CN100404644C - Method and apparatus for processing coked waxy oil - Google Patents

Abstract

The invention discloses coker gatch processing method. It divides the under part of the catalytic cracking riser reactor into two paralleled independent reaction zone in which coker gatch and conventional raw oil are reacted. The reacted matters are meted in the upper part and entered sedimentation stripping system together. The invention also discloses the device that it set the first and second tubes in the under part reaction zone which are upright and paralleled. It can improve the doping quantity of the coker gatch and the quality of the gasoline and diesel oil, and increase liquid yield.

Description

A kind of method of processing coked waxy oil and device

Technical field

The present invention relates to a kind of method and device of processing coked waxy oil, particularly relate to a kind of catalyzed cracking processing Technology and device of delayed coking middle runnings wax tailings.

Background technology

Delayed coking is one of important oil secondary processing process, and inferior raw material is had very strong adaptive faculty.Along with crude oil heaviness day by day, import high-sulfur crude oil ratio inferior constantly increases, and coking has obtained bigger concern, and domestic oil refining enterprises has strengthened the capacity expansion revamping of coker.At present, domestic coker working ability has reached about 4,000 ten thousand tons.

Say that briefly one of difficult problem of restriction coking development is exactly the rational processing and utilization of wax tailings, is the subject matter that present delayed coking process faces.Wax tailings is as the middle distillate product of coking, usually account for 20%～30% of coke chemicals, its majority parameters is near straight-run gas oil, is one of reasonable plan that solves the wax tailings outlet as the higher liquefied gas of catalytically cracked material productive value, gasoline and diesel oil with wax tailings.

Find that but analyze the aromaticity content of wax tailings and nitrogen content particularly basic n content are higher, aromaticity content is generally about 30%, and nitrogen content is about 0.35%.Owing to basic nitrogen compound in the catalytic cracking reaction process can and acidity of catalyst central role reduce activity of such catalysts, show on the products distribution it is that coking yield increases, yield of light oil decline.The result of study of TOPSOE company is thought, every increase by the 100 μ g/g of the nitrogen in the catalytic cracking charging, and transformation efficiency reduces by 0.3～0.5 percentage point, and the VOLUME LOSS of gasoline and loss of conversion were near 1: 1, and gasoline bromine valency increases by 2～3 units approximately; The result of study of Engelhard company thinks that when the raw material total nitrogen was lower than 2000 μ g/g, every increase by 100 μ g/g nitrogen can make 0.7～0.9 percentage point of loss of conversion; ARCO company points out that most of catalytic cracking unit can anti-2000 μ g/g total nitrogens and 1000 μ g/g alkali nitrogen.And China's wax tailings nitrogen content far exceeds the requirement for restriction of catalytic cracking unit to nitrogen generally all more than 0.35%, and therefore, wax tailings will reduce transformation efficiency and yield of light oil during directly as the catalytic cracking unit charging.In the wax tailings nitrogen content especially basic nitrogen compound content and aromaticity content height determined and must carry out certain pre-treatment wax tailings, perhaps improve catalytic cracking process.

When wax tailings is as catalytically cracked material, all carried out hydrotreatment usually in advance abroad, had fcc raw material over half, West Europe about 10% to carry out hydrotreatment as the U.S..Production practice prove, wax tailings is after hydrotreatment, its sulphur, nitrogen (especially basic nitrogen compound) content obviously descend, polycyclic aromatic hydrocarbons reduces, and carbon residue reduces, and removes the part heavy metal, improved its cracking performance, even be better than straight-run gas oil, and be cracking stock preferably, can improve transformation efficiency and yield of light oil greatly.Fushun Petrochemical Research Institute adopts the FCT catalyzer, at 6.4Mpa hydrogen pressure, 380 ℃ and 1.0hr ^-1Condition under, the wax tailings of Nanjing and Chang Ling is handled, the nitrogen extrusion rate reaches more than 80%.Sinopec Research Institute of Petro-Chemical Engineering carries out the hydrogenation pre-treatment earlier to the defeated 4 kinds of wax tailings of grand celebration, triumph, the Liaohe River and pipe, then its catalytic cracking performance is compared, the wax tailings transformation efficiency of discovery after hydrotreatment improves, and liquefied gas and yield of gasoline rise and coke yield decline.

But, owing to be subjected to the restriction of hydrogen addition technology, device and hydrogen source, China's oil refining enterprise is difficult to widely wax tailings be carried out hydrotreatment as abroad, mainly adopt not hydrogenation and directly carry out the method that refining is mixed in catalytic cracking, relative measures has pair wax tailings to carry out pre-treatment to improve wax tailings character, or the improvement of catalytic cracking process.

Bibliographical information in furfural treatment, the organic acid and basic nitrogen compound, mineral acid remove that basic nitrogen compound, solid adsorbent remove basic nitrogen compound, the complexing method is removed basic nitrogen compound and double solvents extraction denitrogenation etc., but still be in the laboratory study stage at present.Just utilize the lubricating oil solvent device to carry out the refining of catalytic cycle oil and wax tailings in the fifties abroad, domestic research report is also more.Utilize lubricating oil Extract extraction wax tailings, can obviously reduce basic nitrogen compound and gum level, can improve the yield that wax tailings is raffinated oil simultaneously.This technology is not used fresh solvent, does not increase the process cost of novel solvent consumption and recovery.But discover that though furfural denitrogenation ability is very strong, can the treated oil yield is very low after extracting, its selectivity is too poor.

Utilize mineral acid example hydrochloric acid, sulfuric acid etc. to handle wax tailings, make nitride generate soluble salt and remove, can remove nitride 80%.But because it is applicable to that relatively molecular-weight average is 120 to 350 oil product, and along with the increase of molecular weight, denitrification percent reduces, and therefore the effect of deviating to nitride in the wax tailings is difficult to reach production requirement.Use for reference complex compound method lubricating oil denitrogenation mechanism, carrying out removing of wax tailings basic nitrogen compound also is the route that is worth exploration, because the WSQ-2 type lubricating oil denitrfying agent that Wuhan Petroleum Chemical Engineering Institute develops is all obtained good effect at Jingmen refinery and factory of high bridge petrochemical refining industrial amplification test.The TTS and the STS lubricating oil denitrfying agent of Chinese Petroleum Univ. development also successfully have been applied to the denitrification process of lubricating oil, have removed the alkali nitrogen more than 90% in the lubricating oil.But network and denitrogenation exist that complexing metal costs an arm and a leg and problem such as denitrfying agent recycling difficulty.

Mix aspect the coking wax oil process modification in catalytic cracking, adopting anti-nitrogen cracking catalyst is the simple pathway that solves wax tailings alkali nitrogen problem.Studies show that under identical micro-activity, the molecular sieve that acid site density is high is favourable to improving activity of such catalysts as catalyst activity component; The existence of molecular sieve middle-weight rare earths also helps anti-nitrogen; Also is to alleviate the important channel that nitrogen is poisoned with acid additive as the catcher of nitrogen.But because wax tailings basic n content height, some anti-nitrogen catalyzer that adopt such as RHZ-200, LC-7, CCC-1, RHZ-300 have little effect at present.

Zhang Rui speeds to wait the characteristics at wax tailings, has proposed catalytic cracking absorption conversion method processing coked waxy oil technology (DNCC) technology, applies for and obtained Chinese invention patent (ZL 92114045.2).This patented technology proposes to adopt sectional feeding, the FCC raw material at first contacts with regenerator in the riser tube bottom, carry out catalytic cracking reaction, and wax tailings contacts with carbon deposited catalyst in the charging of riser tube top, utilizes the absorption of wax tailings on carbon deposited catalyst to transform, a part is cracked into low molecule product, another part removes nuisances such as part sulphur, nitrogen compound and changes into high quality raw material, reaches the purpose of refining wax tailings, carries out catalytic cracking reaction as recycle stock then.But this technology exists recycle ratio to increase, and process cost improves, problems such as environmental pollution.

WO9955801 discloses a kind of method of non-linear charging, and distillate is injected same riser tube by different nozzles respectively with inferior heavy oil, or injects the differential responses district of the axial division of same riser tube respectively.When petroleum hydrocarbon of different nature injects same riser tube by different nozzles respectively, because the back-mixing of catalyzer and reaction oil gas will cause bad influence to the implementation result of non-linear charging.When petroleum hydrocarbon of different nature injects the axial distribution differential responses district of same riser tube respectively, the reaction severity of the petroleum hydrocarbon of injecting lift pipe lower reaction zone is higher, and the reaction severity of the petroleum hydrocarbon of injecting lift pipe top reaction zone is low, thereby total reaction conversion ratio and product selectivity can be subjected to influence to a certain degree, is difficult to guarantee the implementation result of non-linear charging.

Chinese patent ZL00122842.0 discloses a kind of catalytically cracked material feed process, promptly above the regenerated catalyst inlet of riser reactor inside, the finish sparger is set, the lower middle portion of riser reactor is divided into is parallel to 2～4 axial reaction zones, and corresponding hydrocarbon raw material nozzle is set at each reaction zone; High temperature catalyst uniform distribution in each reaction zone from revivifier; Hydrocarbon raw material of different nature injects different reaction zones respectively, contacts with the high temperature regeneration agent and reacts; Reacted logistics is up along riser tube in reaction zone separately, leave the finish sparger after, each logistics mixes in continuing the process up along riser tube mutually; Reaction product isolated, spent agent returns riser reactor and recycles after gas is carried, regenerated.Chinese patent ZL00122836.6 discloses a kind of contact method for catalytic cracking of oil, promptly locate the finish sparger to be set between the main raw material ingress in the pre-lifting medium inlet of riser tube inside, the lower section of riser reactor is divided into is parallel to 2～4 axial reaction zones, and corresponding catalyst inlet and pre-upgrading raw material nozzles are set at each reaction zone; Enter different reaction zones respectively from the high temperature regeneration agent of revivifier, cooled half regenerator and/or from the spent agent of stripping section; Pre-upgrading raw material injects 1,2 or 3 reaction zones wherein, and is up along riser tube in reaction zone separately with the catalyzer in the reaction zone, after finish sparger exit is converged, through the main raw material contact of steam atomizing and react; Reaction product isolated, and spent agent is carried out gas carry and regenerate, above-mentioned finish contact process circulation is carried out.These two patents all proposed with quality preferably the relatively poor stock oil of stock oil such as straight-run gas oil and cracking performance such as vacuum residuum or wax tailings respectively with catalyzer contact reacts in the differential responses district of identical or different regeneration level, and then suitable position is converged in riser reactor, has improved product and has distributed and quality product.

But at the feed zone of catalytic cracking riser reactor, stock oil is spurted in the riser reactor with the speed about 60m/s through after the nozzle atomization.Because the injection of raw material oil gas high-speed jet and entrainmenting, granules of catalyst also is accompanied by and carries out violent motion, reactor wall has been produced intensive washed away.In order to reduce this effect, in the industrial practice, must be that even numbers of nozzles is arranged symmetrically on the riser reactor, otherwise the riser tube wall is very fast promptly to be punched by mill, influences its normal running.Above-mentioned patent is difficult to the reasonable Arrangement feed nozzle because circular cross section is divided unevenly for 2～4 zones, difficult enforcement on engineering.

In sum, existing wax tailings processing technology all can not solve the influence to catalytic cracking process of the aromatic hydrocarbons that exists in the wax tailings and nitrogen well.Raw material is day by day to today of heaviness and diversified development, how to effectively utilize the catalytic cracking unit processing coked waxy oil and will be that each refinery increases the benefit and an effective way of enhancing efficiency by relying on tapping internal latent power.

Summary of the invention

The objective of the invention is to solve the aromatic hydrocarbons that exists in the wax tailings and nitrogen problem, and make full use of the processing that existing catalytic cracking unit is carried out wax tailings effectively the influence of catalytic cracking process.

In order to achieve the above object, the present invention proposes a kind of method of processing coked waxy oil, this method is divided into two vertical parallel separate reaction zones with the bottom of the riser reactor of catalytic cracking unit, allow wax tailings and the conventional stock oil of other comparison fine enter different reaction zones and carry out catalytic cracking reaction, logistics behind two reaction zone internal reactions converges on the top of described riser reactor, and, enter the sedimentation stripping system more together by riser reactor.

The catalyzer that uses in the above-mentioned catalytic cracking reaction can enter described two reaction zones through a pre lift zone, or respectively through two independently pre lift zone enter described two reaction zones.

The catalyzer that uses in the above-mentioned catalytic cracking reaction also can be earlier through a mixing step before entering pre lift zone: the reclaimable catalyst with 20～60% mixes with regenerated catalyst, burn reaction, the catalyzer that reacted temperature reduces enters described pre lift zone again.

The reaction conditions of above-mentioned conventional stock oil and wax tailings is: preheating temperature is 100～300 ℃, preferred 150～250 ℃, temperature of reaction is 460～550 ℃, and preferred 480～510 ℃, agent-oil ratio is 4～12, preferred 6～9, catalyst activity is 50～70, and is preferred 58～65, and the reaction times is 2.0～3.5s, preferred 2.5～3.0s, reaction pressure is 0.1～0.4MPa.

The used catalyzer of the present invention can be any catalyzer that is applicable to catalytic cracking process, and promptly the catalytic cracking reaction of wax tailings is realized by the heavy oil catalytically cracking equipment catalyzer.For example, amorphous silicon aluminium catalyzer or molecular sieve catalyst, wherein, the active ingredient of molecular sieve catalyst is selected from one or more in Y type or HY type zeolite, the ultrastable Y that contains or do not contain rare earth and/or phosphorus, the ZSM-5 series zeolite that contains or do not conform to rare earth and/or phosphorus or the supersiliceous zeolite with five-membered ring structure, b zeolite, the ferrierite.

The present invention also provides a kind of device of processing coked waxy oil, comprise riser reactor, this riser reactor is divided into reaction zone and following reaction zone, described top of going up reaction zone is connected with the quick gas-solid separating device of efficient outlet, described reaction zone down is set to two vertical first pipeline and second pipelines of placing side by side, the bottom of described first pipeline and second pipeline is connected with the pre lift zone top, and the top of described first pipeline and second pipeline is connected with last reaction zone bottom.

Above-mentioned reaction zone length down is 5～50% of described riser reactor useful length, preferred 10～30%.

The bottom that a pre lift zone or above-mentioned first pipeline and second pipeline can be converged and be connected in the bottom of above-mentioned first pipeline and second pipeline can respectively be provided with a pre lift zone.

This device also comprises a revivifier, links to each other by pipeline with described reaction zone down with the described reaction zone of going up respectively; Also can set up a catalyst mix jar on the revivifier next door, this catalyst mix jar connects stripping stage and regenerator bottoms respectively by two inclined tubes, also connects described pre lift zone by an inclined tube.

Wherein first pipeline is used for the catalytic cracking reaction of conventional stock oil, the catalytic cracking that described second pipeline is used for wax tailings send out should, the ratio of described first pipeline and the cross-sectional area of second pipeline equals the ratio of described conventional stock oil and the consumption of wax tailings.For example, mix 20% wax tailings in conventional catalytically cracked stock, so, the ratio of the cross-sectional area of first pipeline and second pipeline is 80: 20.

The present invention is by being divided into the riser tube bottom diametrically two vertical parallel separate reaction zones, allow wax tailings and other compare fine stock oil and separate charging and reaction, make regenerator avoid the murder by poisoning of pollutents such as burnt wax neutral and alkali nitrogen, reach the fully cracking of high quality raw material oil, obtained the effect that good quality production distributes.

Technology advantage of the present invention is to consider when the coking wax oil is mixed in catalytic cracking, basic nitrogen compound preferentially adsorbed wherein is to catalyzer, poison the acid active centre of catalyzer, make cracking reaction product distribution variation, thereby proposed to allow wax tailings and other compare the complete processing scheme that fine stock oil separates the subregion conversion wax tailings of charging, and the five kinds of riser reactor partition schemes that can conveniently implement are proposed on industrial catalyticing cracking device, do not influencing on other basis of comparing the cracking reaction of fine raw material, improving the incorporation of wax tailings.Mixing the coking wax oil with conventional catalytic cracking compares, the present invention is when improving wax tailings incorporation ratio, liquid yield has the raising of different amplitudes, the time petrol and diesel oil quality product also be improved significantly, the puzzlement that solves China's wax tailings difficult processing to a certain extent.

Description of drawings

Fig. 1 is the synoptic diagram of the method and apparatus embodiment 1 of processing coked waxy oil of the present invention.

Fig. 2 is the synoptic diagram of the method and apparatus embodiment 2 of processing coked waxy oil of the present invention.

Fig. 3 is the synoptic diagram of the method and apparatus embodiment 3 of processing coked waxy oil of the present invention.

Fig. 4 is the synoptic diagram of the method and apparatus embodiment 4 of processing coked waxy oil of the present invention.

Fig. 5 is the synoptic diagram of the method and apparatus embodiment 5 of processing coked waxy oil of the present invention.

Embodiment

Describe method and apparatus of the present invention in detail below in conjunction with accompanying drawing.

The embodiment 1 of the method and apparatus of the processing coked waxy oil that the present invention proposes as shown in Figure 1.This method is at first being divided into the riser reactor 1 of conventional catalytic cracking unit two reaction zones up and down, following reaction zone 2 and last reaction zone 3, the top of the bottom of following reaction zone 2 and a pre lift zone 4 joins, the bottom connection of top and last reaction zone 3, last reaction zone 3 outlets are connected with the quick gas-solid separating device 5 of efficient outlet.The riser reactor length of two reaction zones is called the useful length of riser reactor about comprising.The length of following reaction zone 2 is riser reactor useful length 5～50%, preferred 10～30%.On this basis, following reaction zone 2 is made by the vertical structure of placing side by side, all unifying from beginning to end of two sections pipes, material and making method form two vertical parallel separate reaction zones 6 and 7 with conventional riser reactor.Separate reaction zones 6 and 7 cross section are determined by the ratio of the flow of conventional stock oil and wax tailings.As mix 20% wax tailings in conventional catalytically cracked stock, so, separate reaction zones 6 and 7 cross-sectional area ratio are 80: 20.

Its technological process is for being 100～300 ℃ with preheating temperature, the feed nozzle that preferred 150～250 ℃ conventional stock oil 8 distributes by circumferential direction symmetrically and evenly from reaction zone 6 bottoms enters reaction zone 6 and is 600～750 ℃ from revivifier 14 by the temperature that pre-lifting steam 17 promotes, preferred 650～700 ℃ regenerator is 460～550 ℃ in temperature of reaction, preferred 480～510 ℃, agent-oil ratio is 4～12, preferred 6～9, catalyst activity is 50～70, preferred 58～65, reaction times is 2.0～3.5s, preferred 2.5～3.0s, reaction pressure is to contact under the condition of 0.1～0.4MPa, gasification, mix and reaction oil gas, water vapour upwards enters the last reaction zone 3 of riser reactor 1 with catalyzer.Preheating temperature is 100～300 ℃, the feed nozzle that preferred 150～250 ℃ wax tailings 9 distributes by circumferential direction symmetrically and evenly from reaction zone 7 bottoms enters reaction zone 7 and is 600～750 ℃ from revivifier 14 by the temperature that pre-lifting steam 17 promotes, preferred 650～700 ℃ regenerator is 460～550 ℃ in temperature of reaction, preferred 480～510 ℃, agent-oil ratio is 4～12, preferred 6～9, catalyst activity is 50～70, preferred 58～65, reaction times is 2.0～3.5s, preferred 2.5～3.0s, reaction pressure is to contact under 0.1～0.4MPa, gasification, mix and reaction, oil gas, water vapour upwards enters the last reaction zone 3 of riser reactor 1 with catalyzer, after the catalyzer of reaction zone 6 and oil gas mix, last reaction zone by riser reactor 1, enter riser reactor afterwards and export efficient fast gas-solid separator 5, top cyclonic separator 10 and settling vessel 11, after this was with mixed oil and gas and catalyst separating, mixed oil and gas 12 entered main fractionating system through main oil gas piping and carries out rich gas, raw gasline, solar oil, recycle stock, the separation of slurry oil; After catalyzer enters stripping stage 13 strippings, enter revivifier 14 regeneration.Catalyzer 15 after the regeneration returns the pre lift zone 4 of riser reactor 1 bottom by inclined tube 16, after being promoted by pre-lifting steam 17, is further divided into two strands and enters down reaction zone 2, with wax tailings 8 and conventional stock oil 9 contact reactss, recycles respectively.

Fig. 2 shows the embodiment 2 of the method and apparatus of processing coked waxy oil of the present invention.This device at first is divided into two reaction zones up and down with the riser reactor 101 of conventional catalytic cracking unit, following reaction zone 102 and last reaction zone 103, the top of the bottom of following reaction zone 102 and pre lift zone 104 and 94 joins, the bottom connection of top and last reaction zone 103, last reaction zone 103 outlets are connected with the quick gas-solid separating device 105 of efficient outlet.The length of following reaction zone 102 is riser reactor useful length 5～50%, preferred 10～30%.

Following reaction zone 102 is made the structure of being converged mutually by two sections pipes vertical placement, top side by side, and material and making method form two vertical separate reaction zones 106 and 107 that walk abreast with conventional riser reactor.In revivifier 1014 bottoms two regenerator inclined tubes 1016 and 916 are set, connect pre lift zone 104 and 94 respectively. Separate reaction zones 106 and 107 cross section are determined by the ratio of conventional stock oil and wax tailings flow.As mix 20% wax tailings in conventional catalytically cracked stock, so, separate reaction zones 106 and 107 cross-sectional area ratio are 80: 20.

Its technological process is for being 100～300 ℃ with preheating temperature, the feed nozzle that preferred 150～250 ℃ conventional stock oil 108 distributes by circumferential direction symmetrically and evenly from reaction zone 106 bottoms enters reaction zone 106 and is 600～750 ℃ from revivifier 1014 by the temperature that pre-lifting steam 1017 promotes, preferred 650～700 ℃ regenerator is 460～550 ℃ in temperature of reaction, preferred 480～510 ℃, agent-oil ratio is 4～12, preferred 6～9, catalyst activity is 50～70, preferred 58～65, reaction times is 2.0～3.5s, preferred 2.5～3.0s, reaction pressure is to contact under 0.1～0.4MPa, gasification, mix and reaction oil gas, water vapour upwards enters the last reaction zone 103 of riser reactor 101 with catalyzer.Preheating temperature is 100～300 ℃, the feed nozzle that preferred 150～250 ℃ wax tailings 109 distributes by circumferential direction symmetrically and evenly from reaction zone 107 bottoms enters reaction zone 107 and is 600～750 ℃ from revivifier 1014 by the temperature that pre-lifting steam 917 promotes, preferred 650～720 ℃ regenerator is 460～550 ℃ in temperature of reaction, preferred 480～510 ℃, agent-oil ratio is 4～12, preferred 6～9, catalyst activity is 50～70, preferred 58～65, reaction times is 2.0～3.5s, preferred 2.5～3.0s, reaction pressure is to contact under 0.1～0.4MPa, gasification, mix and reaction, oil gas, water vapour upwards enters the last reaction zone 103 of riser reactor 101 with catalyzer, after the catalyzer of reaction zone 106 and oil gas mix, last reaction zone by riser reactor 101, enter riser reactor afterwards and export efficient fast gas-solid separator 105, top cyclonic separator 1010 and settling vessel 1011, after this was with mixed oil and gas and catalyst separating, mixed oil and gas 1012 entered main fractionating system through main oil gas piping and carries out rich gas, raw gasline, solar oil, recycle stock, the separation of slurry oil; After catalyzer enters stripping stage 1013 strippings, enter revivifier 1014 regeneration.

1015 fens two-way of catalyzer after the regeneration leave revivifier 1014, the inclined tube 1016 of leading up to returns the pre lift zone 104 of riser reactor 101 bottoms, enter reaction zone 106 by pre-lifting steam 1017 liftings,, recycle with conventional stock oil 108 contact reactss.The pre lift zone 94 of riser reactor 101 bottoms is returned by inclined tube 916 in another road, is promoted by pre-lifting steam 917 and enters reaction zone 107, with wax tailings 109 contact reactss, recycles.

The present invention can adopt embodiment 3 shown in Figure 3 to implement on mode basis as shown in Figure 1.Device wherein is at first being divided into the riser reactor 21 of conventional catalytic cracking unit two reaction zones up and down, following reaction zone 22 and last reaction zone 23, the top of the bottom of following reaction zone 22 and pre lift zone 24 joins, the bottom connection of top and last reaction zone 23, last reaction zone 23 outlets are connected with the quick gas-solid separating device 25 of efficient outlet.The length of following reaction zone 22 is riser reactor useful length 5～50%, preferred 10～30%.The following reaction zone 22 of riser reactor 21 is made by the vertical structure of placing side by side, all unifying from beginning to end of two sections pipes, and material and making method form two vertical parallel separate reaction zones 26 and 27 with conventional riser reactor. Separate reaction zones 26 and 27 cross section are determined by the ratio of conventional stock oil and wax tailings flow.As mix 20% wax tailings in conventional catalytically cracked stock, so, separate reaction zones 26 and 27 cross-sectional area ratio are 80: 20.

On the other hand, set up a catalyst mix jar 218, be connected revivifier 214, pre lift zone 24 and stripping stage 213 with pipeline 223 by inclined tube 219, inclined tube 216, inclined tube 221 respectively on revivifier 214 next doors.

Its technological process is for guiding to regenerated catalyst 215 with the inclined tube of setting up on the revivifier 214 of drawing high-temperature regenerated catalyst logistics 215 219 bottom of catalyst mix jar 218, simultaneously, reclaimable catalyst with 20～60% is also introduced in the catalyst mix jar 218 through inclined tube 221, two strands of catalyzer are under the fluidisation of the fluidization air 222 of mixing tank 218 bottoms introducing, mix on one side, burn reaction on one side, the fluidizing medium of carrying little amount of catalyst secretly returns in the revivifier 214 through pipeline 223.Another part spent agent returns in the revivifier 214 through inclined tube 220.The catalyzer that mixed temperature reduces enters the pre lift zone 24 of riser reactor 21 bottoms through inclined tube 216.

With preheating temperature is 100～300 ℃, the feed nozzle that preferred 150～250 ℃ conventional stock oil 28 distributes by circumferential direction symmetrically and evenly from reaction zone 26 bottoms enters reaction zone 26 and is 580～730 ℃ from catalyst mix jar 218 by the temperature that pre-lifting steam 217 promotes, preferred 620～670 ℃ catalyzer is 460～550 ℃ in temperature of reaction, preferred 480～510 ℃, agent-oil ratio is 5～13, preferred 8～10, catalyst activity is 50～70, preferred 58～65, reaction times is 2.0～3.5s, preferred 2.5～3.0s, reaction pressure is to contact under 0.1～0.4MPa, gasification, mix and reaction oil gas, water vapour upwards enters the last reaction zone 23 of riser reactor 21 with catalyzer.Preheating temperature is 100～300 ℃, the feed nozzle that preferred 150～250 ℃ wax tailings 29 distributes by circumferential direction symmetrically and evenly from reaction zone 27 bottoms enters reaction zone 27 and is 580～730 ℃ from catalyst mix jar 218 by the temperature that pre-lifting steam 217 promotes, preferred 620～670 ℃ catalyzer is 460～550 ℃ in temperature of reaction, preferred 480～510 ℃, agent-oil ratio is 5～13, preferred 8～10, catalyst activity is 50～70, preferred 58～65, reaction times is 2.0～3.5s, preferred 2.5～3.0s, reaction pressure is to contact under 0.1～0.4MPa, gasification, mix and reaction, oil gas, water vapour with catalyzer by upwards entering the last reaction zone 23 of riser reactor 21, after the catalyzer of reaction zone 26 and oil gas mix, last reaction zone by riser reactor 21, enter riser reactor afterwards and export efficient fast gas-solid separator 25, top cyclonic separator 210 and settling vessel 211, after this was with mixed oil and gas and catalyst separating, mixed oil and gas 212 entered main fractionating system through main oil gas piping and carries out rich gas, raw gasline, solar oil, recycle stock, the separation of slurry oil; After catalyzer enters stripping stage 213 strippings, enter revivifier 214 regeneration.Catalyzer 215 after the regeneration returns the pre lift zone 24 of riser reactor 21 bottoms by inclined tube 216, after being promoted by pre-lifting steam 217, is further divided into two strands and enters down reaction zone 22, with wax tailings 28 and conventional stock oil 29 contact reactss, recycles respectively.

The present invention can also implement by embodiment 4 as shown in Figure 4.Device wherein is at first being divided into the riser reactor 51 of conventional catalytic cracking unit two reaction zones up and down, following reaction zone 52 and last reaction zone 53, the top of the bottom of following reaction zone 52 and pre lift zone 54 and 540 joins, the bottom connection of top and last reaction zone 53, last reaction zone 53 outlets are connected with the quick gas-solid separating device 55 of efficient outlet.The length of following reaction zone 52 is riser reactor useful length 5～50%, preferred 10～30%.

The following reaction zone 52 of riser reactor 51 is made the structure of being converged mutually by two sections pipes vertical placement, top side by side, and material and making method form two vertical parallel separate reaction zones 56 and 57 with conventional riser reactor. Separate reaction zones 56 and 57 cross section are determined by the ratio of conventional stock oil and wax tailings flow.As mix 20% wax tailings in conventional catalytically cracked stock, so, separate reaction zones 56 and 57 cross-sectional area ratio are 80: 20.Set up a catalyst mix jar 68 on revivifier 64 next doors, and be connected to the bottom of catalyst mix jar 68 by an inclined tube 69.Catalyst mix jar 68 is connected stripping stage 63 and revivifier 64 by pre lift zone 540, the two outer inclined tubes 71 that also pass through that an inclined tube 66 connects riser reactor 51 bottoms with pipeline 73.

The technological process of embodiment 4 is for being 100～300 ℃ with preheating temperature, the feed nozzle that preferred 150～250 ℃ conventional stock oil 58 distributes by circumferential direction symmetrically and evenly from reaction zone 56 bottoms enters reaction zone 56 and is 600～750 ℃ from revivifier 64 by the temperature that pre-lifting steam 67 promotes, preferred 650～700 ℃ regenerator 65 is 460～550 ℃ in temperature of reaction, preferred 480～510 ℃, agent-oil ratio is 4～12, preferred 6～9, catalyst activity is 50～70, preferred 58～65, reaction times is 2.0～3.5s, preferred 2.5～3.0s, reaction pressure is to contact under 0.1～0.4MPa, gasification, mix and reaction oil gas, water vapour upwards enters the last reaction zone 53 of riser reactor 51 with catalyzer.In revivifier 64 bottoms two regenerator inclined tubes 69 and 76 are set, 65 fens two-way of catalyzer after the regeneration leave revivifier 64, the inclined tube 76 of leading up to returns the pre lift zone 54 of riser reactor 51 bottoms, enter reaction zone 56 by pre-lifting steam 67 liftings, with conventional stock oil 58 contact reactss, recycle.

Regenerated catalyst 65 is guided to the bottom of catalyst mix jar 68 with the inclined tube of setting up on the revivifier 64 of drawing high-temperature regenerated catalyst logistics 65 69, simultaneously, reclaimable catalyst with 20～60% is also introduced in the catalyst mix jar 68 through inclined tube 71, two strands of catalyzer are under the fluidisation of the fluidization air 72 of mixing tank 68 bottoms introducing, mix on one side, burn reaction on one side, the fluidizing medium of carrying little amount of catalyst secretly returns in the revivifier 64 through pipeline 73.Another part spent agent returns in the revivifier 64 through inclined tube 70.

Mixed temperature is reduced to 580～730 ℃, preferred 620～670 ℃ catalyzer enters the pre lift zone 540 of riser reactor 51 bottoms through inclined tube 66, promote the reaction zone 57 that enters riser reactor 51 bottoms by pre-lifting steam 77 then, the preheating temperature that enters with the feed nozzle that distributes symmetrically and evenly by circumferential direction from reaction zone 57 bottoms is 100～300 ℃, preferred 150～250 ℃ wax tailings 59 is 460～550 ℃ in temperature of reaction, preferred 480～510 ℃, agent-oil ratio is 5～13, preferred 8～10, catalyst activity is 50～70, preferred 58～65, reaction times is 2.0～3.5s, preferred 2.5～3.0s, reaction pressure is to contact under 0.1～0.4MPa, gasification, mix and reaction, oil gas, water vapour upwards flows with catalyzer, enter the last reaction zone 53 of riser reactor 51, after the catalyzer of reaction zone 56 and oil gas mix, last reaction zone 53 by riser reactor 51, enter riser reactor afterwards and export efficient fast gas-solid separator 55, top cyclonic separator 60 and settling vessel 61, after this was with mixed oil and gas and catalyst separating, mixed oil and gas 62 entered main fractionating system through main oil gas piping and carries out rich gas, raw gasline, solar oil, recycle stock, the separation of slurry oil; After catalyzer enters stripping stage 63 strippings, enter revivifier 64 regeneration, recycle then.

The present invention can also implement by embodiment 5 as shown in Figure 5.Device wherein is at first being divided into the riser reactor 81 of conventional catalytic cracking unit two reaction zones up and down, following reaction zone 82 and last reaction zone 83, the top of the bottom of following reaction zone 82 and pre lift zone 84 and 840 joins, the bottom connection of top and last reaction zone 83, last reaction zone 83 outlets are connected with the quick gas-solid separating device 85 of efficient outlet.The length of following reaction zone 82 is riser reactor useful length 5～50%, preferred 10～30%.The following reaction zone 82 of riser reactor 81 is made the structure of being converged mutually by two sections pipes vertical placement, top side by side, and material and making method form two vertical parallel separate reaction zones 86 and 87 with conventional riser reactor. Separate reaction zones 86 and 87 cross section are determined by the ratio of conventional stock oil and wax tailings flow.As mix 20% wax tailings in conventional catalytically cracked stock, so, separate reaction zones 86 and 87 cross-sectional area ratio are 80: 20.

Set up a catalyst mix jar 98 on revivifier 94 next doors, be connected revivifier 94, pre lift zone 84 and 840, stripping stage 93 respectively by inclined tube 99, pipeline 103, inclined tube 96, inclined tube 960 and inclined tube 61 respectively.

Its technological process is, regenerated catalyst 95 is guided to the bottom of catalyst mix jar 98 with the inclined tube of setting up on the revivifier 94 of drawing high-temperature regenerated catalyst logistics 95 99, simultaneously, reclaimable catalyst with 20～60% is also introduced in the catalyst mix jar 98 through inclined tube 61, two strands of catalyzer are under the fluidisation of the fluidization air 102 of mixing tank 98 bottoms introducing, mix on one side, Yi Bian burn reaction, the fluidizing medium of carrying little amount of catalyst secretly returns in the revivifier 94 through pipeline 103.Another part spent agent returns in the revivifier 94 through inclined tube 100.

Two catalyzer inclined tubes 96 that are provided with in catalyst mix jar 98 bottoms and 960, divide two-way to draw catalyst mix jar 98 catalyzer wherein, the inclined tube 96 of leading up to removes the pre lift zone 84 of riser reactor 81 bottoms, promote the reaction zone 86 that enters riser reactor 81 bottoms by pre-lifting steam 97, the preheating temperature that enters with the feed nozzle that distributes symmetrically and evenly by circumferential direction from reaction zone 86 bottoms is 100～300 ℃, preferred 150～250 ℃ conventional stock oil 88 is 460～550 ℃ in temperature of reaction, preferred 480～510 ℃, agent-oil ratio is 5～13, preferred 8～10, catalyst activity is 50～70, preferred 58～65, reaction times is 2.0～3.5s, preferred 2.5～3.0s, reaction pressure is to contact under 0.1～0.4MPa, gasification, mix and reaction oil gas, water vapour upwards flows with catalyzer, enters the last reaction zone 83 of riser reactor 81.

Another road catalyzer that comes out from catalyst mix jar 98 removes the pre lift zone 840 of riser reactor 81 bottoms by inclined tube 960, promote the reaction zone 87 that enters riser reactor 81 bottoms by pre-lifting steam 970, the preheating temperature that enters with the feed nozzle that distributes symmetrically and evenly by circumferential direction from reaction zone 87 bottoms is 100～300 ℃, preferred 150～250 ℃ wax tailings 89 is 460～550 ℃ in temperature of reaction, preferred 480～510 ℃, agent-oil ratio is 5～13, preferred 8～10, catalyst activity is 50～70, preferred 58～65, reaction times is 2.0～3.5s, preferred 2.5～3.0s, reaction pressure is to contact under 0.1～0.4MPa, gasification, mix and reaction, oil gas, water vapour upwards flows with catalyzer, enter the last reaction zone 83 of riser reactor 81, after the catalyzer of reaction zone 86 and oil gas mix, last reaction zone 83 by riser reactor 81, enter riser reactor afterwards and export efficient fast gas-solid separator 85, top cyclonic separator 90 and settling vessel 91, after this was with mixed oil and gas and catalyst separating, mixed oil and gas 92 entered main fractionating system through main oil gas piping and carries out rich gas, raw gasline, solar oil, recycle stock, the separation of slurry oil; After catalyzer enters stripping stage 93 strippings, enter revivifier 94 regeneration.

It should be noted last that: above embodiment is the unrestricted technical scheme of the present invention in order to explanation only, although the present invention is had been described in detail with reference to the foregoing description, those of ordinary skill in the art is to be understood that, still can make amendment and/or be equal to replacement, and not break away from the spirit and scope of the present invention the present invention.

Claims (10)

1. the method for a processing coked waxy oil, it is characterized in that: the bottom of the riser reactor of catalytic cracking unit is divided into two vertical parallel separate reaction zones, allow wax tailings and conventional stock oil enter different reaction zones and carry out catalytic cracking reaction, logistics behind two reaction zone internal reactions converges on the top of described riser reactor, and, enter the sedimentation stripping system more together by described riser reactor.

2. the method for processing coked waxy oil according to claim 1, it is characterized in that: the catalyzer that uses in the catalytic cracking reaction enters described two reaction zones through a pre lift zone, or respectively through two independently pre lift zone enter described two reaction zones.

3. the method for processing coked waxy oil according to claim 1 and 2, it is characterized in that: the catalyzer that uses in the catalytic cracking reaction is first through a mixing step before entering pre lift zone: the reclaimable catalyst with 20～60% mixes with regenerated catalyst, burn reaction, the catalyzer that reacted temperature reduces enters described pre lift zone again.

4. the method for processing coked waxy oil according to claim 1, it is characterized in that: the reaction conditions of described conventional stock oil and wax tailings is: preheating temperature is 100～300 ℃, temperature of reaction is 460～550 ℃, agent-oil ratio is 4～12, catalyst activity is 50～70, reaction times is 2.0～3.5s, and reaction pressure is 0.1～0.4MPa.

5. the method for processing coked waxy oil according to claim 4, it is characterized in that: the reaction conditions of described conventional stock oil and wax tailings is: preheating temperature is 150～250 ℃, temperature of reaction is 480～510 ℃, agent-oil ratio is 6～9, catalyst activity is 58～65, reaction times is 2.5～3.0s, and reaction pressure is 0.1～0.4MPa.

6. the device of a processing coked waxy oil, comprise riser reactor, it is characterized in that: described riser reactor is divided into reaction zone and following reaction zone, described top of going up reaction zone is connected with the quick gas-solid separating device of efficient outlet, described reaction zone down is set to two vertical first pipeline and second pipelines of placing side by side, the bottom of described first pipeline and second pipeline is connected with the pre lift zone top, and the top of described first pipeline and second pipeline is connected with last reaction zone bottom.

7. the device of processing coked waxy oil according to claim 6 is characterized in that: described reaction zone length down is 5～50% of described riser reactor useful length.

8. the device of processing coked waxy oil according to claim 7 is characterized in that: described reaction zone length down is 10～30% of described riser reactor useful length.

9. the device of processing coked waxy oil according to claim 6, it is characterized in that: described first pipeline respectively is provided with a pre lift zone with the bottom that a pre lift zone or described first pipeline and second pipeline are converged and be connected in the bottom of second pipeline.

10. according to the device of claim 6 or 9 described processing coked waxy oils, it is characterized in that: also comprise a revivifier, link to each other by pipeline with described reaction zone down with the described reaction zone of going up respectively; Set up a catalyst mix jar on described revivifier next door, this catalyst mix jar connects stripping stage and regenerator bottoms respectively by two inclined tubes, also connects described pre lift zone by an inclined tube.

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