracking unit comprises the first riser reactor and the second riser reactor, heavy hydrocarbon oil raw material after preheating is introduced to the first riser reactor by bottom, contact with the high-temperature regenerated catalyst coming from revivifier, under catalytic cracking condition, react and make progress and flow, it is separated that reaction oil gas and reclaimable catalyst enter finish separation system by the first riser reactor top outlet, isolated reclaimable catalyst is through stripping, after regeneration, return to first, the second riser reactor recycles, isolated reaction oil gas is introduced main fractionating tower, a part for tower top turning oil is extracted out, by bottom, introduce and in the second riser reactor, carry out freshening, the logistics that the second riser reactor outlet is discharged is separated through finish separation system, isolated reclaimable catalyst is through stripping, after regeneration, return to first, the second riser reactor recycles, the reaction oil gas of isolated reaction oil gas and the first riser reactor enters the further separated product that obtains of subsequent separation system after mixing, and described tower top turning oil boiling range is 80-270 ℃, the catalytic cracking condition of the first described riser tube is: temperature of reaction is 450-650 ℃, and reaction pressure is 100-450kPa, and catalyzer and stock oil mass ratio are (2-20): 1, and the reaction times is 0.1-30 second, the second described riser catalytic cracking condition is: temperature of reaction is 400-560 ℃, and reaction pressure is 100-450kPa, and catalyzer and stock oil mass ratio are (2-20): 1, and the reaction times is 0.1-30 second.
2. according to the method for claim 1, it is characterized in that, the first described riser catalytic cracking condition is: temperature of reaction is 480-550 ℃, and reaction pressure is 100-300kPa, catalyzer and stock oil mass ratio are (3-10): 1, and the reaction times is 0.1-10 second.
3. according to the method for claim 1, it is characterized in that, the second described riser catalytic cracking condition is: temperature of reaction is 450-550 ℃, and reaction pressure is 100-300kPa, catalyzer and stock oil mass ratio are (3-10): 1, and the reaction times is 0.1-5 second.
4. according to the method for claim 1, it is characterized in that, the 1-50% of described tower top turning oil is extracted out to introduce in the second riser reactor and carry out freshening.
5. according to the method for claim 1, it is characterized in that, the tower top turning oil raw material of described introducing the second riser reactor is (0.015-0.8) with the weight ratio of introducing the heavy hydrocarbon oil raw material of the first riser reactor: 1.
6. according to the method for claim 1, it is characterized in that, described heavy hydrocarbon oil raw material is the petroleum hydrocarbon cut that initial boiling point is greater than 250 ℃.
7. according to the method for claim 6, it is characterized in that, described heavy hydrocarbon oil raw material is selected from one or more the mixture in long residuum, decompressed wax oil, vacuum residuum, vacuum residuum solvent-deasphalted oils, hydro-cracking of vacuum residue tail oil and vacuum residuum hydrotreatment oil.
8. according to the method for claim 1, it is characterized in that, described catalyzer is catalytic cracking catalyst.
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| CN109705914B (en) * | 2017-10-25 | 2021-05-14 | 中国石油化工股份有限公司 | Method and system for catalytic cracking by adopting double lifting pipes |
| CN110305694B (en) * | 2018-03-20 | 2021-07-09 | 中国石油化工股份有限公司 | Method for increasing yield of low-carbon olefin and light aromatic hydrocarbon |
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