CN1202207C - Method and device for reducing catalytic cracking gasoline olefine content - Google Patents
Method and device for reducing catalytic cracking gasoline olefine content Download PDFInfo
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- CN1202207C CN1202207C CN 02116787 CN02116787A CN1202207C CN 1202207 C CN1202207 C CN 1202207C CN 02116787 CN02116787 CN 02116787 CN 02116787 A CN02116787 A CN 02116787A CN 1202207 C CN1202207 C CN 1202207C
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Abstract
The present invention relates to a method and a device for reducing the olefine content of catalytically cracked gasoline. A light fraction (a fraction at the temperature of lower than 80 to 110DEG C) of crude gasoline is subjected to a catalytic modification reaction for reducing olefine, wherein the light fraction of the crude gasoline is separated out from a secondary condensation cooling system at the tower top of a fractionating tower. The device for reducing the olefine content of catalytically cracked gasoline comprises a secondary condensation cooling system, an auxiliary modification lift pipe reactor, a high-efficiency gas-solid quick separation device, a simple settling and steam stripping system and a simple separation system, wherein the secondary condensation cooling system is established at the tower top of the original fractionating tower. The present invention has the advantages of mild requisite technological conditions, modification process loss reduction, corresponding amount reduction of gasoline required to be modified, olefine content reduction of the catalytically cracked gasoline and no octane number reduction. Modified gasoline after being introduced into the simple separation system is discharged out of the device without being mixed with the catalytically cracked gasoline in a main lift pipe, and the olefine content of light gasoline returned to the modification lift pipe is the olefine content of the catalytically cracked light gasoline in the main lift pipe. The present invention meets relevant environmental protection requirements.
Description
Technical field:
The present invention relates to a kind of method and device that reduces catalytic cracking gasoline olefine content, specifically be meant a kind of method and device thereof that is used to reduce the catalyzed conversion of catalytic cracking gasoline olefine content, belong to the catalytic conversion technique field of petroleum hydrocarbon.
Background technology:
Along with the increasingly stringent to environmental requirement, the U.S., Japan and European various countries have all issued new gasoline standard in succession in recent years.China has also carried out great adjustment to gasoline standard.State Bureau of Environmental Protection in 1999 has been formulated " motor spirit objectionable impurities standard " and has been required olefin content in gasoline ≯ 35 (v) %, octane value (organon) ≮ 90, aromaticity content ≯ 40 (v) %, sulphur content ≯ 800ppm.And big cities enforcements such as rise in Beijing July 1 2000 regulation fs, Shanghai, Guangzhou, rose on January 1st, 2003 in China and implement.At present, China's motor spirit has data to show that China's catalytically cracked gasoline accounts for the amount of gasoline product up to 74% still based on catalytic cracking (FCC) gasoline.The volume fraction of alkene is 45%-50% in the catalytically cracked gasoline, far above the gasoline standard of new prescription.
The octane value of alkene is higher, but chemical property is active, NO in volatilization back and the atmosphere
XMix,, atmosphere is caused severe contamination through the poisonous photo-chemical smog of solar ultraviolet irradiation formation based on ozone; In addition, when olefin(e) centent is high in the gasoline, can cause that electronic fuel injection engine nozzle, feed valve carbon deposit are serious, cause controlled deviation, cause fuel oil consumption to increase.Therefore, the reduction olefin content in gasoline becomes the urgent task in the current petroleum refining industry.Because refinery's processing is paraffinic crude, its gasoline octane rating (organon) reaches standard reluctantly generally at 89-90, if olefin(e) centent is descended significantly, certainly will can't meet the demands by octane value.How satisfying in the gasoline olefin(e) centent simultaneously is no more than 35 (the v) requirement of % guarantees that again octane value reaches standard, just becomes a very urgently and very problem of difficulty.
In order to reduce the olefin(e) centent of catalytically cracked gasoline, petroleum refining industry produces the measure of going up general employing and is:
The pre-hydrotreatment of fcc raw material improves quality product;
Olefine lowering catalyst is adopted in catalytic cracking, can make 8-10 volume percentage point of content of olefin in gasoline decline, and light olefin productive rate and octane value are constant substantially;
Optimize the catalytic cracking unit operational condition, reduce the catalytic gasoline olefin(e) centent.
But the effect of above-mentioned these methods is limited, and content of olefin in gasoline 10-12 the volume percentage point that can only descend at most can not satisfy the new gasoline standard requirement of compliance with environmental protection requirements.Some research reports that catalytically cracked gasoline carried out independent upgrading also mainly are the means that reduce the olefin(e) centent of catalytically cracked gasoline, for example: petroleum naphtha etherificate, catalytically cracked gasoline desulfurating and reducing olefinic hydrocarbon, catalytic gasoline hydrogenation isomery aromizing, catalytic gasoline hydrogenation desulfurization-reformation etc.; These methods and technology or complex process, investment are big, and many refinerys adopt still very big difficulty, otherwise Technology that is that all right is ripe, still can not industrial applications.
Summary of the invention:
Main purpose of the present invention is to provide a kind of method and device that reduces catalytic cracking gasoline olefine content, by existing heavy oil catalytically cracking equipment is improved, make catalytically cracked gasoline carry out the catalytic reforming reaction, reduce the content of alkene in the catalytically cracked gasoline, guarantee that simultaneously the octane value of reformulated gasoline does not reduce.
Another object of the present invention is to provide a kind of method and device that reduces catalytic cracking gasoline olefine content, and it is simple to the technology that catalytically cracked gasoline carries out catalytic reforming, technology maturation, and less investment is easy to realize.
The object of the present invention is achieved like this:
A kind of method that reduces catalytic cracking gasoline olefine content is set up the B-grade condensation cooling system on the original conventional condensation cooling system of fractionator overhead, be used to isolate the lighting end of raw gasline; The lighting end of the raw gasline of being separated by fractionator overhead B-grade condensation cooling system, described lighting end are boiling point less than 80-110 ℃ cut, are used to reduce the catalytic reforming reaction of olefin(e) centent again, and concrete steps comprise:
Step 1:, from raw gasline, isolate lighting end at the B-grade condensation cooling system that fractionator overhead is set up;
Step 2: lighting end and water vapour, the high temperature catalyst separated in the step 1 are mixed, and in auxiliary upgrading lifting gear, carry out the upgrading reaction;
Step 3: separate through efficient fast gas-solid separator with the catalyst mix body through the reacted oil gas of upgrading in the step 2, the catalyzer of separating returns former revivifier through behind the stripping;
Step 4: the upgrading oil gas after the separation enters simple and easy separation system and isolates rich gas and reformulated gasoline, enters absorbing-stabilizing system again.
The reaction conditions of described catalytic reforming reaction is:
Temperature of reaction is 350～550 ℃;
The gasoline stocks preheating temperature is 40～200 ℃;
Catalyzer oil plant weight ratio is 2～20;
Catalyst activity is 55～65;
Reaction times is 1.0～4.0s;
Reaction pressure is 0.1～0.4MPa.
A kind of device that reduces catalytic cracking gasoline olefine content which comprises at least the B-grade condensation cooling system of setting up in former fractionator overhead, auxiliary upgrading riser reactor, efficient fast gas-solid separator, easy sedimentation stripping system and simple and easy separation system; Wherein,
Set up fractionator overhead B-grade condensation cooling system in former fractionator overhead, promptly before the conventional condensate cooler of former catalytic cracking unit fractionation cat head, add the one-level condensate cooler again, be used for the catalytic cracking raw gasline is separated into lighting end and last running;
Should auxiliary upgrading riser reactor be to introduce a high-temperature regenerated catalyst logistics from the revivifier of original heavy oil catalytically cracking equipment, this riser reactor exit portion enters the sedimentation stripping system of newly establishing, and outlet is provided with efficient fast gas-solid separator; The lighting end of raw gasline, water vapour and enter by the import of its bottom from the catalyzer of former revivifier and to carry out the catalytic reforming reaction;
This efficient fast gas-solid separator is located within the outlet and easy sedimentation stripping system of auxiliary upgrading riser reactor; Its feeding mouth is connected with the outlet of auxiliary upgrading riser reactor;
Isolated rich gas of simple and easy separation system and reformulated gasoline enter the absorbing-stabilizing system of former catalytic cracking unit.
Easy sedimentation stripping system comprises settling vessel and stripping stage, and this stripping stage is connected with former revivifier, is used for the catalyzer after the stripping sedimentation and returns to former revivifier.
Simple and easy separation system comprises: simple and easy washing knockout tower, catch pot, condensate cooler, recycle stock interchanger; Wherein,
The feeding mouth of simple and easy washing knockout tower is the feeding mouth of this simple and easy separation system, and its outlet is connected to condensate cooler;
The outlet of this condensate cooler is connected with catch pot;
This catch pot is rich gas and reformulated gasoline and the absorbing-stabilizing system that outputs to former catalytic cracking unit with the gas-oil separation that whole catalytic reforming reaction process produces;
This recycle stock interchanger is connected with the outlet of simple and easy washing knockout tower bottom, is used for superheated upgrading oil gas is carried out desuperheating and washing catalyst dust.
The recycle stock interchanger comprises at least: desuperheating washing medium interchanger and recycle pump, and this desuperheating washing medium interchanger is connected to the bottom of simple and easy washing knockout tower, and its outlet is connected to recycle pump, and this outlet of circulating pump connects back simple and easy washing knockout tower.
The present invention makes catalytically cracked gasoline carry out the catalytic reforming reaction by existing heavy oil catalytically cracking equipment is improved, and has reduced the content of alkene in the catalytically cracked gasoline, has guaranteed that simultaneously the octane value of reformulated gasoline does not reduce.This device is simple to the technology that catalytically cracked gasoline carries out catalytic reforming, technology maturation, and less investment is easy to realize.
The advantage of Technology of the present invention is to go out device after reformulated gasoline enters simple and easy separation system separately, and do not mix with the catalytically cracked gasoline of main riser tube, so return the olefin(e) centent that the olefin(e) centent of the petroleum naphtha of upgrading riser tube is exactly main riser catalytic cracking petroleum naphtha, needed processing condition comparatively relax, the loss of upgrading process reduces to some extent, need the corresponding reduction of amount of gasoline of upgrading, catalytic cracking gasoline olefine content can reduce greatly, octane value does not reduce simultaneously, satisfies corresponding environmental requirement.
Description of drawings:
Fig. 1 is a ultimate principle schematic flow sheet of the present invention.
Fig. 2 and Fig. 3 are the schematic flow sheet of one embodiment of the invention.
Embodiment:
The present invention is described in further detail below in conjunction with accompanying drawing and specific embodiment:
Starting point of the present invention is: on heavy oil catalytically cracking equipment, fractionator overhead is set up the B-grade condensation cooling system and set up a service hoisting pipe reactor that has independently simple and easy sedimentation stripping system and the simple and easy separation system of upgrading oil gas on revivifier, catalytically cracked gasoline is carried out the catalytic reforming reaction, to reach the purpose that reduces alkene, to guarantee also that simultaneously the octane value of reformulated gasoline does not reduce.
Referring to Fig. 1, it is a ultimate principle schematic flow sheet of the present invention.After raw gasline is isolated lighting end 11 (cut point is 80～110 ℃) by fractionator overhead B-grade condensation cooling system, enter auxiliary upgrading riser reactor 12 from the bottom with water vapour, with the high temperature regeneration agent 14 from former catalytic cracking unit revivifier be 350～550 ℃ in temperature of reaction, the gasoline stocks preheating temperature is 40～200 ℃, catalyzer oil plant weight ratio is 2～20, catalyst activity is 55～65, reaction times is 1.0～4.0s, reaction pressure is to contact under 0.1～0.4MPa, gasification, mix and reaction, oil gas, water vapour passes through auxiliary upgrading riser reactor 12 with catalyzer, upgrading oil gas and catalyzer are separated by efficient fast gas-solid separator to the outlet of upgrading riser reactor, catalyzer enters and newly establishes easy sedimentation stripping system, enters former revivifier 3 through behind the stripping.Upgrading oil gas 18 enters the simple and easy separation system that is made of simple and easy washing knockout tower 19, condensate cooler 20, catch pot 21, desuperheating washing medium interchanger 22 and recycle pump 23, isolate rich gas 24 and reformulated gasoline 25, and then enter the absorbing-stabilizing system of former catalytic cracking unit.Desuperheating and washing catalyst dust are carried out by desuperheating washing medium interchanger 22 and 23 pairs of superheated upgradings of recycle pump oil gas in washing knockout tower 19 bottoms.
Referring to Fig. 2, it is for the main-process stream of the present invention embodiment in the system of whole heavy oil fluid catalytic cracking.The operation of former catalytic-cracking reaction system is constant, be that raw material 1 enters main riser tube 2 with water vapour from the bottom, with the high temperature regeneration agent 5 that promotes by water vapour 4 from revivifier 3 be 460～530 ℃ in temperature of reaction, the fcc raw material preheating temperature is 160～250 ℃, catalyzer oil plant weight ratio is 5～8, catalyst activity is 50～65, and the reaction times is 2.5～3.0s, and reaction pressure is to contact, gasify, mix and react under the condition of 0.1～0.4Mpa; Oil gas, water vapour pass through main riser reactor 2 with catalyzer, revolve 7 to main riser reactor outlet by efficient fast gas-solid separator 6 and settling vessel top, main reaction oil gas and catalyzer are separated, catalyzer enters through settling vessel 8 and enters stripping stage 9, enters former revivifier 3 through behind the stripping.Main reaction oil gas 10 leaves settling vessel 8 and enters the separation that main fractionating tower carries out rich gas, raw gasline lighting end, raw gasline last running, diesel oil, recycle stock, slurry oil.
After raw gasline is isolated lighting end 11 (cut point: 80～110 ℃) by fractionator overhead B-grade condensation cooling system, enter auxiliary upgrading riser reactor 12 from the bottom with water vapour, with the high temperature regeneration agent 14 that promotes by water vapour 13 from revivifier 3 be 350～550 ℃ in temperature of reaction, the gasoline stocks preheating temperature is 40～200 ℃, catalyzer oil plant weight ratio is 2～20, catalyst activity is 55～65, reaction times is 1.0～4.0s, and reaction pressure is to contact, gasify, mix and react under the condition of 0.1～0.4Mpa; Oil gas, water vapour,, are separated upgrading oil gas and catalyzer by efficient fast gas-solid separator 15 to the outlet of upgrading riser reactor by auxiliary upgrading riser reactor 12 with catalyzer; Catalyzer enters and newly establishes easy settling vessel 16 and stripping stage 17, returns former revivifier 3 through behind the stripping.
Upgrading oil gas 18 leaves settling vessel 16 and enters the simple and easy separation system that is made of simple and easy washing knockout tower 19, condensate cooler 20, catch pot 21, desuperheating washing medium interchanger 22 and recycle pump 23, isolate rich gas 24 and reformulated gasoline 25, and then enter the absorbing-stabilizing system of former catalytic cracking unit.Desuperheating and washing catalyst dust are carried out by desuperheating washing medium interchanger 22 and 23 pairs of superheated upgradings of recycle pump oil gas in simple and easy washing knockout tower 19 bottoms.
Referring to Fig. 2, Fig. 3, raw gasline can be summarized as follows by the flow process that fractionator overhead B-grade condensation cooling system separates lighting end (cut point: 80～110 ℃): the main reaction oil gas of being made up of raw gasline and rich gas 10 is come out by the top of separation column 102,103 condensations of process condenser are cooled to enter after 62～80 ℃ separating tank 104 and carry out the separation of profit gas, and condensed water 105 detaches separating tank 104 by condensate pump 106.The product liquid that condensation is got off is catalysis raw gasline last running 107, extract out from separating tank 104 through raw gasline double distilled wheel cylinder 108, a part refluxes 109 as the top of separation column 102, and another part 110 mixes with raw gasline lighting end 121 after supercooler 111 further is cooled to 40 ℃ and enters absorbing-stabilizing system after helping cut raw gasline 123.Uncooled oil gas 112 process condensers 113 condensations of coming out from separating tank 104 are cooled to enter after 40 ℃ separating tank 114 and carry out the separation of profit gas, and condensed water 115 detaches separating tank 114 by condensate pump 116.The uncooled oil gas that comes out from separating tank 114 is rich gas 117, enters rich gas compressor.The condensate oil of being separated by separating tank between the pneumatic press machine 118 turns back to separating tank 114.The product liquid that condensation is got off in the separating tank 114 is that raw gasline lighting end 119 is extracted separated into two parts out by raw gasline lighting end pump 120, part raw gasline lighting end 121 mixes with raw gasline last running 110 and enters absorbing-stabilizing system after helping cut raw gasline 123, and another part raw gasline lighting end 11 enters the upgrading riser reactor and carries out upgrading and fall alkene.
The above-mentioned desuperheating washing medium that is adapted to simple and easy washing knockout tower is recycle stock or heavy gas oil.
The catalyzer of present embodiment can be any catalyzer that is adapted to catalytic cracking process, i.e. modifying catalytically cracked gasoline reaction is realized by former heavy oil catalytic cracking unit catalyzer.
Above embodiment is only in order to explanation and unrestricted technical scheme of the present invention; Although with reference to above-mentioned all embodiments the present invention is had been described in detail, those of ordinary skill in the art can not deny: each technical characterictic among the present invention still can be done corresponding modification, adjusts or be equal to replacement; But all do not break away from any modification or partial replacement of the spirit and scope of the present invention, all should be disclosed technical characterictic, and all should be encompassed in the middle of the claim scope of the present invention.
Claims (6)
1, a kind of method that reduces catalytic cracking gasoline olefine content is characterized in that: set up the B-grade condensation cooling system on the original conventional condensation cooling system of fractionator overhead, be used to isolate the lighting end of raw gasline; The lighting end of the raw gasline of being separated by fractionator overhead B-grade condensation cooling system is used to reduce the catalytic reforming reaction of olefin(e) centent again, and concrete steps comprise:
Step 1:, from raw gasline, isolate lighting end at the B-grade condensation cooling system that fractionator overhead is set up;
Step 2: lighting end and water vapour, the high temperature catalyst separated in the step 1 are mixed, and in auxiliary upgrading lifting gear, carry out the upgrading reaction;
Step 3: separate through efficient fast gas-solid separator with the catalyst mix body through the reacted oil gas of upgrading in the step 2, the catalyzer of separating returns former revivifier through behind the stripping;
Step 4: the upgrading oil gas after the separation enters simple and easy separation system and isolates rich gas and reformulated gasoline, enters absorbing-stabilizing system again.
2, the method for reduction catalytic cracking gasoline olefine content according to claim 1 is characterized in that: the reaction conditions of described catalytic reforming reaction is:
Temperature of reaction is 350～550 ℃;
The gasoline stocks preheating temperature is 40～200 ℃;
Catalyzer oil plant weight ratio is 2～20;
Catalyst activity is 55～65;
Reaction times is 1.0～4.0s;
Reaction pressure is 0.1～0.4MPa.
3, a kind of device that reduces catalytic cracking gasoline olefine content is characterized in that: which comprises at least the B-grade condensation cooling system of setting up in former fractionator overhead, auxiliary upgrading riser reactor, efficient fast gas-solid separator, easy sedimentation stripping system and simple and easy separation system; Wherein,
Set up fractionator overhead B-grade condensation cooling system in former fractionator overhead, promptly before the conventional condensate cooler of former catalytic cracking unit fractionation cat head, add the one-level condensate cooler again, be used for the catalytic cracking raw gasline is separated into lighting end and last running;
Should auxiliary upgrading riser reactor be to introduce a high-temperature regenerated catalyst logistics from the revivifier of original heavy oil catalytically cracking equipment, this riser reactor exit portion enters the sedimentation stripping system of newly establishing, and outlet is provided with efficient fast gas-solid separator; The lighting end of raw gasline, water vapour and enter by the import of its bottom from the catalyzer of former revivifier and to carry out the catalytic reforming reaction;
This efficient fast gas-solid separator is located within the outlet and easy sedimentation stripping system of auxiliary upgrading riser reactor; Its feeding mouth is connected with the outlet of auxiliary upgrading riser reactor;
Isolated rich gas of simple and easy separation system and reformulated gasoline enter the absorbing-stabilizing system of former catalytic cracking unit.
4, the device of reduction catalytic cracking gasoline olefine content according to claim 3, it is characterized in that: this easy sedimentation stripping system comprises settling vessel and stripping stage, this stripping stage is connected with former revivifier, is used for the catalyzer after the stripping sedimentation and returns to former revivifier.
5, the device of reduction catalytic cracking gasoline olefine content according to claim 3 is characterized in that: this simple and easy separation system comprises: simple and easy washing knockout tower, catch pot, condensate cooler, recycle stock interchanger; Wherein,
The feeding mouth of simple and easy washing knockout tower is the feeding mouth of this simple and easy separation system, and its outlet is connected to condensate cooler;
The outlet of this condensate cooler is connected with catch pot;
This catch pot is rich gas and reformulated gasoline and the absorbing-stabilizing system that outputs to former catalytic cracking unit with the gas-oil separation that whole catalytic reforming reaction process produces;
This recycle stock interchanger is connected with the outlet of simple and easy washing knockout tower bottom, is used for superheated upgrading oil gas is carried out desuperheating and washing catalyst dust.
6, the device of reduction catalytic cracking gasoline olefine content according to claim 5, it is characterized in that: this recycle stock interchanger comprises at least: desuperheating washing medium interchanger and recycle pump, this desuperheating washing medium interchanger is connected to the bottom of simple and easy washing knockout tower, its outlet is connected to recycle pump, and this outlet of circulating pump connects back simple and easy washing knockout tower.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 02116787 CN1202207C (en) | 2002-05-13 | 2002-05-13 | Method and device for reducing catalytic cracking gasoline olefine content |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 02116787 CN1202207C (en) | 2002-05-13 | 2002-05-13 | Method and device for reducing catalytic cracking gasoline olefine content |
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| CN1458227A CN1458227A (en) | 2003-11-26 |
| CN1202207C true CN1202207C (en) | 2005-05-18 |
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| CN 02116787 Expired - Fee Related CN1202207C (en) | 2002-05-13 | 2002-05-13 | Method and device for reducing catalytic cracking gasoline olefine content |
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Families Citing this family (4)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN102234533B (en) * | 2010-05-05 | 2014-01-01 | 中国石油化工集团公司 | Delayed coking method |
| CN102453509B (en) * | 2010-10-27 | 2014-03-26 | 中国石油化工股份有限公司 | Catalytic conversion method for hydrocarbon oil |
| CN102453516A (en) * | 2010-10-27 | 2012-05-16 | 中国石油化工股份有限公司 | Method for catalytically converting hydrocarbon oil with single lifting pipe |
| CN106800947A (en) * | 2017-02-28 | 2017-06-06 | 中石化炼化工程（集团）股份有限公司 | A kind of method for modifying of catalytically cracked gasoline |
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