CN1611572A - Catalytic converting method for improving petrol octane number - Google Patents
Catalytic converting method for improving petrol octane number Download PDFInfo
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- CN1611572A CN1611572A CN 200310103038 CN200310103038A CN1611572A CN 1611572 A CN1611572 A CN 1611572A CN 200310103038 CN200310103038 CN 200310103038 CN 200310103038 A CN200310103038 A CN 200310103038A CN 1611572 A CN1611572 A CN 1611572A
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- 230000003197 catalytic effect Effects 0.000 title claims description 10
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- 239000007795 chemical reaction product Substances 0.000 claims abstract description 11
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- 238000009835 boiling Methods 0.000 claims description 33
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- 239000000203 mixture Substances 0.000 description 15
- 229910021536 Zeolite Inorganic materials 0.000 description 14
- HNPSIPDUKPIQMN-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical compound O=[Si]=O.O=[Al]O[Al]=O HNPSIPDUKPIQMN-UHFFFAOYSA-N 0.000 description 14
- 239000010457 zeolite Substances 0.000 description 14
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 13
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- 238000005336 cracking Methods 0.000 description 12
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- 229910052782 aluminium Inorganic materials 0.000 description 1
- 239000004411 aluminium Substances 0.000 description 1
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 description 1
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- UQSXHKLRYXJYBZ-UHFFFAOYSA-N iron oxide Inorganic materials [Fe]=O UQSXHKLRYXJYBZ-UHFFFAOYSA-N 0.000 description 1
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- 238000006384 oligomerization reaction Methods 0.000 description 1
- TWNQGVIAIRXVLR-UHFFFAOYSA-N oxo(oxoalumanyloxy)alumane Chemical compound O=[Al]O[Al]=O TWNQGVIAIRXVLR-UHFFFAOYSA-N 0.000 description 1
- NDLPOXTZKUMGOV-UHFFFAOYSA-N oxo(oxoferriooxy)iron hydrate Chemical compound O.O=[Fe]O[Fe]=O NDLPOXTZKUMGOV-UHFFFAOYSA-N 0.000 description 1
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- KKCBUQHMOMHUOY-UHFFFAOYSA-N sodium oxide Chemical compound [O-2].[Na+].[Na+] KKCBUQHMOMHUOY-UHFFFAOYSA-N 0.000 description 1
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Abstract
One catalyzed conversion method to increase gasoline octane number is that, contact the heavy petrol whose first distillate point is higher than 100deg.C with catalyst whose temperature is lower than 700deg.C, under the condition of 300-600deg.C, 130-450Kpa, weight hourly space velocity (WHSV) of 1-120h-1, weight ratio between catalyst and gasoline fraction, between water vapor and gasoline fraction is respectively 2-20, 0-0,1,reaction happens, separate the reaction product from after stripping and regeneration, it can be recycled. Adopting this method can increase octane number of catalyzed cracked gasoline by 3-20 units.
Description
Technical field
The invention belongs to the catalysis conversion method of petroleum hydrocarbon under the situation that does not have hydrogen, a kind of catalysis conversion method that improves gasoline octane rating of more specifically saying so.
Technical background
Catalytically cracked gasoline is the chief component of China's motor spirit, thereby the height of its octane value directly affects the octane value level of gasoline product.At present China is based on No. 90 gasoline, but along with the improving constantly and the continuous increase of domestic imported auto recoverable amount of domestic automobile production level, and the demand of No. 93 or more high-octane gasoline is increased day by day.Catalytically cracked gasoline is owing to be subjected to the restriction of catalytic cracking process self, its octane value is generally below No. 93, thereby become the restraining factors of the further boosting of octane rating level of gasoline product, need to seek a kind of method that improves the catalytically cracked gasoline octane value for this reason.
CN1160746A discloses a kind of catalysis conversion method that improves gasoline octane number.This method is with in the upstream injecting lift pipe reactor of low octane value gasoline by conventional catalytically cracked material inlet, contacts with high temperature catalyst from revivifier, and be that 600～730 ℃, agent-oil ratio are 6～180, weight hourly space velocity is 1～180 o'clock in temperature of reaction
-1Condition under react.This method can make the octane value of gasoline obviously improve, but the waste of gasoline is bigger.
USP5,409,596 disclose a kind of catalysis conversion method that improves the hydrogenated gasoline octane value.This method is that the gasoline fraction after the hydrofining is contacted with the catalyzer that contains mesopore zeolite, is that 150～482 ℃, liquid hourly space velocity are 0.5～10 o'clock in temperature of reaction
-1, reaction pressure is that the volume ratio of 0.35MPa～10.4Mpa, hydrogen and hydro carbons is under 0～900 the condition, to carry out the normal paraffin cracking reaction, thereby the octane value of gasoline fraction is improved.
USP5,154,818 to disclose a kind of be the catalyst cracking method of raw material production stop bracket gasoline with multiple petroleum hydrocarbon.This method is that riser reactor is divided into first reaction zone and second reaction zone from bottom to top; Gasoline fraction contacts at first reaction zone with the reclaimable catalyst that contains shape-selective molecular sieve or mesoporous molecular sieve, and generation aromatization and oligomerization, temperature of reaction is 371～538 ℃, and the form that the reactant flow that is generated is carried with dilute phase is along being advanced into second reaction zone on the riser tube; And heavier hydrocarbon feeds contacts at second reaction zone with regenerated catalyst, and conventional catalytic cracking reaction takes place; The oil gas that generates separates in settling vessel with reclaimable catalyst, oil gas goes subsequent separation system, and reclaimable catalyst is behind stripping, and a part is returned above-mentioned first reaction zone, another part then enters the revivifier coke burning regeneration, and the regenerated catalyst of heat returns second reaction zone and recycles.
Summary of the invention
The objective of the invention is to provide on the basis of existing technology a kind of catalysis conversion method of new raising gasoline octane rating.
Method provided by the invention is: initial boiling point is lower than 700 ℃ catalyzer greater than 100 ℃ heavy naphtha and temperature and contacts, and is 1～120h at 300～660 ℃, 130～450Kpa, weight hourly space velocity
-1, catalyzer and gasoline fraction weight ratio be 2～20, the weight ratio of water vapour and gasoline fraction is to react under 0～0.1 the condition, reaction product isolated and spent agent, spent agent recycles after stripping, regeneration.
Compared with prior art, method provided by the invention has following characteristics:
1, adopt method provided by the invention can make the octane value of catalytically cracked gasoline improve 3～10 units.
2, the present invention does not have special requirement to catalyzer, and conventional catalytic cracking catalyst all is applicable to the present invention.Special needs to be pointed out is: when the present invention implements separately, the poiser that can use catalytic cracking unit to draw off.Like this, the quality by the present invention had both improved gasoline fraction can reduce running cost again.
3, the present invention has adopted device form more flexibly, both can implement separately, again can with existing catalytic cracking unit Joint Implementation.In numerous oil refining enterprises, the phenomenon that has the above catalytic cracking unit of two covers is very general.Yet for the problem that solves that there is lack of raw materials or in order to reduce cost, to form certain process scale, increase economic efficiency, many refineries all left unused a cover or two cover catalytic cracking unit.Therefore, can utilize existing, the idle catalytic cracking unit in refinery to implement the present invention.Adopt the mode of Joint Implementation also smaller to the transformation of existing catalytic cracking unit, can with the shared settling vessel of existing catalytic cracking unit, stripper, subsequent separation system and regeneration system rapidly etc., only need increase a riser reactor or a fluidized-bed reactor of handling gasoline stocks.Therefore, plant modification investment required for the present invention is less.
4, adopt method provided by the invention to handle above-mentioned gasoline fraction, in resulting material balance, gasoline yield accounts for more than the 80 heavy %, and rest part is dry gas, liquefied gas, diesel oil and coke, and the olefin(e) centent of gained gasoline products is less than 20 heavy %.In addition, the desulfurization degree of method provided by the invention can reach more than 50%.Therefore, implementation result of the present invention is apparent in view.
When 5, implementing method provided by the invention, the catalyzer cooling apparatus can be set, thereby increase the handiness of operation.Can be as required in actual production process the yield of the octane value of gasoline and gasoline be taken all factors into consideration and adjusted.
Description of drawings
Fig. 1 is the schematic flow sheet of embodiment A provided by the invention.
Fig. 2 is the schematic flow sheet of embodiment B provided by the invention.
Fig. 3 is the schematic flow sheet of embodiment C provided by the invention.
Embodiment
The hydrocarbon raw material that the present invention is suitable for is an initial boiling point greater than 100 ℃, the preferred initial boiling point heavy naphtha greater than 110 ℃, and further preferred initial boiling point is greater than 110 ℃ and the final boiling point heavy naphtha less than 180 ℃.This heavy naphtha can be from catalytically cracked gasoline, also can be the catalytically cracked gasoline through hydrotreatment, can also be the mixture of above-mentioned gasoline fraction.Heavy naphtha of the present invention preferably earlier through preheating, for example, was preheating to heavy naphtha more than 150 ℃ before injecting reactor.
Any catalyzer that is used for catalytic cracking process, 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.
In method provided by the invention, with initial boiling point greater than 100 ℃, preferably initial boiling point contact greater than 110 ℃ heavy naphtha and temperature to be lower than 700 ℃ catalyzer be the regenerated catalyst of the heavy % in coke content≤0.50, the regenerated catalyst of preferred coke content≤0.10 heavy %.
The specific embodiments of method provided by the present invention is as follows:
Method provided by the invention can be implemented separately on the riser tube of handling gasoline stocks or fluidized bed catalytic cracker, also can with the riser tube or the fluidized bed catalytic cracker Joint Implementation of the conventional catalytically cracked material of processing.The heavy naphtha catalytic convention design is identical with conventional catalytic cracking unit, and just operational condition is different from conventional catalytic cracking unit.When adopting the mode of Joint Implementation, heavy naphtha and conventional catalytically cracked material react in reactor separately respectively; And settling vessel, stripper and subsequent separation system can be shared, also can be separately independently; The regeneration system rapidly of catalyzer is shared.
In such scheme, when adopting the mode of Joint Implementation, the catalyzer that contacts with heavy naphtha can be identical with the catalyzer that contacts with conventional catalytically cracked material, also can be different.When adopting different catalyzer, the zeolite of the zeolite of the catalyzer that contacts with heavy naphtha and the catalyzer that contacts with conventional catalytically cracked material all can be selected from y-type zeolite, HY type zeolite, ultrastable Y, ZSM-5 series zeolite or have the supersiliceous zeolite of five-membered ring structure, one or more the mixture of arbitrary proportion in the ferrierite.Above-mentioned zeolite can contain rare earth and/or phosphorus, also can be not contain rare earth and phosphorus.In order to make above-mentioned two kinds of catalyzer in catalytic cracking unit, be convenient to separate, should be prepared as catalyzer with different physical properties, such as, different particle diameters, different apparent densities etc.Above-mentioned two kinds of different catalyzer enter different reactors respectively, contact, react with heavy naphtha or conventional catalytically cracked material.For example, the bigger catalyzer of particle diameter that contains ultrastable Y contacts, reacts with conventional catalytically cracked material, to strengthen heavy oil cracking ability, improves reaction preference; And the less catalyzer of the particle diameter that contains rare earth Y type zeolite contacts, reacts with heavy naphtha, to increase the hydrogen transfer reactions of heavy naphtha; Above-mentioned two kinds of different catalyzer after finish separates, common stripping and regeneration, after being separated according to the difference of its physical properties in stripper and revivifier, different catalyst transport is returned corresponding reactor, reaction and regenerative process is circulated carry out.The catalyzer that granular size is different can adopt boundary between 30～40 microns, and the catalyzer that apparent bulk density is different can adopt boundary between 0.6～0.7 gram/cubic centimetre.
Method provided by the invention can further describe as follows:
Initial boiling point after the preheating greater than 100 ℃, preferably enter in the riser tube or fluidized-bed reactor of gasoline catalyzing conversion system greater than 110 ℃ heavy naphtha, the regenerated catalyst that is lower than 700 ℃ with temperature contacted, 300～660 ℃ of temperature of reaction, reaction pressure 130～450kpa, weight hourly space velocity 1～120 hour
-1, catalyzer and heavy naphtha weight ratio be 2～15, the weight ratio of water vapor and heavy naphtha is to react under 0～0.1 the condition, preferred reaction conditions is as follows: 350～600 ℃ of temperature of reaction, reaction pressure 250～400kpa, weight hourly space velocity 2～100 hours
-1, the weight ratio of catalyzer and gasoline fraction is 3～10, the weight ratio of water vapor and heavy naphtha is 0.01～0.05; Reaction product, water vapor and reacted band Pd/carbon catalyst carry out gas solid separation; Reaction product isolated obtains dry gas, liquefied gas, is rich in main productss such as the stop bracket gasoline of isoparaffin and aromatic hydrocarbons, diesel oil; Reclaimable catalyst enters stripping stage, and the water steam stripped is admitted to revivifier after going out the hydrocarbon product that adsorbs on the catalyzer, coke burning regeneration in the presence of oxygen-containing gas; The pyritous regenerated catalyst is through also recycling without Returning reactor after the cooling of water cooler; The process of cooling of regenerated catalyst is the heat transfer process of high temperature catalyst and cryogenic media.This process can be finished in this device, also can finish in other device; The employed water cooler of this process can be independent, and is also can right and wrong independent.
Heavy naphtha and temperature are lower than the reaction process of 700 ℃ regenerated catalyst and can implement separately on the gasoline catalyzing conversion system, also can with processing conventional catalytically cracked material riser fluid catalytic cracking or fluidized bed catalytic cracker Joint Implementation, promptly, according to requirement of the present invention the device of processing conventional catalytically cracked material is slightly done transformation, gasoline fraction and conventional catalytically cracked material are at first reacted in reactor separately; And the stripping process of the separation of the separating of reacted oil gas and catalyzer, reaction product and reaction back band Pd/carbon catalyst can above-mentioned two bursts of reactant flow carry out separately separately, also two bursts of reactant flow can be lumped together and carry out jointly; The regenerative process of reclaimable catalyst is carried out jointly, a promptly shared cover regeneration system rapidly.
Enumerate three kinds of concrete embodiments below and further specify technological process described in the invention, but the present invention is not limited to any embodiment hereinafter.
Embodiment A: idle riser fluid catalytic cracking transform the gasoline catalyzing conversion system as, the cracking stock of routine can be replaced by initial boiling point greater than 100 ℃, preferably greater than 110 ℃ heavy naphtha, this cut contacts with thermocatalyst from revivifier and reacts, the reactant flow that generates enters settling vessel, realization response oil gas separates with reclaimable catalyst, and reaction oil gas enters follow-up fractionating system and carries out product separation; Reclaimable catalyst is transported to the revivifier coke burning regeneration behind stripping, the catalyzer after the regeneration turns back to the riser tube bottom cycle and uses.
Embodiment B:, need a newly-built riser reactor for the catalytic cracking unit of single riser reactor.The shared original settling vessel of newly-built riser reactor and original riser reactor, stripper, subsequent separation system and regeneration system rapidly.The raw material of newly-built reactor be initial boiling point greater than 100 ℃, preferably greater than 110 ℃ heavy naphtha, this reactor is called gasoline rising pipe; The raw material of original riser reactor is conventional cracking stock, and this reactor is called the stock oil riser tube.Gasoline stocks and conventional cracking stock react in gasoline rising pipe and stock oil riser tube respectively, and reaction oil gas and mixture of catalysts enter settling vessel and subsequent separation system jointly.Isolated raw gasline can partly return the raw material as gasoline rising pipe.Reclaimable catalyst is regenerated behind stripping, and the catalyzer after the regeneration is divided into two portions, and wherein a part is returned the stock oil riser tube, and another part returns gasoline rising pipe after the catalyst cooler cooling.
Embodiment C: for the catalytic cracking unit of single riser reactor, need a newly-built fluidized-bed reactor that has or do not have riser tube, this reactor can have or not have stripping stage.Newly-built reactor and original reactor common regenerator.The raw material of newly-built reactor be initial boiling point greater than 100 ℃, preferably greater than 110 ℃ heavy naphtha, this reactor is called the gasoline reactor; The raw material of original reactor is conventional cracking stock, and this reactor is called the stock oil riser reactor.Heavy naphtha and conventional cracking stock react in gasoline reactor and stock oil riser reactor respectively; Enter subsequent separation system after the reaction oil gas that reaction oil gas that heavy naphtha generates and conventional cracking stock generate mixes, perhaps enter subsequent separation system separately respectively, isolated raw gasline can partly return the raw material as gasoline rising pipe.Reclaimable catalyst is regenerated behind stripping, and the catalyzer after the regeneration is divided into two portions, and wherein a part is returned the stock oil riser tube, and another part returns the gasoline reactor through water cooler.
Below in conjunction with accompanying drawing the present invention is illustrated, but therefore the present invention is not subjected to any restriction.
As shown in Figure 1, initial boiling point after the preheating greater than 100 ℃, preferably enter riser tube 2 bottoms through pipeline 1 greater than 110 ℃ heavy naphtha, mix, react with regenerator from regenerator sloped tube 4, reactant flow enters the settling vessel 5 that has or do not have the dense fluidized bed bioreactor, and reaction oil gas and water vapor enter catalytic cracking fractionating tower 10 through pipeline 9.Reacted gas, gasoline fraction and water vapor are distillated by the top of separation column 10, enter first-stage condenser 11, condensation goes out water vapor and initial boiling point greater than 100 ℃ or greater than 110 ℃ heavy naphtha, reacted gas and do less than 100 ℃ or distillate less than 110 ℃ the light gasoline fraction top by first-stage condenser 11 enters secondary condenser 12.After enter revivifier 6, spent agent is coke burning regeneration under the effect of oxygen-containing gas through the water vapor stripping for spent agent, and regenerated flue gas is drawn by the top of revivifier 6.The pyritous regenerator turns back to the riser tube bottom through regenerator sloped tube 4, recycles.
As shown in Figure 2, initial boiling point after the preheating greater than 100 ℃, preferably enter the bottom of gasoline rising pipe 2 through pipeline 1 greater than 110 ℃ heavy naphtha, mix, react with regenerator from regenerator sloped tube 4.1, reactant flow enters the settling vessel 5 that has or do not have the dense fluidized bed bioreactor, the separating of realization response oil gas and catalyzer.Simultaneously, the high temperature regeneration agent enters the bottom of conventional FCC raw material riser tube 2 ' through regenerator sloped tube 4 ', promote by pre-lifting medium, conventional cracking stock after the preheating injects this riser tube through pipeline 13, mix with the high temperature regeneration agent and react, reactant flow enters the settling vessel 5 that has or do not have the dense fluidized bed bioreactor, the separating of realization response oil gas and catalyzer.Reaction oil gas enters catalytic cracking fractionating tower 10 through pipeline 9.Reacted gas, gasoline fraction and water vapor are distillated by the top of separation column, enter first-stage condenser 11, condensation goes out water vapor and the initial boiling point heavy naphtha greater than 100 ℃ or 110 ℃, reacted gas and do less than 100 ℃ or distillate less than 110 ℃ the light gasoline fraction top by first-stage condenser enters secondary condenser 12.Spent agent enters stripper 14, behind the reaction oil gas that the water vapor stripping goes out to carry, enters revivifier 6, and spent agent is coke burning regeneration under the effect of oxygen-containing gas, and regenerated flue gas is drawn by the top of revivifier.The high temperature regeneration agent is divided into two portions, and wherein, a part of regenerator enters catalyst cooler 3 through regenerator sloped tube 4, and cooled regenerator returns the gasoline rising pipe bottom cycle by regenerator sloped tube 4.1 and uses; Another part regenerator returns conventional riser tube 2 ' through regenerator sloped tube 4 ' and recycles.
As shown in Figure 3, initial boiling point after the preheating greater than 100 ℃, enter the bottom of gasoline rising pipe 2 through pipeline 1 more preferably greater than 110 ℃ heavy naphthas, mix, react with regenerator from regenerator sloped tube 4.1, reactant flow enters the settling vessel 5 ' that has or do not have the dense fluidized bed bioreactor, the separating of realization response oil gas and catalyzer.Reaction oil gas and water vapor together enter separation column 10 through pipeline 15 and reaction oil gas from conventional settling vessel 5 tops.Reacted gas, gasoline fraction and water vapor are distillated by the top of separation column, enter first-stage condenser 11, condensation goes out water vapor and initial boiling point greater than 100 ℃ or greater than 110 ℃ heavy naphtha, reacted gas and do less than 100 ℃ or distillate less than 110 ℃ the light gasoline fraction top by first-stage condenser 11 enters secondary condenser 12.Meanwhile, the pyritous regenerated catalyst enters the bottom of conventional riser tube 2 ' through regenerator sloped tube 4 ', is promoted by pre-lifting medium; Conventional cracking stock after the preheating enters the bottom of riser tube 2 ' through pipeline 13, and reacts after high-temperature regenerated catalyst mixes, and reactant flow enters the settling vessel 5 that has or do not have the dense fluidized bed bioreactor; The reaction oil gas of conventional cracking stock and water vapor together enter separation column 10 through pipeline 9 and oil gas from settling vessel 5 '.The reclaimable catalyst of gasoline reactor enters stripper 17, behind the water vapor stripping, enter conventional settling vessel 5 by transfer lime 7, together enter stripper 14 with reclaimable catalyst from the stock oil riser tube, catalyzer behind the stripping enters revivifier 6, reclaimable catalyst is coke burning regeneration in air, and regenerated flue gas is drawn by the top of revivifier.The pyritous regenerator is divided into two portions, and wherein a part is returned stock oil riser tube 2 ' through regenerator sloped tube 4 '; Another part enters water cooler 3 through regenerator sloped tube 4, after the cooling, returns gasoline rising pipe 2 by regenerator sloped tube 4.1 and recycles according to a conventional method.
The following examples will be further specified method provided by the invention, but therefore not make the present invention be subjected to any restriction.Employed catalyzer of embodiment and raw material oil properties are listed in table 1 and table 2 respectively.Catalyzer in the table 1 is by Qilu Petrochemical company of China PetroChemical Corporation catalyst plant industrial production.
Method provided by the invention is adopted in the present embodiment explanation, uses dissimilar catalyzer catalyzed conversion in the small-sized fluidized bed reactor to improve the situation of gasoline octane rating.
Is raw material with the listed initial boiling point of table 2 greater than 110 ℃ heavy naphtha C, uses the listed four kinds of dissimilar catalyzer of table 1, carries out the test that gasoline catalyzing transforms boosting of octane rating in the small-sized fluidized bed reactor of successive reaction regenerative operation.Heavy naphtha C mixes with high-temperature water vapor laggardly to go in the fluidized-bed reactor, is 450 ℃ in temperature of reaction, and reactor head pressure is 0.2 MPa, and weight hourly space velocity is 4 hours
-1, agent-oil ratio is 6, water-oil ratio is to contact the reaction of carrying out the catalyzed conversion boosting of octane rating under 0.03 the condition with catalyzer.Reaction product, steam and reclaimable catalyst separate in settling vessel, and reaction product isolated obtains gaseous product and product liquid, and reclaimable catalyst enters stripper, is gone out the hydrocarbon product that adsorbs on the reclaimable catalyst by the water vapor stripping.Catalyzer behind the stripping enters into revivifier, contacts with the warm air that heated and regenerates, and the catalyzer cooling after the regeneration turns back to reactor cycles again and uses.Test conditions, product distribute and the character of gasoline is all listed in table 3.
As can be seen from Table 3, dissimilar catalyzer has certain influence to the result of gasoline stocks catalytic conversion reaction.When using four kinds of listed catalyzer, can make the octane value of gasoline improve 3～5 units.From the group composition data of gasoline as can be seen, when 450 ℃ temperature of reaction, last running gasoline is main in catalytic conversion process, and conversion of olefines takes place is the reaction of isoparaffin, and a spot of aromatization.In addition, the sulphur content in the gasoline has been fallen more than the 980ppm, and decreasing ratio is near 50%; Nitrogen content drops to 1.2～3.0ppm, and decreasing ratio has reached 90%.
Method provided by the invention is adopted in the present embodiment explanation, uses dissimilar gasoline stocks, the situation of catalyzed conversion boosting of octane rating in the small-sized fluidized bed reactor.
The four kind gasoline listed with table 2 are raw material, use the listed catalyst A of table 1, and its coke content is 0.05 heavy %, carry out gasoline catalyzing and transform the boosting of octane rating test in the small-sized fluidized bed reactor of successive reaction regenerative operation.Concrete testing sequence is identical with embodiment 1.
Test conditions, product distribute and the character of gasoline is listed in table 4.As can be seen from Table 4, dissimilar catalytic cracking heavy petrol are behind catalyzed conversion, and the octane value of gasoline all is greatly improved.In addition, the sulphur content in the raw material is high more, and then the ratio that removes of sulphur is just big more.
Embodiment 3
Method provided by the invention is adopted in the present embodiment explanation, and gasoline stocks adopts different operational conditions, the situation of catalyzed conversion boosting of octane rating in the small-sized fluidized bed reactor.
Listed gasoline C is a raw material with table 2, uses the listed catalyst A of table 1, and its coke content is 0.05 heavy %, carries out gasoline catalyzing and transform the boosting of octane rating test in the small-sized fluidized bed reactor of successive reaction regenerative operation.Main operational condition is: temperature of reaction is that 350～650 ℃, reactor head pressure are that 0.2 MPa, weight hourly space velocity are 4～10 hours
-1, agent-oil ratio is 3～8, water-oil ratio is 0.03～0.05.Concrete testing sequence is identical with embodiment 1.Test conditions, product distribute and the character of gasoline is listed in table 5.
As can be seen from Table 5, different operational conditions when temperature is low, mainly is that the isoparaffin increase is more to gasoline stocks catalyzed conversion influence degree difference; When temperature is higher, then be that the content of aromatic hydrocarbons increases more.Sulphur content in the gasoline and nitrogen content, particularly sulphur content all reduces along with the raising of temperature of reaction.In trial stretch, the RON of gasoline has improved 3～9 units, and MON has improved 3～6 units.
Method provided by the invention is adopted in the present embodiment explanation, and initial boiling point improves the situation of gasoline octane rating greater than catalytic cracking last running gasoline catalyzed conversion on medium-sized riser fluid catalytic cracking of 110 ℃.This test-results is in order to the gasoline rising pipe in the simulated dual riser reactor.
Listed gasoline C is a raw material with table 2, uses the listed catalyst A of table 1, and its coke content is 0.05 heavy %, carries out the test that gasoline catalyzing transforms boosting of octane rating, reduces sulphur, nitrogen content on the medium-sized riser fluid catalytic cracking of successive reaction regenerative operation.Initial boiling point greater than 110 ℃ catalytic cracking last running gasoline stocks with enter the riser tube bottom after high-temperature water vapor mixes, contact with 550 ℃ of regenerated catalysts and to carry out catalytic conversion reaction, reaction conditions is as follows: temperature of reaction is 550 ℃, reactor head pressure is 0.2 MPa, and weight hourly space velocity is 50 hours
-1, agent-oil ratio is 6, water-oil ratio is 0.03.Reaction product, steam and reclaimable catalyst separate in settling vessel, and reaction product is gone to separate and obtained gaseous product and product liquid, and reclaimable catalyst enters stripper, is gone out the hydrocarbon product that adsorbs on the reclaimable catalyst by the water vapor stripping.Catalyzer behind the stripping enters into revivifier, contacts with the warm air that heated and regenerates, and the catalyzer after the regeneration turns back to reactor cycles and uses after cooling.Test conditions, product distribute and gasoline property is listed in table 6.
As can be seen from Table 6, the RON of gasoline and MON have improved 4.5 and 3.6 units respectively.Sulphur content in the gasoline drops to 784ppm, and nitrogen content drops to 1.3ppm.
Comparative Examples
The explanation of this Comparative Examples: with catalytic cracking full distillate gasoline is raw material, the test-results when other operational conditions are all identical with embodiment 4.
The character of the catalytic cracking full distillate gasoline that this Comparative Examples adopted sees Table 7, and test-results sees Table 6.As can be seen from Table 6, when adopting full distillation gasoline to be raw material, not only octane value improves seldom, and the yield of gasoline is low, and desulfurization, denitrification percent are also lower.
Table 1
Catalyzer numbering A B C D
Trade names CRC-1 RHZ-200 ZCM-7 RAG-1
Zeolite type REY REHY USY REY-USY-ZRP
Chemical constitution, heavy %
Aluminum oxide 26.5 33.0 46.4 44.6
Sodium oxide 0.19 0.29 0.22 0.13
Ferric oxide 0.09 1.1 0.32/
Apparent density, kilogram/rice
3450 560 690 620
Pore volume, milliliter/gram 0.41 0.25 0.38 0.36
Specific surface area, rice
2Restrain 132 92 164 232
Abrasion index is when weighing %
-14.2 3.2/2.5
Size composition, heavy %
0～40 micron 7.3 15.2 4.8 13.1
40～80 micron 43.7 55.1 47.9 54.9
＞80 micron 49.0 29.7 47.3 32.0
Micro-activity 70 68 69 66
Table 2
Gasoline stocks numbering A B C D
Group composition (chromatogram), heavy %
Normal paraffin 5.1 4.9 5.5 5.2
Isoparaffin 19.5 18.2 15.8 14.8
Alkene 25.4 24.1 23.1 30.5
Naphthenic hydrocarbon 12.8 16.3 13.1 14.3
Aromatic hydrocarbons 37.2 36.5 42.5 35.2
Octane value
RON 88.2 87.4 87.5 86.3
MON 78.5 78.0 78.2 77.9
Sulphur, microgram/gram 1,500 1,600 2,000 1000
Nitrogen, microgram/gram 45 24 30 16
Boiling range, ℃
Initial boiling point 110 109 112 111
5％ 117 120 119 121
10％ 126 129 128 127
30％ 139 142 140 136
50％ 158 164 160 153
70％ 180 182 178 161
Do 203 204 204 183
Table 3
Catalyst A B C D
Temperature of reaction, ℃ 450 450 450 450
Weight hourly space velocity, hour
-14444
Agent-oil ratio 6666
Water-oil ratio 0.03 0.03 0.03 0.03
Product distributes, heavy %
Dry gas 1.36 0.87 0.65 0.56
Liquefied gas 3.87 4.69 4.76 4.93
Gasoline 85.97 86.85 88.70 89.95
Solar oil 4.37 3.98 3.01 2.36
Heavy gas oil 2.43 2.02 1.63 1.23
Coke 1.98 1.56 1.23 0.93
Lose 0.02 0.03 0.02 0.04
Gasoline property
Sulphur, microgram/gram 952 964 980 1020
Nitrogen, microgram/gram 1.2 2.2 3.0 2.4
Octane value
RON 91.5 91.3 92.2 92.5
MON 81.7 81.5 82.0 82.1
Group composition, heavy %
Normal paraffin 4.05 3.98 3.85 3.42
Isoparaffin 36.82 37.19 37.22 38.24
Alkene 7.27 7.68 7.42 6.02
Naphthenic hydrocarbon 5.57 5.17 4.92 4.98
Aromatic hydrocarbons 46.29 45.98 46.59 47.34
Table 4
Gasoline numbering A B C D
Reaction conditions
Temperature of reaction, ℃ 450 450 450 450
Weight hourly space velocity, hour
-14444
Agent-oil ratio 6666
Water-oil ratio 0.03 0.03 0.03 0.03
Product distributes, heavy %
Dry gas 1.42 1.4 1.36 1.48
Liquefied gas 4.11 4.08 3.87 4.25
Gasoline 85.43 85.64 85.97 84.58
Solar oil 4.41 4.36 4.37 4.85
Heavy gas oil 2.52 2.48 2.43 2.58
Coke 2.09 2.01 1.98 2.24
Lose 0.02 0.03 0.02 0.02
Gasoline property 1,500 1,600 2,000 1000
Sulphur, microgram/gram 736 758 952 524
Nitrogen, microgram/gram 4.8 2.2 1.2 0.8
Octane value
RON 91.2 91.0 91.5 90.9
MON 81.5 81.1 81.7 81.0
Group composition, heavy %
Normal paraffin 4.32 4.74 4.05 4.32
Isoparaffin 39.03 38.48 36.82 36.56
Alkene 8.69 8.06 7.27 11.27
Naphthenic hydrocarbon 5.09 6.21 5.57 5.29
Aromatic hydrocarbons 42.87 42.51 46.29 42.56
Table 5
Reaction conditions
Temperature, ℃ 350 450 450 550 650
Weight hourly space velocity, hour
-144 10 4 10
Agent-oil ratio 66366
Water-oil ratio 0.03 0.03 0.05 0.03 0.05
Product distributes, heavy %
Dry gas 0.56 1.36 1.25 3.04 4.52
Liquefied gas 1.96 3.87 3.62 10.02 13.15
Gasoline 90.02 85.97 86.95 80.01 74.02
Solar oil 3.47 4.37 4.01 2.36 2.15
Heavy gas oil 1.86 2.43 2.21 1.53 1.85
Coke 2.07 1.98 1.93 3.01 4.26
Lose 0.06 0.02 0.03 0.03 0.05
Gasoline property
Octane value
RON 90.5 91.5 91.4 93.8 96.3
MON 81.2 81.2 81.1 83.8 84.2
Sulphur, microgram/gram 1,010 952 963 724 685
Nitrogen, microgram/gram 3.1 1.2 1.8 0.8 0.4
Group composition, heavy %
Normal paraffin 4.21 4.05 4.11 3.01 1.22
Isoparaffin 30.78 36.82 35.48 33.26 30.21
Alkene 15.05 7.27 8.61 5.26 2.08
Naphthenic hydrocarbon 6.52 5.57 5.82 4.02 3.21
Aromatic hydrocarbons 43.44 46.29 45.98 54.45 63.28
Table 6
Temperature, 550 550
Weight hourly space velocity, hour
-150 50
Agent-oil ratio 6.0 6.0
Water-oil ratio 0.03 0.03
Product distributes, heavy %
Dry gas 3.1 4.42
Liquefied gas 5.98 7.66
Gasoline 80.67 75.98
Solar oil 4.24 4.52
Heavy gas oil 3.01 4.05
Coke 2.98 3.32
Lose 0.02 0.05
Gasoline property
Octane value
RON 92.5 91.3
MON 83.5 81.5
Sulphur, microgram/gram 784 685
Nitrogen, microgram/gram 1.3 1.1
Group composition, heavy %
Normal paraffin 3.21 4.01
Isoparaffin 32.85 35.97
Alkene 7.52 19.24
Naphthenic hydrocarbon 4.38 5.26
Aromatic hydrocarbons 52.04 35.52
Table 7
The full distillation gasoline of gasoline stocks FCC
Group composition (chromatogram), heavy %
Normal paraffin 5.51
Isoparaffin 18.97
Alkene 44.24
Naphthenic hydrocarbon 6.26
Aromatic hydrocarbons 25.02
Octane value
RON 91.2
MON 80.5
Sulphur, microgram/gram 1000
Nitrogen, microgram/gram 23
Boiling range, ℃
Initial boiling point 39
5％ 43
10％ 51
30％ 68
50％ 89
70％ 135
Do 203
Claims (10)
1, a kind of catalysis conversion method that improves gasoline octane rating is to make initial boiling point be lower than 700 ℃ catalyzer greater than 100 ℃ heavy naphtha and temperature to contact, at 300～660 ℃ of temperature of reaction, reaction pressure 130～450Kpa, weight hourly space velocity 1～120h
-1, catalyzer and gasoline fraction weight ratio be 2～20, the weight ratio of water vapor and gasoline fraction is to react under 0～0.1 the condition, reaction product isolated and spent agent, spent agent recycles after stripping, regeneration.
2,, it is characterized in that described heavy naphtha is an initial boiling point greater than 110 ℃ heavy naphtha according to the method for claim 1.
3,, it is characterized in that the process preheating before injecting reactor of described heavy naphtha according to the method for claim 1 or 2.
4, according to the method for claim 1, what it is characterized in that described and initial boiling point contact greater than 100 ℃ heavy naphtha is that temperature is lower than 700 ℃ catalyzer.
5, according to the method for claim 1, it is characterized in that this method is to implement separately on the riser tube of handling the heavy petrol raw material or fluidized bed catalytic cracker, or with the riser tube or the fluidized bed catalytic cracker Joint Implementation of the conventional catalytically cracked material of processing.
6,, it is characterized in that gasoline fraction and conventional catalytically cracked material react respectively when adopting the mode of Joint Implementation in reactor separately according to the method for claim 5; And settling vessel, stripper and subsequent separation system are shared, or separately independently; The regeneration system rapidly of catalyzer is shared.
7,, it is characterized in that when adopting the mode of Joint Implementation, the catalyzer that contacts with heavy naphtha is identical with the catalyzer that contacts with conventional catalytically cracked material, or different according to the method for claim 5 or 6.
8,, it is characterized in that 350～600 ℃ of temperature of reaction, reaction pressure 250～400Kpa, weight hourly space velocity 2～100h according to the method for claim 1
-1, the weight ratio of catalyzer and gasoline fraction is 3～10, the weight ratio of water vapor and gasoline fraction is 0.01～0.05.
9,, it is characterized in that described heavy naphtha is an initial boiling point greater than 110 ℃ and the final boiling point heavy naphtha less than 180 ℃ according to the method for claim 2.
10, according to the method for claim 1, it is characterized in that describedly sending into separation column with the reaction product after spent agent separates, reacted gas, gasoline and water vapor enter first-stage condenser after being extracted out by fractionator overhead, making initial boiling point is liquid phase greater than 100 ℃ heavy naphtha and water vapor condensation, water of condensation is extracted out by this condenser bottom, and initial boiling point is extracted the back out as the heavy petrol charging greater than 100 ℃ heavy naphtha by the side line of this condenser; Reacted gas and initial boiling point enter the further condensation of secondary condenser less than 100 ℃ gasoline fraction through the first-stage condenser top; Initial boiling point is extracted out by the bottom of secondary condenser less than 100 ℃ gasoline fraction, and rich gas is drawn by the top of secondary condenser.
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| CN101469274B (en) * | 2007-12-28 | 2012-06-27 | 中国石油化工股份有限公司 | Method for producing high-octane petrol |
| US10266778B2 (en) | 2015-02-04 | 2019-04-23 | China University Of Petroleum-Beijing | Method for upgrading fluid catalytic cracking gasoline |
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| JP2003238970A (en) * | 2001-12-13 | 2003-08-27 | Idemitsu Kosan Co Ltd | Method for producing low-sulfur gasoline base material |
| EP1357167A1 (en) * | 2002-04-18 | 2003-10-29 | Haldor Topsoe A/S | Process for production of high quality gasoline with low aromatic content |
| CN1258580C (en) * | 2002-07-05 | 2006-06-07 | 石油大学(北京) | Upgrading method and system of heavily reducing olefinic hydrocarbon and increasing octane rating for catalytically cracked gasoline |
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| CN101469274B (en) * | 2007-12-28 | 2012-06-27 | 中国石油化工股份有限公司 | Method for producing high-octane petrol |
| US10266778B2 (en) | 2015-02-04 | 2019-04-23 | China University Of Petroleum-Beijing | Method for upgrading fluid catalytic cracking gasoline |
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