CN100455640C - Hydrocarbons raw material double lifting leg catalytic conversion apparatus - Google Patents
Hydrocarbons raw material double lifting leg catalytic conversion apparatus Download PDFInfo
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- CN100455640C CN100455640C CNB2005100179084A CN200510017908A CN100455640C CN 100455640 C CN100455640 C CN 100455640C CN B2005100179084 A CNB2005100179084 A CN B2005100179084A CN 200510017908 A CN200510017908 A CN 200510017908A CN 100455640 C CN100455640 C CN 100455640C
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Abstract
The invention relates the hydrocarbons double-lift leg catalytic conversion device. The device comprises heavy oil lift leg reactor and petrol lift leg reactor. The exit of petrol lift leg is connected with petrol gas-oil separator in depressor, the lower exit of the separator is connected with catalyst storage area, the storage area is connected with the bottom or middle heavy oil lift leg reactor; the exit of heavy oil lift leg reactor is connected with heavy oil gas-oil separator in the same depressor, the depressor is connected with regenerator by stripping device and stand pipe, the regenerator is connected with the bottom of heavy oil lift leg reactor by stand pipe and petrol lift leg reactor. On the bottom of catalyst storage area there is exit connected with catalyst and stripping device. The invention can improve the heavy oil reaction rate by 1-2%, and reduce the olefin content by 15%. The device has advantages of simple device and low cost.
Description
Technical field
The invention belongs to petroleum hydrocarbon raw material catalytic conversion technique field, particularly a kind ofly can improve the catalytic cracking yield, improve quality product, particularly reduce the catalysis conversion method and the device of content of olefin in gasoline.
Background technology
Catalytic cracking is the important secondary processing means of oil heavy ends.Especially in China, about 80% gasoline is from catalytic cracking unit.How to improve the efficient of catalytic cracking unit, it is very important to improve production quality.Conventional catalyst cracking method and device use riser reactor, and its reaction process exists significantly not enough.At first be that the regenerator temperature is higher, limited the agent-oil ratio and the heavy oil preheating temperature of reaction; Next is that the latter half of efficient of riser reactor is lower; In addition, the quality product of catalytic cracking unit is unsatisfactory, and especially (v) % does not meet environmental requirement to content of olefin in gasoline 45～55 mostly.
The latter half of inefficient major reason of riser reactor is a catalyst deactivation.In order to improve the reaction efficiency of heavy raw oil in catalytic cracking riser reactor, the invention of the latter half of catalyst activity of multiple raising reactor has appearred in succession.Chinese patent CN1302843A has proposed catalyzer relay scheme, promptly carry out the catalyzer displacement at the riser tube middle part, the catalyzer that reacted is all isolated, be replaced as high reactivity, low-temp recovery catalyzer, make the riser tube second half section return to preceding half section efficient fully through lowering the temperature and handling.99109193.0,02149313.8 and 200410060430.9 of Chinese patent application has proposed half-way house, the low activity catalyst of reacting in the riser reactor bottom does not displace, only pass through to replenish part high reactivity, low-temp recovery catalyzer to the riser tube middle part, thus the suitable latter half of efficient of raising reactor.
Contact temperature, rising agent oil ratio in order to improve catalyzer with heavy raw oil contact condition, reduction, Uop Inc. has announced the RxCAT technology in the NPRA2004 meeting.Its essence is to draw and get back to the riser tube bottom, mixes, make the temperature reduction of regenerator, again with the heavy oil contact reacts with the high temperature regeneration agent from the low temperature reclaimable catalyst of stripping stage after with partial reaction.But, when reducing catalyst temperature, rising agent oil ratio, also reduced activity of such catalysts because the reacted reclaimable catalyst activity of heavy oil is very low.
U.S. Pat P3784463 and Chinese patent application 02116786.9,02139064.9,02123817.0 have been announced and have been built riser reactor in addition, make gasoline carry out the method for catalytic conversion reaction again in independent riser tube.Its benefit is to reduce content of olefin in gasoline significantly, or is converted into low charcoal product, forms industrial chemicals.
Gasoline reaction response heat is less, green coke also seldom, the catalyzer that reacted still has higher activity.But in existing gasoline reaction process, directly contact with the high temperature regeneration agent because of gasoline on the one hand, the reaction process temperature difference is bigger, causes the product selectivity variation; On the other hand reaction back low temperature, lowly contain charcoal, highly active catalyzer is not well utilized, but has directly sent into revivifier, and is unfavorable to regenerating on the contrary.
Summary of the invention
The object of the invention is to provide a kind of can improve the heavy raw oil reaction efficiency, improves the device total recovery, catalytic convention design that again can the improvement purpose product quality.
For reaching above-mentioned purpose, the present invention adopts following technical scheme: a kind of hydrocarbons raw material double lifting leg catalytic conversion apparatus, comprise heavy oil riser reactor and gasoline rising pipe reactor, the gasoline rising pipe reactor outlet is connected with the first separator of the gasoline reaction oil gas in the settling vessel, outlet pipe connects gasoline post catalyst reaction storage area under this separator, and this storage area is connected with heavy oil riser reactor bottom or/and middle part; The outlet of heavy oil riser reactor is connected with the first separator of the heavy oil reaction oil gas in the same settling vessel, settling vessel connects revivifier by stripper, regeneration standpipe, and revivifier is connected with heavy oil riser reactor bottom with the gasoline rising pipe reactor by the regeneration standpipe.
Bottom, gasoline post catalyst reaction storage area is provided with the catalyst stream outlet, and this spout is connected with stripper.
The reacted catalyst inlet of gasoline is arranged at 6～15m place, heavy oil riser tube opening for feed top.
Heavy oil riser reactor middle part catalyzer admission port is fluidized-bed pattern or conventional riser tube pattern with top.
The present invention is by being provided with dividing plate in settling vessel, space in the settling vessel is divided into two districts, less district is used to store the reacted catalyzer of gasoline, and bigger district is connected with stripping stage, is used to install heavy oil riser tube work off one's feeling vent one's spleen solid separator and reaction oil gas primary cyclone.The catalyzer cyclonic separator is established in the gasoline rising pipe outlet, isolated catalyzer is sent into gasoline catalyzing agent storage area in the settling vessel from dipleg, reacted catalyzer of gasoline and the reacted catalyzer of heavy oil are separated, and the reacted catalyzer of heavy oil then directly enters the stripper of settling vessel below.Between settling vessel gasoline catalysts storage area and heavy oil riser tube middle part and bottom catalyst transport is set, makes the reacted catalyzer of gasoline return the heavy oil riser tube and carry out the heavy oil reaction again.Its amount of returning is controlled by guiding valve respectively.More than the reacted catalyzer of part gasoline of heavy oil reaction needed, the opening by settling vessel internal partition top or bottom enters catalyst stripping equipment.When being main purpose with the raising yield, the reacted catalyzer of gasoline preferentially or is all sent into heavy oil riser tube bottom, its catalyst transport amount is pressed 600～650 ℃ of controls of catalyst mix temperature before heavy oil riser tube bottom does not contact with stock oil, preferably is controlled at 620～650 ℃.When being main purpose with the content of olefin in gasoline that reduces the generation of heavy oil riser tube, the reacted catalyzer of gasoline preferentially or is all sent into heavy oil riser tube middle part, and its catalyst transport amount is no more than 30 with the reduction of heavy oil riser tube temperature of reaction.When being main purpose with the content of olefin in gasoline that reduces the generation of heavy oil riser tube, heavy oil riser tube middle part is advanced agent mouth (catalyst inlet) and is adopted fluidized-bed form riser tube with top, and gas superficial flow velocity 5～10m/s carries out conversion of olefines so that time enough to be arranged; When being main purpose to improve the heavy oil reaction yield, it is conventional riser tube with top that the agent mouth is advanced at heavy oil riser tube middle part, gas superficial flow velocity 10～20m/S.
Reaction unit of the present invention comprises two riser reactors, shared reacting-settler, stripping stage, catalyst regenerator, catalyst transport.Riser reactor is by catalyst mix, pre lift zone, and conversion zone, outlet pipe, catalyzer enter pipe and form.
Heavy oil reaction process of the present invention is: regenerated catalyst enters the heavy oil reactor through the pre lift zone of regeneration standpipe below raw material inlet; Simultaneously, enter heavy oil riser tube bottom, two burst catalyst mix, catalyst stream that formation temperature than regenerated catalyst low from settling vessel through transfer lime through the part low temperature catalyst behind the gasoline reactor reaction; Stock oil and recycle stock enter riser tube after nozzle atomization, contact with catalyzer and up along reactor, carry out catalytic cracking reaction simultaneously; The reacted catalyzer of part gasoline also enters heavy oil riser tube middle part through transfer lime, mixes with the reactant flow in the riser tube, and the agent-oil ratio in the heavy oil riser tube is improved, and has also improved catalyst activity simultaneously, improves riser tube efficient, improves quality product; Heavy oil enters settling vessel after finishing reaction, isolates catalyzer at settling vessel, and reaction oil gas is discharged through pipeline; Isolated catalyzer in stripper by steam displace carry oil gas secretly after, return revivifier through regeneration standpipe.
Gasoline reaction process of the present invention is: regenerated catalyst enters the gasoline reactor through the regeneration standpipe below the gasoline admission port, gasoline enters from inlet after nozzle atomization, contact also uply with catalyzer, carries out catalytic conversion reaction; Reaction oil gas enters the first cyclonic separator of gasoline in the settling vessel, and isolated catalyzer enters gasoline catalyzing agent storage area, and gasoline oil gas then again behind the further separating catalyst of cyclone separator, is discharged reactive system; The reacted catalyzer of the gasoline of storage area enters heavy oil reactor bottom and middle part respectively through transfer lime.
Catalyzer in the revivifier of the present invention enters gasoline and heavy oil reactor through different pipeline (regeneration standpipe), but returns revivifier through common stripper and regeneration standpipe.Gasoline reactive moieties of the present invention is only used riser reactor, does not establish gasoline reacting-settler and catalyst stripping equipment.
Heavy oil of the present invention and gasoline two cover reactive systems make heavy raw oil and gasoline respectively in reactor separately, carry out catalyzed conversion by the reaction conditions of requirement separately; The reacted catalyzer of gasoline no longer directly enters revivifier, but enters the heavy oil reactor, realizes that catalyzer is shared fully at two reactive systems; Need not to make regenerated catalyst and other medium heat exchange or cooling, can realize the low contact of heavy oil temperature, high agent-oil ratio reaction operating mode; Because the gasoline temperature of reaction is generally lower, the reacted catalyst make-up of gasoline can improve the activity of heavy oil catalysts to heavy oil riser tube middle part, improves riser tube efficient.
The present invention only uses a settling vessel, adopts sectional way to realize the separation of heavy oil reaction and gasoline catalysts.The present invention realizes the serial connection of gasoline reaction and heavy oil catalysts, makes the reacted catalyzer of gasoline be optimized the heavy oil reaction conditions.The present invention need not special regeneration, uses simple conventional regeneration device to get final product.Device is simple, reduces investment outlay.
The present invention can make the heavy oil reaction conversion ratio improve 3～5 percentage points, and the heavy oil reaction generates content of olefin in gasoline and reduces by 10～20 percentage points (v); Gasoline rising pipe makes content of olefin in gasoline be reduced to 20%, and (v), octane value increases a unit.
Description of drawings
Fig. 1 is structural representation of the present invention (heavy oil reaction riser reactor adopts conventional riser tube pattern, between settling vessel and heavy oil riser tube bottom and the middle part gasoline post catalyst reaction transfer lime is set all); Fig. 1-1 is that gasoline post catalyst reaction storage area and settling vessel other parts concern synoptic diagram; Fig. 2 is second kind of structural representation of the present invention (heavy oil reaction riser reactor adopts the fluidized-bed pattern, produces content of olefin in gasoline to reduce the heavy oil reaction, between settling vessel and heavy oil riser tube bottom and the middle part gasoline post catalyst reaction transfer lime is set all); Fig. 3 is the third structural representation of the present invention (heavy oil reaction riser reactor adopts conventional riser tube pattern, and settling vessel and heavy oil riser tube bottom are provided with gasoline post catalyst reaction transfer lime); Fig. 4 is the 4th kind of structural representation of the present invention (heavy oil reaction riser reactor adopts conventional riser tube pattern, between settling vessel and the heavy oil riser tube middle part gasoline post catalyst reaction transfer lime is set).
Embodiment
180～250 ℃ stock oil, recycle stock about 350 ℃, slurry oil by nozzle atomization after, 11 enter heavy oil riser reactor 10 through entering the mouth, with gasified after the catalyst mix, with the first flow velocity about 10m/s along riser tube to the top limit reaction of flowing, under 500～550 ℃ of temperature environments, finished catalytic cracking reaction through 2～4 seconds left and right sides time, enter settling vessel 30 from outlet pipe 18 then, isolated catalyzer by gas- solid separator 31,32, oil gas is through gas pipeline 33 bleeders; 40～150 ℃ gasoline 21 enters gasoline rising pipe reactor 20 through entering the mouth, contact with catalyzer, after the gasification, with the upwards mobile limit reaction of the speed limit of 7～15m/s, under 400～530 ℃ of temperature, agent-oil ratio 6～12 environment, after 3～6s time is finished reaction, enter settling vessel 30 through outlet pipe 28, isolated catalyzer by gas-solid separator 35, through gas pipeline 33 bleeders; Regenerated catalyst in the revivifier 70 enters each reactor bottom through standpipe 71,71B respectively, after finishing reaction, enter reacting-settler 30 through heavy oil riser reactor outlet pipe 18, carry out gas solid separation, isolated catalyzer then contacts with steam in stripper 50, displaces entrained oil gas, enters revivifier from regeneration standpipe 80 then, contact under 650～720 ℃ of temperature with air 75 and to regenerate, finish circulation.Enter the regenerated catalyst of gasoline rising pipe reactor 20, after finishing reaction, in settling vessel 30, told by the first cyclonic separator 35 of gasoline oil gas, enter gasoline catalyzing agent storage area 37 through dipleg 36, send into heavy oil riser reactor 10 from catalyst transport 14,14B again, 15,15B is a guiding valve, and 16B is gasoline post catalyst reaction inlet; 38 is dividing plate, and 39 is set opening on gasoline post catalyst reaction storage area 37 base plates, makes unnecessary catalyzer enter revivifier.The temperature of reaction of heavy oil cracking and gasoline reaction is by guiding valve 73,73B control.16,26 be respectively heavy oil riser reactor and gasoline rising pipe reactor regenerated catalyst inlet pipe, 13,23 for promoting medium, and 81 is guiding valve.
Embodiment 1, reaction mass are: the defeated atmospheric residue 100t/h heavy oil of pipe, and gasoline feeding is that heavy oil reacts self-produced gasoline; The olefin(e) centent that main purpose makes the heavy oil reaction produce gasoline reduces.220 ℃ of heavy oil preheatings, 40 ℃ in gasoline; Raw material oil content four tunnel enters heavy oil reaction riser tube, and recycle stock divides two-way to enter heavy oil reaction riser tube above the stock oil inlet, and gasoline divides two-way to enter the gasoline reactor; The reacted catalyzer of gasoline enters the heavy oil riser tube from stock oil inlet top 10m; 515 ℃ of gasoline catalyzing agent admission port below heavy oil cracking temperature of reaction, reaction times 0.8s; The part that gasoline catalyzing agent admission port is above, 490 ℃ of heavy oil temperature of reaction, reaction times 2.2s; 430 ℃ of gasoline temperature of reaction, reaction times 3.5s; 690 ℃ of regeneration temperatures.
Present embodiment uses the device of accompanying drawing 1 or accompanying drawing 4.When the device that uses shown in the accompanying drawing 1, close the valve 15 on the catalyst transport 14.In this device, gasoline rising pipe reactor 20 at other settling vessel 30 shared in parallel of heavy oil riser reactor 10 (adopting conventional riser tube pattern) and revivifier 70 with it, gasoline rising pipe reactor 20 outlet and settling vessel 30 interior first cyclonic separators 35 are connected, make and finish the gasoline catalyst for reaction and be introduced into the catalyst stores district 37 that in settling vessel 30, is separated out by dividing plate 38, enter heavy oil riser tube middle part from catalyst transport 14B again.
Comparative Examples: adopt existing independently double lifting leg reaction technology, conventional riser tube is used in gasoline reaction and heavy oil reaction; The reacted catalyzer of gasoline directly enters revivifier; The different of heavy oil reactive moieties and the embodiment of the invention are that heavy oil riser tube middle part is make-up catalyst not.
The contrast reaction result provides in table 1.As can be seen, under identical reaction conditions, heavy oil reaction liquid product yield of the present invention has increased by 0.5 percentage point, generates gasoline olefin and reduces by 13 percentage points.
Embodiment 2, reaction mass are: grand celebration atmospheric residue 100t/h heavy oil, and gasoline feeding is the catalytic gasoline of other devices, 40t/h; 220 ℃ of heavy oil preheatings, 40 ℃ in gasoline; The heavy oil reaction raw materials divides four the tunnel to enter riser tube, and gasoline divides two-way to enter reactor; The reacted catalyzer of gasoline enters the bottom and the middle part of heavy oil reactor respectively; The ratio that enters heavy oil riser tube bottom is reduced to 640 ℃ of controls according to the mixing temperature that heavy oil riser tube reaction raw materials enters procatalyst, and redundance enters the heavy oil riser tube from the middle part; 510 ℃ of the heavy oil cracking temperature of reaction of gasoline catalyzing agent admission port below, reaction times 1.1s; The part that gasoline catalyzing agent admission port is above, 490 ℃ of heavy oil temperature of reaction, oil gas flow velocity 6m/s, reaction times 3.5s; 430 ℃ of gasoline temperature of reaction, reaction times 3.0s; 690 ℃ of regeneration temperatures.
The present embodiment apparatus structure is seen Fig. 4, as different from Example 1, gasoline post catalyst reaction transfer lime 14B only is set between settling vessel 30 and heavy oil riser reactor 10 middle parts.
Comparative Examples: embodiment 1 as a comparison case, what Comparative Examples heavy oil reactive moieties was different with embodiment is, the gasoline catalyzing agent all enters heavy oil riser tube middle part.Heavy oil riser tube middle part tonic mouth still is conventional high flow rate operating mode with top.
Comparing result sees Table 2.From table 2 data as can be seen, heavy oil reaction liquid product yield of the present invention has increased by 0.8 percentage point, and gasoline olefin maintains an equal level.
Table 1, embodiment 1 scheme and prior art contrast
Table 2, embodiment 2 schemes and embodiment 1 contrast
Claims (4)
1, a kind of hydrocarbons raw material double lifting leg catalytic conversion apparatus, it is characterized in that, comprise heavy oil riser reactor and gasoline rising pipe reactor, the gasoline rising pipe reactor outlet is connected with the first separator of the gasoline reaction oil gas in the settling vessel, outlet pipe connects gasoline post catalyst reaction storage area under this separator, and this storage area is connected with heavy oil riser reactor bottom or/and middle part; The outlet of heavy oil riser reactor is connected with the first separator of the heavy oil reaction oil gas in the same settling vessel, settling vessel connects revivifier by stripper, regeneration standpipe, and revivifier is connected with heavy oil riser reactor bottom with the gasoline rising pipe reactor by the regeneration standpipe.
2, device as claimed in claim 1 is characterized in that, bottom, gasoline post catalyst reaction storage area is provided with the catalyst stream outlet, and this spout is connected with stripper.
3, device as claimed in claim 1 or 2 is characterized in that, the reacted catalyst inlet of gasoline is arranged at 6～15m place, heavy oil riser tube opening for feed top.
4, device as claimed in claim 3 is characterized in that, heavy oil riser reactor middle part catalyzer admission port is fluidized-bed pattern or conventional riser tube pattern with top.
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| Application Number | Priority Date | Filing Date | Title |
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| CNB2005100179084A CN100455640C (en) | 2005-08-24 | 2005-08-24 | Hydrocarbons raw material double lifting leg catalytic conversion apparatus |
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| Application Number | Priority Date | Filing Date | Title |
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| CNB2005100179084A CN100455640C (en) | 2005-08-24 | 2005-08-24 | Hydrocarbons raw material double lifting leg catalytic conversion apparatus |
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| CN1919971A CN1919971A (en) | 2007-02-28 |
| CN100455640C true CN100455640C (en) | 2009-01-28 |
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| CN104342196B (en) * | 2013-08-03 | 2016-06-08 | 中石化洛阳工程有限公司 | A kind of catalyst cracking method and device thereof |
| CN104342197B (en) * | 2013-08-03 | 2016-06-08 | 中石化洛阳工程有限公司 | A kind of double lift pipe catalytic cracking method and device thereof |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP0493932A1 (en) * | 1990-12-31 | 1992-07-08 | Mobil Oil Corporation | Heavy oil catalytic cracking process and apparatus |
| CN1621494A (en) * | 2003-11-28 | 2005-06-01 | 中国石油化工股份有限公司 | Catalytic cracking process for preparing high-grade gasoline |
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Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP0493932A1 (en) * | 1990-12-31 | 1992-07-08 | Mobil Oil Corporation | Heavy oil catalytic cracking process and apparatus |
| CN1621494A (en) * | 2003-11-28 | 2005-06-01 | 中国石油化工股份有限公司 | Catalytic cracking process for preparing high-grade gasoline |
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