CN1948440A - Catalytic conversion method of double reactor and its device - Google Patents
Catalytic conversion method of double reactor and its device Download PDFInfo
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- CN1948440A CN1948440A CN 200510018086 CN200510018086A CN1948440A CN 1948440 A CN1948440 A CN 1948440A CN 200510018086 CN200510018086 CN 200510018086 CN 200510018086 A CN200510018086 A CN 200510018086A CN 1948440 A CN1948440 A CN 1948440A
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- 238000006243 chemical reaction Methods 0.000 title claims abstract description 107
- 238000000034 method Methods 0.000 title claims abstract description 16
- 230000003197 catalytic effect Effects 0.000 title claims abstract description 8
- 239000000295 fuel oil Substances 0.000 claims abstract description 100
- 239000003921 oil Substances 0.000 claims abstract description 64
- 238000004523 catalytic cracking Methods 0.000 claims abstract description 13
- 239000002994 raw material Substances 0.000 claims abstract description 4
- 239000003502 gasoline Substances 0.000 claims description 145
- 239000003054 catalyst Substances 0.000 claims description 38
- 230000008929 regeneration Effects 0.000 claims description 22
- 238000011069 regeneration method Methods 0.000 claims description 22
- 238000000926 separation method Methods 0.000 claims description 14
- 239000007787 solid Substances 0.000 claims description 11
- 235000008733 Citrus aurantifolia Nutrition 0.000 claims description 8
- 235000011941 Tilia x europaea Nutrition 0.000 claims description 8
- 239000004571 lime Substances 0.000 claims description 8
- 238000006555 catalytic reaction Methods 0.000 claims description 5
- 239000000203 mixture Substances 0.000 claims description 4
- 239000002002 slurry Substances 0.000 claims description 4
- 238000010992 reflux Methods 0.000 claims description 3
- 239000002131 composite material Substances 0.000 claims description 2
- 239000003209 petroleum derivative Substances 0.000 claims description 2
- 239000000376 reactant Substances 0.000 claims description 2
- 239000010743 number 2 fuel oil Substances 0.000 claims 1
- 239000003208 petroleum Substances 0.000 abstract 11
- 230000008878 coupling Effects 0.000 abstract 3
- 238000010168 coupling process Methods 0.000 abstract 3
- 238000005859 coupling reaction Methods 0.000 abstract 3
- 239000000463 material Substances 0.000 abstract 2
- 230000003134 recirculating effect Effects 0.000 abstract 2
- 230000007420 reactivation Effects 0.000 abstract 1
- 239000000047 product Substances 0.000 description 18
- 150000001336 alkenes Chemical class 0.000 description 13
- 230000035484 reaction time Effects 0.000 description 9
- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 description 8
- 240000006909 Tilia x europaea Species 0.000 description 7
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 6
- 239000003795 chemical substances by application Substances 0.000 description 6
- 239000000571 coke Substances 0.000 description 6
- 230000000052 comparative effect Effects 0.000 description 5
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 description 5
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 description 5
- 239000013049 sediment Substances 0.000 description 5
- 239000005864 Sulphur Substances 0.000 description 4
- 238000002309 gasification Methods 0.000 description 4
- 238000002156 mixing Methods 0.000 description 4
- 239000003153 chemical reaction reagent Substances 0.000 description 3
- 238000010586 diagram Methods 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- TVMXDCGIABBOFY-UHFFFAOYSA-N octane Chemical compound CCCCCCCC TVMXDCGIABBOFY-UHFFFAOYSA-N 0.000 description 3
- 230000001172 regenerating effect Effects 0.000 description 3
- 230000000630 rising effect Effects 0.000 description 3
- 239000003610 charcoal Substances 0.000 description 2
- 239000012295 chemical reaction liquid Substances 0.000 description 2
- 239000004567 concrete Substances 0.000 description 2
- 229910052717 sulfur Inorganic materials 0.000 description 2
- 239000011593 sulfur Substances 0.000 description 2
- 238000000889 atomisation Methods 0.000 description 1
- 230000008901 benefit Effects 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 239000007795 chemical reaction product Substances 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 238000005336 cracking Methods 0.000 description 1
- 230000002708 enhancing effect Effects 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 239000012467 final product Substances 0.000 description 1
- 239000002010 green coke Substances 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 239000003317 industrial substance Substances 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 238000003541 multi-stage reaction Methods 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 230000009466 transformation Effects 0.000 description 1
- 238000009834 vaporization Methods 0.000 description 1
- 230000008016 vaporization Effects 0.000 description 1
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Abstract
This invention provides a catalytic cracking method, and it will make sure that raw material oil and petroleum react separately in their own demands by using coupling reactors. In order to improve agent-oil ratio, the accelerant with low temperature from petroleum reaction reenters into the pre-upgrading section of raw material oil reaction. It will low the temperature of accelerant of petroleum reaction and improve agent-oil ratio before low temperature accelerant from petroleum reaction recirculating into petroleum reactor before feeding material. The equipment of this catalytic cracker uses coupling reactor, and the accelerant after the reaction of petroleum will be directly send into the pre-promotion section of heavy oil reactivation from petroleum reactor by accelerant transport pipe between the petroleum reactor and heavy oil reactor. The accelerant recirculating pipe designed with petroleum reactor to make part of the accelerant return to petroleum reactor before feeding material. The catalytic cracking equipment is a settling vessel, which will separate the oil gas from different reactor and enter their own fractionating tower to form the program of single settling vessel and coupling fractionating tower to receive pure petroleum upgrading product.
Description
Technical field
The invention belongs to petroleum hydrocarbon catalytic conversion technique field, particularly a kind ofly can improve catalytic cracking yield, the catalysis conversion method that improves quality product and device.
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 product yield 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 reagent oil ratio and heavy oil preheating temperature; Influence product yield; In addition, the quality product of catalytic cracking unit is unsatisfactory, and especially (v) %, octane value is lower mostly 45～55 for content of olefin in gasoline.
In order to improve catalyzer and heavy raw oil contact condition, reduce the contact temperature, the rising agent oil ratio, Uop Inc. has proposed 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.
For satisfying environmental protection, and to the demand of Chemicals rapid growth, effective means is to utilize catalytic cracking unit that gasoline is transformed once more.U.S. Pat P3784463 and Chinese patent application 02116786.9,02139064.9 and 02123817.0 have proposed to build in addition riser reactor, 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, boosting of octane rating, or be converted into low charcoal alkene, industrial chemicals such as propylene enhancing.
The gasoline endothermic heat of reaction 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, and agent-oil ratio is less, 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.
The method that patent CN1498950A re-uses the reacted catalyst member of gasoline is sent into the reacted catalyzer of part gasoline the middle part of heavy oil reactor from petrol sediment bulb, other parts are still sent into revivifier.But still need to build petrol sediment bulb, and device is complicated, and investment is big, is difficult for implementing.
Summary of the invention
The object of the invention is to provide a kind of petrol sediment bulb of not establishing, not only realized that heavy raw oil and gasoline separate and reacted the improvement purpose product quality, but also utilize again by the reacted catalyzer of gasoline and to realize stock oil and low temperature, the high agent-oil ratio reaction conditions of contact of gasoline, thus the catalysis conversion method and the device of raising device total recovery.
For reaching above-mentioned purpose, the present invention adopts following technical scheme:
Catalytic cracking reaction-regenerating unit comprises and carries out heavy oil catalytic cracking reaction and the gasoline reactive moieties of catalytic conversion reaction again, shared settling vessel and catalyst regenerator, fcc raw material oil (heavy oil) and gasoline is reaction separately, and the reacted catalyzer of gasoline continues on for the heavy oil reaction.The gasoline reactor outlet is connected with shared settling vessel, and reaction oil gas is drawn settling vessel through gas pipeline.
A kind of catalytic convention design, reactive moieties comprises gasoline reactor and heavy oil reactor, turning oil such as heavy oil and recycle stock, slurry oil is at heavy oil reactor internal reaction, gasoline is at gasoline reactor internal reaction, two reactors are communicated with by the catalyst transport serial connection, form combination form, from the gasoline reactor, draw the reacted catalyzer of gasoline and send into the pre lift zone of heavy oil reactor, continue to participate in the heavy oil reaction from transfer lime.
The reactor that the gasoline reactor provides for 200510017986.4 patent for application number, be that reactor is riser tube evaporator section and fast fluidized bed conversion zone composite type, contain the catalyzer return line, from reactor, draw a part of catalyzer and return the pre lift zone of gasoline reactor bottom, the catalyst temperature before the gasoline reaction is reduced from return line.
The heavy oil reactor can be the riser tube pattern, and the heavy oil reactor can also be riser tube and the placed in-line combination form of fast bed, also can be the pattern of patent 200410060321.7, and catalyzer can reflux at the middle part.
Establish petrol vapour solid separator (being generally cyclonic separator) in the shared settling vessel, be connected, be used to separate the remainder catalyzer that does not enter the heavy oil reactor with the gasoline reactor outlet.The gasoline reaction oil gas is said
Do not mix, but directly draw, enter gasoline oil gas separation column, obtain pure gasoline reactor product, form the two separation column schemes of single settling vessel through the gasoline gas pipeline with the heavy oil reaction oil gas; Isolated
Catalyzer then enters shared stripping stage, and enters revivifier regeneration through same regeneration standpipe.
Also can establish heavy oil and petrol vapour solid separator (being generally cyclonic separator) in the shared settling vessel, be connected with the gasoline reactor outlet with heavy oil respectively, isolate the catalyzer that carries after, reaction oil gas mixes, and draw through the common gas pipeline, enter follow-up parts such as separation column; Catalyzer then enters shared stripping stage, and enters revivifier regeneration through same regeneration standpipe.
Apparatus of the present invention are used a settling vessel, realize that two catalyst in reactor are shared, and reaction oil gas separately can guarantee that the reacted again product of gasoline is not subjected to the influence of heavy oil reaction.Device is obviously simplified, and is convenient to implement.
Apparatus of the present invention are used a settling vessel, realize that heavy oil and gasoline reactor product separate fully, use separation column separately to carry out product separation, obtain pure gasoline upgrading product.
In the method for the invention, the heavy oil reaction process is: regenerated catalyst partly enters the heavy oil reactor through the pre lift zone of regeneration standpipe below the heavy oil admission port; Simultaneously, draw from the gasoline reactor, send into the pre lift zone of heavy oil reactor, mixing the catalyst stream that formation temperature is lower than regenerated catalyst with regenerated catalyst with first before heavy oil contact through transfer lime through the low temperature catalyst behind the gasoline reactor reaction; Heavy oil enters the heavy oil reactor above pre lift zone, contact with mixed low temperature catalyst and up along reactor, carries out catalytic cracking reaction simultaneously; Reaction oil gas enters reacting-settler with reclaimable catalyst subsequently; After settling vessel was isolated catalyzer, oil gas was discharged from pipeline; Isolated catalyzer in stripper by steam displace carry oil gas secretly after, return revivifier from regeneration standpipe.The present invention is under the constant situation of the regeneration dosage 52B that enters the heavy oil reactor and temperature of reaction, and making the total catalyst levels that participates in reaction is 52B and 19A sum, has increased actual agent-oil ratio.
Gasoline reaction process of the present invention is: regenerated catalyst enters the gasoline reactor through standpipe below the gasoline admission port, mixes with the low temperature catalyst that refluxes from the gasoline reactor, forms about 500～620 ℃ catalyzer; Gasoline contacts with catalyzer after entering reactor, and up, carries out catalytic conversion reaction; The reacted catalyzer of gasoline is drawn from the gasoline reactor, sends into heavy oil reactor pre lift zone through transfer lime, continues to participate in the heavy oil reaction.Reaction oil gas is isolated remaining catalyzer (19B) by gas-solid separator in shared settling vessel after, discharge reactive system.The present invention under the constant situation of the regeneration dosage 52A that enters the gasoline reactor and temperature of reaction, make the total catalyst levels increment that participates in reaction for 52A with 19 with, increased actual agent-oil ratio.
Heavy oil reaction conditions of the present invention is: 480～550 ℃ of temperature of reaction (reactor outlet), agent-oil ratio 8～20, the oil gas mean residence time in reactor 2～6 seconds.The gasoline reaction conditions is: 380～560 ℃ of temperature of reaction (outlet), 500～620 ℃ of reaction procatalyst mixing temperatures, reagent oil ratio 6～20, the mean residence time of oil gas in reactor 2～6 seconds.
Heavy oil of the present invention and gasoline reaction unit make heavy raw oil and gasoline respectively in reactor separately, carry out catalyzed conversion by the reaction conditions of requirement separately, and reaction oil gas is discharged through pipeline separately, is independent of each other; The reacted catalyzer of gasoline no longer directly enters revivifier, but directly 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 reaction operating mode of low contact temperature, high agent-oil ratio; Need not special regeneration, use simple conventional regeneration device to get final product.The present invention can make heavy oil reagent oil ratio improve 30～50%, and transformation efficiency improves 3～5 percentage points; Make the agent-oil ratio of gasoline reaction improve 50～150%, content of olefin in gasoline is reduced to 20%, and (v), octane value increases a unit, and productivity of propylene can reach 10%, and the gasoline loss reduces 30%～50%.
The present invention need not establish petrol sediment bulb.
Description of drawings
Fig. 1 is the distinct device synoptic diagram of heavy oil of the present invention, gasoline reaction oil gas;
Fig. 2 is heavy oil of the present invention and gasoline reaction oil gas blended device synoptic diagram in gas pipeline;
Fig. 3,4, the 5th, combined reactor structural representation of the present invention.
Fig. 6 is the device synoptic diagram that heavy oil gasoline reactor outlet of the present invention directly merges.
The numbering tag content is as follows among the figure: 1 composite reaction part, 10 gasoline reactors; 11 gasoline reactor catalysts inlet, 12 catalyst mix pre lift zones, 13 gasoline rising pipe gasification section; 14 rectification sections, 14A gasoline fast bed conversion zone; 15 gasoline reactant flow transfer limes, 15-1 gasoline reactor outlet; 16,16-1 gasoline catalyzing agent transfer lime; 16-A, 16-B gasoline catalyzing agent guiding valve; 17 catalyzer promote medium; 17-1 promotes the medium inlet in advance; 18 gasoline, 18-1 gasoline inlet; 19,19A, 19B, 52A, 52B catalyst stream; 20 heavy oil reactors; 28 heavy oil, 28-1 heavy oil inlet; 21 heavy oil reactor catalysts inlet; 27 catalyzer promote medium, and 27-1 promotes the medium inlet in advance; 23 high flow rate conversion zones, 24A second conversion zone, 24 rectification sections; 25 logistics transfer limes, 25-1 heavy oil reactor outlet pipe; 3 shared reacting-settlers; 31 gas-solid separators; 32 oil gas pipes, 35 petrol vapour solid separators, 36 gasoline transportation pipe lines; 5 catalyst stripping equipments, 51 regeneration standpipes; 7 revivifiers; 71A, the 71B standpipe of regenerating; 54A, the 54B guiding valve of regenerating; 75 air.
Embodiment
180～250 ℃ heavy oil 28 is by after the nozzle atomization, 28-1 enters riser reactor 20 through inlet, with gasified after about 600～650 ℃ the catalyst mix, upwards flow along riser reactor with the flow velocity about 10m/s (meter per second, down with), under 480～550 ℃ of temperature environments, after 2～6s (second, down together) time is finished reaction, enter settling vessel 3, isolated catalyzer by gas-solid separator 31, oil gas is through gas pipeline 32 bleeders.40～70 ℃ gasoline enters the vaporization section 13 of gasoline reactor 10 through inlet, contact with the catalyzer about 550 ℃～620 ℃, limit upwards mobile limit gasification, enter fast bed reaction zone 14 subsequently, 14A, at 380～560 ℃ (when being main purpose to reduce gasoline olefin, adopt 380～450 ℃ of temperature, when being main purpose with the producing more propylene, adopt 500～560 ℃ of temperature), under agent-oil ratio 6～20 environment, after 2～6s time is finished reaction, reaction oil gas enters settling vessel 3, is divided 35 catalyzer of carrying secretly by gas-solid separator in going out oil gas, through gas pipeline 36 bleeders.Interior about the 700 ℃ regenerated catalyst of revivifier 7 is respectively through standpipe 71A, 71B enters two reactor bottoms, after finishing reaction, enter shared settling vessel through the heavy oil reactor, carry out gas solid separation, isolated catalyzer then contacts with steam in stripper 5, enters revivifier from regeneration standpipe 51 after displacing entrained oil gas, contact under 660～720 ℃ of temperature with air and to regenerate, finish circulation.Enter the catalyzer of gasoline reactor 10, finish reaction after, do not enter revivifier 7, but send into heavy oil reactor 20 through transfer lime.The temperature of reaction procatalyst is by guiding valve 16-A control in the gasoline reactor, and in the heavy oil reactor, the temperature of reaction procatalyst is controlled by guiding valve 16-B.
According to the present invention, can form multiple concrete catalysis conversion method: (1) gasoline and heavy oil reactor use conventional riser tube shown in Figure 3, and the reacted catalyzer of gasoline all enters heavy oil riser tube bottom, participates in whole heavy oil reaction process.(2) gasoline and heavy oil reactor use conventional riser tube, the reacted catalyzer separated into two parts of gasoline, and a part (19A) enters heavy oil riser tube bottom, participates in whole heavy oil reaction process; Another part (19B) is in settling vessel and gas-oil separation.(3) gasoline reactor use application number shown in Figure 4 is the reactor of 200510017986.4 patents.(4) in above embodiment, heavy oil riser tube middle part changes the fluidized-bed form into, as shown in Figure 5.
The concrete application example of the present invention is as follows:
The device that uses in the present embodiment is seen Fig. 1.Wherein reactor partly uses pattern shown in Figure 4.Primary cyclone 35 is established in 10 outlets of gasoline reactor.The gasoline reaction oil gas is sent into follow-up gasoline oil gas separation column through independent gas pipeline 36, obtains the reacted again product of pure gasoline.
Comparative Examples: adopt existing independently double lifting leg, two settling vessels, two separation column technology.The heavy oil reactive moieties and the embodiment of the invention do not exist together, and the heavy oil reaction only contacts with high-temperature regenerated catalyst.What the gasoline reactive moieties was different with embodiment is, from the high temperature catalyst of revivifier directly and the gasoline contact reacts, the reacted catalyzer of gasoline enters revivifier separately, and other is provided with independent settling vessel.
Comparative Examples needs to establish petrol sediment bulb more.
Product 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 1.4 percentage points, generates gasoline olefin and reduces by 8 percentage points; Gasoline is reaction result and prior art ratio again, and olefin(e) centent is low by 20%, and sulphur content is low by 10%, and coke and dry gas overall yield descend 40%.
Embodiment 2.Reaction mass is: grand celebration atmospheric residue, 100t/h heavy oil, gasoline feeding are that heavy oil reacts self-produced gasoline; 220 ℃ of heavy oil preheatings, 40 ℃ in gasoline; The heavy oil reactor is the riser tube form, and the gasoline reactor is riser tube gasification section and fast fluidized bed series connection form; Heavy oil divides four the tunnel to enter riser tube, and gasoline divides two-way to enter reactor; 515 ℃ of heavy oil temperature of reaction, reaction times 2.5s; 525 ℃ of gasoline temperature of reaction, reaction times 4s, wherein gasoline is at gasification section residence time 0.5s, the residence time 3.5s in the fast fluidized bed of middle part; Oil gas apparent velocity 4.0m/s in the fluidized-bed; 620 ℃ of heavy oil riser tube reaction procatalyst mixing temperatures, 620 ℃ of gasoline reactor internal reaction procatalyst temperature; 690 ℃ of regeneration temperatures.The device form that uses is seen Fig. 1, and wherein reactor partly uses pattern shown in Figure 4.
Comparative Examples: what the heavy oil reactive moieties was different with embodiment is that the heavy oil reaction only contacts with high-temperature regenerated catalyst.What the gasoline reactive moieties was different with embodiment is, from the high temperature catalyst of revivifier directly and the gasoline contact reacts, reactor is the riser tube pattern in the prior art, reaction times 2.2s.
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 1.7 percentage points, and gasoline olefin reduces by 5 percentage points; After gasoline reacted again, olefin(e) centent was suitable, and productivity of propylene is suitable, and sulphur content is reduced to 220ppm from 400ppm, reduced by 45%, and dry gas adds coke yield and descends 33%.
Table 1, embodiment 1 scheme and prior art contrast
| Project | Comparative Examples | Embodiment |
| The heavy oil temperature of reaction, ℃ gasoline temperature of reaction, ℃ regeneration temperature, ℃ heavy oil reaction times, the s gasoline reaction times, s heavy oil reactor product: % (w) dry gas liquefied gas gasoline, diesel slurry oil coke loss heavy oil reaction quality of gasoline sulphur, ppm alkene, % (v) gasoline reaction result: sulfur in gasoline, alkene in the ppm gasoline, % (v) coke+dry gas, % (w) | 500 430 690 2.5 3.0 3.5 14.0 41.0 26.5 5.0 9.5 0.5 600 50 400 18 2.5 | 500 430 690 2.5 3.0 3.0 14.2 41.5 27.2 4.4 9.2 0.5 580 42 370 15 1.5 |
Table 2, embodiment 2 schemes and prior art contrast
| Project | Comparative Examples | Embodiment |
| The heavy oil temperature of reaction, ℃ gasoline temperature of reaction, ℃ regeneration temperature, ℃ heavy oil reaction times, the s gasoline reaction times, s heavy oil reactor product: % (m) dry gas liquefied gas gasoline, diesel slurry oil coke loss heavy oil reaction quality of gasoline sulphur, ppm alkene, % (v) gasoline reaction result sulfur in gasoline, alkene in the ppm gasoline, % (v) gasoline productivity of propylene, % (m) dry gas+coke, % (m) | 515 550 690 2.5 2.2 4.0 18.0 36.5 26.0 5.0 10.0 0.5 600 43 400 13 8.5 6.0 | 515 525 690 2.5 4.0 3.2 16.5 38.5 27.2 4.8 9.3 0.5 580 38 220 14 8.0 4.0 |
Claims (10)
1, a kind of catalysis conversion method of petroleum hydrocarbon and device, it is characterized in that, catalytic cracking reaction-regenerating unit comprises and carries out heavy oil catalytic cracking reaction and gasoline reactive moieties, shared settling vessel and the catalyst regenerator of catalytic conversion reaction again, fcc raw material oil (heavy oil) and gasoline is reaction separately, the reacted catalyzer of gasoline continues on for the heavy oil reaction, the gasoline reactor outlet is connected with shared settling vessel, and reaction oil gas is drawn settling vessel through gas pipeline.
2, the method for claim 1 and device, it is characterized in that, reactive moieties comprises gasoline reactor and heavy oil reactor, turning oil such as heavy oil and recycle stock, slurry oil is at heavy oil reactor internal reaction, gasoline is at gasoline reactor internal reaction, and two reactors are communicated with the catalyst transport serial connection, form combination form, from the gasoline reactor, draw the reacted catalyzer of gasoline and send into the pre lift zone of heavy oil reactor, make the reacted catalyzer of gasoline continue to participate in the heavy oil reaction from transfer lime.
3, device as claimed in claim 2 is characterized in that, the gasoline reactor is provided with the catalyzer return line, draws a part of catalyzer and return the pre lift zone of gasoline reactor bottom from return line from reactor, and the catalyst temperature before the gasoline reaction is reduced.
4, device as claimed in claim 3, it is characterized in that the reactor that the patent of gasoline reactor request for utilization numbers 200510017986.4 provides is riser tube evaporator section and fast fluidized bed conversion zone composite type, contain the catalyzer return line, the preceding catalyst temperature of gasoline reaction is reduced.
5, device as claimed in claim 2 is characterized in that, the heavy oil reactor is the riser tube pattern.
6, device as claimed in claim 5 is characterized in that, the heavy oil reactor is riser tube and fast bed series connection pattern, also can be the pattern of patent 200410060321.7, and catalyzer can reflux at the middle part.
7, the method for claim 1 and device is characterized in that, establish the gasoline cyclonic separator in the settling vessel, are connected with the gasoline reactor outlet, and the gasoline reaction oil gas is not anti-with heavy oil
8, answer oil gas to mix, but after will not entered the remainder catalyst separating of heavy oil reactor, directly draw settling vessel through the gasoline gas pipeline by cyclonic separator, enter follow-up gasoline oil gas separation column, obtain pure gasoline reactor product, form two separation column schemes of a settling vessel; The catalyzer that is separated from the gasoline reaction oil gas then enters shared stripping stage, and enters revivifier regeneration from regeneration standpipe.
9, method and apparatus as claimed in claim 7, it is characterized in that, establish two bunker A oil gas-solid separators in the settling vessel, if one-level gasoline cyclonic separator, after isolating the catalyzer that carries, the gasoline reaction oil gas does not enter settling vessel, and enters the heavy oil gas pipeline behind the heavy oil gas-solid separator of the second stage, mix with heavy oil oil gas, and draw through this gas pipeline; Catalyzer then enters shared stripping stage, and enters revivifier regeneration through same regeneration standpipe.
9, method and apparatus as claimed in claim 8, it is characterized in that the heavy oil of reactive moieties and gasoline reactor outlet directly merge, reactant flow enters shared settling vessel through same pipeline, after being told catalyzer by shared gas solid separation system, oil gas is drawn from pipeline.
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| Application Number | Priority Date | Filing Date | Title |
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| CNB2005100180861A CN100519703C (en) | 2005-10-12 | 2005-10-12 | Catalytic conversion method of double reactor and its device |
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| CNB2005100180861A CN100519703C (en) | 2005-10-12 | 2005-10-12 | Catalytic conversion method of double reactor and its device |
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Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101760228A (en) * | 2008-12-25 | 2010-06-30 | 中国石油化工股份有限公司 | Catalytic conversion method for preparing propylene and high octane gasoline |
| CN101993709A (en) * | 2009-08-11 | 2011-03-30 | 中国石化集团洛阳石油化工工程公司 | Catalytic cracking method and device thereof |
| CN101993708A (en) * | 2009-08-11 | 2011-03-30 | 中国石化集团洛阳石油化工工程公司 | Catalytic cracking method and device |
| CN102373079A (en) * | 2010-08-19 | 2012-03-14 | 中国石油化工股份有限公司 | Catalytic conversion method for increasing low-carbon olefin production |
| CN101591562B (en) * | 2009-06-25 | 2012-09-26 | 中国石油化工集团公司 | Fluid catalytic cracking method and device thereof |
-
2005
- 2005-10-12 CN CNB2005100180861A patent/CN100519703C/en not_active Expired - Fee Related
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101760228A (en) * | 2008-12-25 | 2010-06-30 | 中国石油化工股份有限公司 | Catalytic conversion method for preparing propylene and high octane gasoline |
| CN101760228B (en) * | 2008-12-25 | 2013-06-26 | 中国石油化工股份有限公司 | Catalytic conversion method for preparing propylene and high octane gasoline |
| CN101591562B (en) * | 2009-06-25 | 2012-09-26 | 中国石油化工集团公司 | Fluid catalytic cracking method and device thereof |
| CN101993709A (en) * | 2009-08-11 | 2011-03-30 | 中国石化集团洛阳石油化工工程公司 | Catalytic cracking method and device thereof |
| CN101993708A (en) * | 2009-08-11 | 2011-03-30 | 中国石化集团洛阳石油化工工程公司 | Catalytic cracking method and device |
| CN102373079A (en) * | 2010-08-19 | 2012-03-14 | 中国石油化工股份有限公司 | Catalytic conversion method for increasing low-carbon olefin production |
| CN102373079B (en) * | 2010-08-19 | 2013-11-06 | 中国石油化工股份有限公司 | Catalytic conversion method for increasing low-carbon olefin production |
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| CN100519703C (en) | 2009-07-29 |
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