CN1209441C - Separation method of catalytic gasoline quality improved oil and gas and its installation - Google Patents
Separation method of catalytic gasoline quality improved oil and gas and its installation Download PDFInfo
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- CN1209441C CN1209441C CN 02146135 CN02146135A CN1209441C CN 1209441 C CN1209441 C CN 1209441C CN 02146135 CN02146135 CN 02146135 CN 02146135 A CN02146135 A CN 02146135A CN 1209441 C CN1209441 C CN 1209441C
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Abstract
The present invention discloses a separation method and a device for modified oil and gas of catalytic gasoline. The method comprises the separation steps that modified oil and gas flow into a simple fractionating tower and come into a countercurrent contact with oil slurry in the catalyst washing and desuperheating section at the bottom to wash catalyst powder and exchange heat; then, the modified oil and gas flow upwards to the rectification section of the fractionating tower to separate diesel oil fractions, gasoline fractions and cracked gas. Alternatively, the method comprises the separation steps that the modified oil and gas flow into a simple washing tower and comes into a countercurrent contact with oil slurry to exchange heat and wash catalyst powder; then, the high-temperature heat of the modified oil and gas is recovered again in a steam generator; finally, the modified oil and gas flow into a simple fractionating tower for separating diesel oil fractions, gasoline fractions and cracked gas; after heat exchange, the oil slurry flows into the steam generator to recover high-temperature heat. The present invention has the technical advantages of high-temperature heat recovery, low energy consumption in the process, simple flow path, low investment, stable and convenient operation and easy realization and can effectively separate the modified oil from gas in the catalytic cracked gasoline so that the olefin content of the catalytic gasoline is reduced to less than 25(v) % and an octane value is not lowered so as to meet the requirements of environmental laws and regulations.
Description
Technical field
The present invention relates to the separating process of petroleum hydrocarbon, be meant the Technology of catalytic gasoline upgrading gas-oil separation especially, belong to the petrochemical technology field.
Background technology
Increasingly stringent along with environmental requirement, motor spirit objectionable impurities standard-required olefin content in gasoline ≯ 35 (v) %, octane value (organon) ≮ 90, aromaticity content ≯ 40 (v) %, sulphur content ≯ 800ppm, and be defined in to rise on January 1st, 2003 in China and implement.At present, motor spirit has data to show that catalytically cracked gasoline accounts for the amount of gasoline product up to 85% still based on catalytically cracked gasoline.The volume fraction of alkene is 45%-60% in the catalytically cracked gasoline, far above the gasoline standard of new prescription.Because the chemical property of alkene 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.In order to reduce the olefin(e) centent of catalytically cracked gasoline, the general measure of adopting of petroleum refining industry has: the pre-hydrotreatment of fcc raw material; Olefine lowering catalyst is adopted in catalytic cracking; Optimize the catalytic cracking unit operational condition.But the effect of these methods is restricted, and 10-12 volume percentage point of the maximum decline of content of olefin in gasoline can not reach the requirement of new gasoline standard.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, as petroleum naphtha etherificate, catalytically cracked gasoline desulfurating and reducing olefinic hydrocarbon, catalytic gasoline hydrogenation isomery aromizing and catalytic gasoline hydrogenation desulfurization-reformation etc., these methods and technology or complex process, investment is big, many refinerys adopt still very big difficulty, perhaps that is that all right is ripe for Technology, does not have industrial applications.
In order to reduce the olefin(e) centent of catalytically cracked gasoline effectively, satisfy the requirement of environmental regulation and new gasoline standard, proposed on conventional catalytic cracking unit, to set up subsidiary riser or auxiliary reactor that catalytically cracked gasoline is carried out further upgrading, and applied for relevant patent, comprise: the method and the device of easy catalytic cracking sasoline modifincation and olefine reducing, application number: 02116786.9; Reduce the method and system of catalytic cracking gasoline olefine content, application number: 02123817.0, the method for modifying of heavily reducing olefinic hydrocarbon and increasing octane rating for catalytically cracked gasoline and device, application number: 02123655.0, reduce catalytic cracking gasoline olefine content and keep the method and system of octane value, application number: 02123494.9, the method for modifying of gasoline catalyzing and olefine reducing boosting of octane rating and device, application number: 02123658.9, reduce the method and the device of catalytic cracking gasoline olefine content, application number: 02116787.7.These method and apparatus that reduce catalytic cracking gasoline olefine content adopt subsidiary riser or auxiliary reactor that the high temperature regeneration agent is mixed with normal temperature Liquid Phase by Catalytic gasoline and contact, carry out hydrogen transference, aromizing, isomerization and the reaction of cracked upgrading, generate upgrading oil gas.In the foregoing invention patent, the separation of upgrading oil gas has two kinds of methods, and the one, in the settling vessel of former catalytic cracking unit, mix the laggard main fractionating tower of going into catalytic cracking main reaction oil gas, separate accordingly then; The 2nd, enter the simple and easy fractionating system of setting up separately and separate, can be with reference to patent of invention: the method for modifying of heavily reducing olefinic hydrocarbon and increasing octane rating for catalytically cracked gasoline and device, application number: 02123655.0, the method for modifying of gasoline catalyzing and olefine reducing boosting of octane rating and device, application number: 02123658.9, reduce the method and the device of catalytic cracking gasoline olefine content, application number: 02116787.7.Because the fractions consisting of modifying catalytically cracked gasoline oil gas is significantly different with conventional catalytic cracking reaction oil gas, the reacted gas that contains 5～10wt%, the gasoline fraction of 85～95wt% and the diesel oil distillate of 1～5wt%, the catalyst fines that also contains simultaneously trace, therefore, in order to separate this part upgrading oil gas effectively, and can reclaim heat of high temperature, reduction process energy consumption, the necessary separation system that adopts particular design.
Summary of the invention
Main purpose of the present invention is, a kind of separation method and device of catalytic gasoline upgrading oil gas is provided, and can separate upgrading oil gas effectively, reduces olefin(e) centent, keeps octane value constant.
Another object of the present invention is to, a kind of separation method and device of catalytic gasoline upgrading oil gas is provided, when separating upgrading oil gas, can reclaim heat of high temperature as much as possible, reduce the process energy consumption,
And guarantee that flow process is simple, easy to operate.
The objective of the invention is to be achieved through the following technical solutions.
Wherein, a kind of technical scheme of method is:
A kind of separation method of catalytic gasoline upgrading oil gas, the sepn process of upgrading oil gas is:
Step 1: upgrading oil gas enters a simple and easy separation column after catalytically cracked gasoline subsidiary riser or auxiliary reactor are drawn, in the catalyst detergent desuperheating section of bottom and slurry oil counter current contact from former catalytic cracking unit, the washing catalyst powder also carries out heat exchange, the slurry oil heat exchange temperature back that raises is drawn from the separation column bottom and is entered oil slurry steam generator and reclaim heat of high temperature, returns the riser reactor of former catalytic cracking unit then;
Step 2: the rectifying section that the oil gas after being washed upwards enters separation column carries out separating of diesel oil distillate, gasoline fraction and reacted gas.
Another technical scheme of method is:
A kind of separation method of catalytic gasoline upgrading oil gas, the sepn process of upgrading oil gas is:
Step 1: upgrading oil gas enters a simple and easy washing tower after catalytically cracked gasoline subsidiary riser or auxiliary reactor are drawn, carry out counter current contact heat exchange and washing catalyst powder with slurry oil from former catalytic cracking unit, slurry oil enters vapour generator to reclaim heat of high temperature, returns the riser reactor of former catalytic cracking unit then;
Step 2: the oil gas after being washed enters vapour generator and reclaims upgrading oil-gas high-temperature position heat once more, enters a simple and easy separation column at last and carries out separating of diesel oil distillate, gasoline fraction and reacted gas.
In two kinds of above-mentioned technical schemes, the condition of upgrading gas-oil separation process is:
Tower top temperature: 80～120 ℃; Diesel oil distillate is extracted temperature out: 170～250 ℃; Tower top pressure: 0.08～0.12Mpa gauge pressure; Described upgrading oil gas comprises at least and the full cut of catalytic cracking unit raw gasline or boiling range is carried out less than 110 ℃ raw gasline lighting end greater than 60 ℃ raw gasline last running or boiling range the catalytic reforming process obtains; Described catalyzer comprises any catalyzer of catalytic cracking process, is amorphous silicon aluminium catalyzer or molecular sieve catalyst or fluidisation catalyst for performing catalytic reforming; And the reacted gas after separating enters the rich gas compressor inlet of former catalytic cracking unit, gasoline fraction after the separation enters the absorbing-stabilizing system of former catalytic cracking unit, and the diesel oil distillate after the separation goes the gasoline stabilizer of former catalytic cracking device absorption stabilizing system as absorption agent.
A kind of technical scheme of device of the present invention is:
A kind of tripping device of catalytic gasoline upgrading oil gas, this device comprises: the top of subsidiary riser or auxiliary reactor links to each other with the bottom of a simple and easy separation column; Wherein, simple and easy separation column bottom connects oil-slurry pump, oil slurry steam generator and interchanger successively, and the separation column middle part is connected with diesel oil pump, and the separation column top connects oil gas condenser and catch pot successively.
Another implementation of apparatus of the present invention is:
A kind of tripping device of catalytic gasoline upgrading oil gas, this device comprises: the top of subsidiary riser or auxiliary reactor links to each other with the bottom of a simple and easy washing tower; Wherein, wash tower bottoms connects oil-slurry pump and oil slurry steam generator successively, and the washing tower top is connected with simple and easy separation column by vapour generator; Simple and easy knockout tower bottom is connected with diesel oil pump, and the top connects oil gas condenser and catch pot successively.
By above technical scheme, Technology advantage of the present invention is: can reclaim heat of high temperature, reduce the process energy consumption, flow process is simple, less investment, and stable operation is convenient, is easy to realize.Modifying catalytically cracked gasoline oil gas effectively can be separated, make the catalytic gasoline olefin(e) centent be reduced to 25 and (v) below the %, and keep octane value not reduce, can satisfy the requirement of national environmental protection rules.
Description of drawings
Fig. 1 constitutes technical process embodiment synoptic diagram for a kind of apparatus system of the present invention;
Fig. 2 constitutes technical process embodiment synoptic diagram for the another kind of apparatus system of the present invention.
Embodiment
The present invention will be further described below in conjunction with the drawings and specific embodiments:
Embodiment 1:
The separation process of upgrading oil gas is as shown in Figure 1: the temperature of drawing from catalytically cracked gasoline subsidiary riser or auxiliary reactor 1 top is the bottom that 350～500 ℃ upgrading oil gas 2 enters the catalyst detergent desuperheating section 4 that is located at simple and easy separation column 3 bottoms, carry out the washing of catalyst fines and carry out heat exchange in catalyst detergent desuperheating section 4 with the slurry oil 5 through heat exchange that attracts from former catalytic cracking unit, slurry oil 5 is introduced from the top of catalyst detergent desuperheating section 4.Slurry oil 5 is drawn through oil-slurry pump 6 from the separation column bottom and is entered oil slurry steam generator 7 and the recovery heat of high temperature then, enter interchanger 8 heat exchange again, return the riser reactor of former catalytic cracking unit then, the slurry oil temperature before the control oil-slurry pump 6 is 280～350 ℃.Set up the extraction line of diesel oil distillate at the middle part of simple and easy separation column 3, extract diesel oil distillate 10 out by diesel oil pump 9, it is 220～250 ℃ that control diesel oil is extracted temperature out.Set up oil gas condenser 11 and catch pot 12 at the top of separation column 3, to isolate reacted gas 13 and gasoline fraction 14, reacted gas 13 can enter the rich gas compressor inlet of former catalytic cracking unit, part gasoline fraction 141 returns separation column 3 tops as trim the top of column, and remainder 142 enters the absorbing-stabilizing system of former catalytic cracking unit.The catalyst detergent desuperheating section 4 of separation column bottom can be established 3～10 layers of chevron shaped baffle plate, and 5～30 layers of tower tray can be established in separation column inside.
Embodiment 2:
The separation process of upgrading oil gas can also be a mode shown in Figure 2: the temperature of drawing from catalytically cracked gasoline subsidiary riser or auxiliary reactor 1 top is the bottom that 350～500 ℃ upgrading oil gas 2 enters an easy washing tower 15, in simple and easy washing tower, carry out counter current contact with the slurry oil 5 that enters from simple and easy washing tower 15 tops from former catalytic cracking unit separation column and process heat exchange, carry out the washing of heat exchange and catalyst fines, the slurry oil 5 that temperature raises after the heat exchange is squeezed into oil slurry steam generator 7 to reclaim heat of high temperature through oil-slurry pump 6, returns the riser reactor of former catalytic cracking unit then.Simple and easy washing tower 15 can be established 2～10 layers of chevron shaped baffle plate, is 300～340 ℃ from the slurry oil temperature of former catalytic cracking unit separation column, and slurry oil temperature and upgrading oil gas temperature are 360～420 ℃ after the heat exchange.Oil gas 2 after being washed enters the high potential temperature heat of vapour generator 16 with further recovery upgrading oil gas, temperature is reduced to the middle and lower part that enters a simple and easy separation column 3 after 250～300 ℃, diesel oil distillate 10 is extracted out with diesel oil pump 9 in simple and easy separation column 3 bottoms, the gasoline stabilizer that can remove former catalytic cracking device absorption stabilizing system is as absorption agent.It is 220～250 ℃ that control diesel oil is extracted temperature out.At simple and easy separation column 3 tops oil gas 2 is introduced oil gas condenser 11 and carry out separating of reacted gas 13 and gasoline fraction 14 with catch pot 12, reacted gas 13 can enter the rich gas compressor inlet of former catalytic cracking unit, the part of gasoline fraction 14 is returned simple and easy separation column 3 tops as refluxing 141, and another part 142 enters the absorbing-stabilizing system of former catalytic cracking unit.Simple and easy separation column 3 can be established 5～30 layers of tower tray.
Upgrading oil gas can carry out that upgrading obtains with any catalyzer of catalytic cracking process to catalytically cracked gasoline, 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 contain rare earth and/or phosphorus or the supersiliceous zeolite with five-membered ring structure, β zeolite, the ferrierite, also can be to carry out upgrading with the further novel fluidisation catalyst for performing catalytic reforming of exploitation to obtain.
Claims (10)
1, a kind of separation method of catalytic gasoline upgrading oil gas, it is characterized in that: the sepn process of upgrading oil gas is:
Step 1: upgrading oil gas enters a simple and easy separation column after catalytically cracked gasoline subsidiary riser or auxiliary reactor are drawn, in the catalyst detergent desuperheating section of bottom and slurry oil counter current contact from former catalytic cracking unit, the washing catalyst powder also carries out heat exchange, the slurry oil heat exchange temperature back that raises is drawn from the separation column bottom and is entered oil slurry steam generator and reclaim heat of high temperature, returns the riser reactor of former catalytic cracking unit then;
Step 2: the rectifying section that the oil gas after being washed upwards enters separation column carries out separating of diesel oil distillate, gasoline fraction and reacted gas.
2, a kind of separation method of catalytic gasoline upgrading oil gas, it is characterized in that: the sepn process of upgrading oil gas is:
Step 1: upgrading oil gas enters a simple and easy washing tower after catalytically cracked gasoline subsidiary riser or auxiliary reactor are drawn, carry out counter current contact heat exchange and washing catalyst powder with slurry oil from former catalytic cracking unit, slurry oil enters vapour generator to reclaim heat of high temperature, returns the riser reactor of former catalytic cracking unit then;
Step 2: the oil gas after being washed enters vapour generator and reclaims upgrading oil-gas high-temperature position heat once more, enters a simple and easy separation column at last and carries out separating of diesel oil distillate, gasoline fraction and reacted gas.
3, the separation method of catalytic gasoline upgrading oil gas according to claim 1 and 2 is characterized in that: the condition of upgrading gas-oil separation process is:
Tower top temperature: 80～120 ℃; Diesel oil distillate is extracted temperature out: 170～250 ℃;
Tower top pressure: 0.08～0.12Mpa gauge pressure.
4, the separation method of catalytic gasoline upgrading oil gas according to claim 1 and 2 is characterized in that: described upgrading oil gas comprises at least and the full cut of catalytic cracking unit raw gasline or boiling range is carried out less than 110 ℃ raw gasline lighting end greater than 60 ℃ raw gasline last running or boiling range the catalytic reforming process obtains.
5, the isolating method of catalytic gasoline upgrading oil gas according to claim 1 and 2, it is characterized in that: described catalyzer comprises any catalyzer of catalytic cracking process, is amorphous silicon aluminium catalyzer or molecular sieve catalyst or fluidisation catalyst for performing catalytic reforming.
6, the separation method of catalytic gasoline upgrading oil gas according to claim 1 and 2, it is characterized in that: the reacted gas after the separation enters the rich gas compressor inlet of former catalytic cracking unit, gasoline fraction after the separation enters the absorbing-stabilizing system of former catalytic cracking unit, and the diesel oil distillate after the separation goes the gasoline stabilizer of former catalytic cracking device absorption stabilizing system as absorption agent.
7, a kind of tripping device of catalytic gasoline upgrading oil gas, it is characterized in that: this device comprises: the top of subsidiary riser or auxiliary reactor links to each other with the bottom of a simple and easy separation column; Wherein, simple and easy separation column bottom connects oil-slurry pump, oil slurry steam generator and interchanger successively, and the separation column middle part is connected with diesel oil pump, and the separation column top connects oil gas condenser and catch pot successively.
8, a kind of tripping device of catalytic gasoline upgrading oil gas, it is characterized in that: this device comprises: the top of subsidiary riser or auxiliary reactor links to each other with the bottom of a simple and easy washing tower; Wherein, wash tower bottoms connects oil-slurry pump and oil slurry steam generator successively, and the washing tower top is connected with simple and easy separation column by vapour generator; Simple and easy knockout tower bottom is connected with diesel oil pump, and the top connects oil gas condenser and catch pot successively.
9, the tripping device of catalytic gasoline upgrading oil gas according to claim 7 is characterized in that: described simple and easy separation column is provided with 5-30 layer tower tray, and this separation column also is provided with the catalyst detergent desuperheating section in the bottom, and the chevron shaped baffle plate of 3-10 layer wherein arranged.
10, the tripping device of catalytic gasoline upgrading oil gas according to claim 8 is characterized in that: described simple and easy washing tower is provided with the chevron shaped baffle plate of 2-10 layer; Described simple and easy separation column is provided with 5-30 layer tower tray.
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|---|---|---|---|
| CN 02146135 CN1209441C (en) | 2002-11-01 | 2002-11-01 | Separation method of catalytic gasoline quality improved oil and gas and its installation |
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| CN 02146135 CN1209441C (en) | 2002-11-01 | 2002-11-01 | Separation method of catalytic gasoline quality improved oil and gas and its installation |
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| CN1209441C true CN1209441C (en) | 2005-07-06 |
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| FR2871168B1 (en) * | 2004-06-04 | 2006-08-04 | Inst Francais Du Petrole | METHOD FOR IMPROVING ESSENTIAL CUPS AND GAS PROCESSING WITH COMPLEMENTARY TREATMENT FOR INCREASING THE YIELD OF THE GAS CUTTING |
| CN107723024A (en) * | 2017-11-02 | 2018-02-23 | 陈文星 | A kind of intensive slurry oil utilization system and its handling process |
| CN113717754B (en) * | 2021-09-24 | 2023-04-25 | 上海纳科助剂有限公司 | Catalytic cracking process for producing high aromatic hydrocarbon oil and high yield liquefied gas |
| CN113755208B (en) * | 2021-09-24 | 2023-04-25 | 上海纳科助剂有限公司 | High aromatic hydrocarbon oil material and preparation method and application thereof |
| CN113773874B (en) * | 2021-09-24 | 2023-04-25 | 上海纳科助剂有限公司 | High aromatic hydrocarbon oil material and preparation method and application thereof |
| CN113717752B (en) * | 2021-09-24 | 2023-04-25 | 上海纳科助剂有限公司 | High aromatic hydrocarbon oil material and preparation method and application thereof |
| WO2023046081A1 (en) * | 2021-09-24 | 2023-03-30 | 上海纳科助剂有限公司 | High aromatic oil, and preparation method therefor and use thereof |
| CN113897220B (en) * | 2021-09-24 | 2023-04-25 | 上海纳科助剂有限公司 | High aromatic hydrocarbon oil material and preparation method and application thereof |
| CN113717753B (en) * | 2021-09-24 | 2023-04-25 | 上海纳科助剂有限公司 | High aromatic hydrocarbon oil material and preparation method and application thereof |
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