CN1100117C - Method for increasing liquefied gas yield and gasoline octane number - Google Patents
Method for increasing liquefied gas yield and gasoline octane number Download PDFInfo
- Publication number
- CN1100117C CN1100117C CN00100398A CN00100398A CN1100117C CN 1100117 C CN1100117 C CN 1100117C CN 00100398 A CN00100398 A CN 00100398A CN 00100398 A CN00100398 A CN 00100398A CN 1100117 C CN1100117 C CN 1100117C
- Authority
- CN
- China
- Prior art keywords
- catalyst
- zeolite
- oil
- gasoline
- weight
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired - Fee Related
Links
Landscapes
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
一种提高液化气产率和汽油辛烷值的方法，是将来自催化裂解装置和/或多产气态烯烃和高辛烷值汽油的催化转化装置的平衡催化剂从再生器上的催化剂补充口加入，与来自汽提器的含炭的常规裂化催化剂一起烧焦再生，再生后的催化剂在预提升介质的提升作用下从提升管下部进入，与从提升管的底部或下部进入的原料接触，生成的油气与待生催化剂颗粒进入沉降器，分离出的油气去分馏，待生催化剂经汽提、烧焦再生后循环使用。该方法不仅提高了汽油的辛烷值，而且还增加了液化气的产率，既充分利用了催化剂的资源，也有利于环境保护。A method to increase the yield of liquefied gas and the octane number of gasoline is to add the equilibrium catalyst from the catalytic cracking unit and/or the catalytic conversion unit that produces more gaseous olefins and high-octane gasoline from the catalyst replenishment port on the regenerator , together with the carbon-containing conventional cracking catalyst from the stripper for coke regeneration, the regenerated catalyst enters from the lower part of the riser under the lifting effect of the pre-lift medium, and contacts the raw material entering from the bottom or lower part of the riser to form The oil gas and catalyst particles to be used enter the settler, the separated oil and gas are fractionated, and the catalyst to be used is recycled after being stripped and burnt. The method not only increases the octane number of gasoline, but also increases the yield of liquefied gas, which not only makes full use of catalyst resources, but also is beneficial to environmental protection.
Description
The present invention relates to a kind of under the situation that does not have hydrogen the catalysis conversion method of hydrocarbon ils, specifically, be a kind of method that improves liquefied gas yield and gasoline octane rating.
Usually adopt catalytic cracking, thermo-cracking or catalytic thermal cracking method from petroleum hydrocarbon production liquefied gas and gasoline.
If conventional cracking catalyst is adopted in conventional catalytic cracking, though can obtain the gasoline of high yield, the octane value of gasoline can not satisfy the requirement of blending commercial gasoline, and yield of liquefied gas is lower, and especially propylene, butylene are few.
Thermo-cracking mainly is to be purpose to produce ethene, and the octane value of product gasoline is lower, needs higher temperature of reaction and corresponding high temperature resistant reaction equipment material more than 700 ℃.
CN1102431A discloses a kind of catalytic cracking method of low-carbon olefines high-output, be that the petroleum hydrocarbon of preheating is contacted with solid acid catalyst, in temperature is that 480～680 ℃, duration of contact are that 0.1～6.0 second, agent-oil ratio are 4～20: 1, the weight ratio of water vapor and stock oil is to carry out catalytic conversion reaction under 0.01～0.5: 1 the condition, and separated product obtains low-carbon alkene and liquid product.Wherein the active ingredient of solid acid catalyst is made up of the five-ring supersiliceous zeolite that contains rare earth and phosphorus of 25～100 heavy %, the type-Y high silicon zeolite of 0～75 heavy % and the y-type zeolite that contains rare earth of 0～25 heavy %, and carrier is selected from aluminum oxide, pure aluminium silicate or natural clay-aluminum oxide.
CN1085885A disclosed the method that a kind of fecund is rich in the liquefied gas and the stop bracket gasoline of propylene, butylene, and raw material hydrocarbon contacts with solid acid catalyst in riser tube or fluidized-bed reactor, 480～550 ℃, heavy hourly space velocity 1～150 hour
-1, catalyzer and raw material hydrocarbon weight ratio be 4～15, water vapor and raw material hydrocarbon weight ratio be to carry out conversion reaction under 0.05～0.12: 1 the condition.The productive rate of liquefied gas reaches 30～40 heavy % on middle-scale device, and the productive rate of gasoline reaches 40～55 heavy %.Wherein solid acid catalyst is to be active ingredient with the rare-earth five-membered ring supersiliceous zeolite that contains that accounts for the heavy % of catalyst weight 10～40, and is aided with the full synthesis carrier of surplus or contains the semi-synthetic carrier of 10～40 heavy % (in catalyst weight) silicon and/or al binder and constitute.
The used catalyzer of the method for mentioning among CN1102431A, the CN1085885A all is microspheroidal, and micro-spherical catalyst is experiencing the process of living and wearing and tearing of falling in reaction.The result of wearing and tearing produces the thinner microballoon of comparatively fresh agent granularity, and the thinner microsphere particle of major part can be reclaimed by the cyclonic separator on revivifier top, and small amount of fines will escape into atmosphere.Keep constantly for the catalyst inventory that makes reactor, need constantly termly live catalyst to be added reaction-regeneration system.Catalyzer is experiencing the reaction-regenerative process under the high-temperature water heat condition repeatedly in catalytic cracking unit, causes the decline of catalyst activity.In order to make in the device catalyzer keep the certain activity level, need from revivifier, draw off a part of old catalyzer, add a certain amount of live catalyst simultaneously.The live catalyst of adding apparatus is active high, and the catalyst activity that adds was low in the past, thereby activity of such catalysts is the total effect of different times adding apparatus (being different ages) catalyst activity, i.e. equilibrium catalyst activity in the device.The catalyzer that draws off from catalytic cracking unit is equilibrium catalyst.The performance of equilibrium catalyst and activity level depend on composition and its natural characteristics, process conditions and the live catalyst supplementary rate of live catalyst.When process conditions and catalyst make-up rate were determined, the composition of live catalyst and natural characteristics had determined the performance of equilibrium catalyst.The equilibrium catalyst that draws off in the device of mentioning from CN1102431A, CN1085885A is because active on the low side, except that going into operation as new device with the agent, general discarded, this not only causes environmental pollution, and its active ingredient five-ring supersiliceous zeolite also is not fully utilized.
The objective of the invention is to provide on the basis of existing technology the method that a kind of process is simple, can improve liquefied gas yield and gasoline octane rating simultaneously.
Method provided by the invention is: will add from the catalyst make-up mouth on the revivifier from the equilibrium catalyst of other catalytic convention design, with the conventional cracking catalyst coke burning regeneration that contains charcoal from stripper, catalyzer after the regeneration enters from the riser tube bottom under the castering action of pre-lifting medium, contact with the raw material that bottom or bottom from riser tube enters, the oil gas and the reclaimable catalyst particle that generate enter settling vessel, isolated oil gas goes fractionation plant further to separate, the reclaimable catalyst particle enters stripper and enter the revivifier coke burning regeneration behind stripping medium stripping, and the regenerated catalyst Returning reactor recycles.
The used raw material of the present invention is selected from one or more the mixture in solar oil, vacuum gas oil, coker gas oil, deasphalted oil, hydrofined oil, hydrocracking tail oil, vacuum residuum, the long residuum.
The reaction conditions of riser reactor is: temperature of reaction is 500～540 ℃, and the reaction times is 2～4 seconds, the weight ratio 6～12: 1 of catalyzer and stock oil, the weight ratio 0.01～0.08: 1 of water vapor and raw material.
Is 0.01～0.5: 1 from the equilibrium catalyst of other catalytic convention design with weight ratio from the reclaimable catalyst of stripper.
The used conventional active component of cracking catalyst of the present invention is REY type zeolite, USY type zeolite or HY type zeolite, carrier is a clay, clay can be natural or synthetic, through or without various chemistry and/or physical treatment, as kaolin and halloysite etc.
Other used catalytic convention design equilibrium catalyst of the present invention comes from the devices such as catalyzed conversion of catalytic pyrolysis, voluminous gaseous olefin and stop bracket gasoline, and this activity of such catalysts is lower, and micro-activity (MAT) is generally 55～65.Equilibrium catalyst weighs the % zeolites and the full synthesis carrier of surplus or the semi-synthetic carrier of siliceous and/or al binder by 10～40 and constitutes.Zeolite can be the mixture that five-ring supersiliceous zeolite and the y-type zeolite by phosphorous and rare earth constitutes, and wherein the five-ring supersiliceous zeolite accounts for zeolite content and is 25～75 heavy %, and is phosphorous (with P in the five-ring supersiliceous zeolite
2O
5Meter) 2～20 heavy % contain rare earth (with RE
2O
3Meter) 2～10 heavy %; Zeolite also can be by containing the mixture that rare-earth five-membered ring supersiliceous zeolite, REY zeolite and type-Y high silicon zeolite constitute, and wherein to account for zeolite content be 3～50 heavy % to the five-ring supersiliceous zeolite.Full synthesis carrier is, SiO that glue method or step-by-step precipitation method are made with being total to
2Content is not more than amorphous aluminum silicide or the silicon magnesium of 70 heavy %.The binding agent of semi-synthetic carrier is Al
2O
3, SiO
2, SiO
2Al
2O
3, semi-synthetic carrier medium clay soil is kaolin or halloysite.
Y-type zeolite in this catalyzer can be that the content of rare earth that obtains after rare earth ion exchange is (with RE
2O
3Meter) being not less than the REY zeolite of 14 heavy %, also can be through various chemistry and/or physical method,, stabilization higher as the silica alumina ratio that obtains after the processing such as hydrothermal method, acidic treatment, aluminium-eliminating and silicon-replenishing method, silicon tetrachloride method type-Y high silicon zeolite.
The five-ring supersiliceous zeolite (trade names are ZRP) that contains rare earth has the x-ray diffraction spectra of ZSM-5 zeolite family, and its anhydrous chemical constitution expression formula is: 0.01～0.3RE
2O
30.4～1.0Na
2OAl
2O
320～60SiO
2, the used faujasite seeds that contains rare earth when synthetic of the rare earth in this composition, the orifice throat ratio ZSM-5 zeolite of this zeolite narrow, it is 2～4 times of ZSM-5 zeolite to the ratio of the adsorptive capacity of normal hexane and hexanaphthene.This zeolite is a raw material with water glass, aluminum phosphate and mineral acid promptly with the preparation of CN1058382A disclosed method, is crystal seed with REY or REHY zeolite, makes in 12～60 hours 130～200 ℃ of following crystallization.
The method for making of the used live catalyst of other catalytic convention design is as follows:
When adopting full synthesis carrier, the Preparation of catalysts method is: above-mentioned zeolite is made mixed serum in predetermined ratio, add with being total to amorphous aluminum silicide or the silicon magnesium slurries that glue method or step-by-step precipitation method are made, homogeneous aftershaping, washing, drying.
When adopting semi-synthetic carrier, the Preparation of catalysts method is: will be selected from the binding agent precursor of aluminium colloidal sol, pseudo-boehmite, silicon sol, silicon-aluminum sol and the clay slurry of predetermined amount and mix, aging or not aging, mixed serum with above-mentioned zeolite adds wherein homogeneous aftershaping, washing, drying then.
The ZRP zeolite that the equilibrium catalyst that draws off from the processes such as catalyzed conversion of other catalytic convention design such as catalytic pyrolysis, voluminous gaseous olefin and gasoline has the good hydrothermal stability of q.s, this equilibrium catalyst joined in the conventional catalytic cracking unit as octane enhancing additive go, not only improve the octane value of gasoline, but also increased the productive rate of liquefied gas.Method provided by the invention has made full use of the resource of catalyzer, also helps environment protection.
The following examples will give further instruction to method provided by the invention, but not thereby limiting the invention.
Testing raw materials used is solar oil A, B, its character is as shown in table 1, the equilibrium catalyst CRC of used conventional catalytic cracking is taken from the Cangzhou Refinery catalytic cracking unit, the equilibrium catalyst CRP-1 that contains the ZRP zeolite takes from Anqing refinery cat-cracker, and the equilibrium catalyst RMG that contains the ZRP zeolite is a catalytic convention design of taking from Lanzhou Oil Refinery fecund gaseous olefin and stop bracket gasoline.Above-mentioned three kinds of catalyzer are all produced by Qilu Petrochemical company Zhou village catalyst plant, and its character is as shown in table 2.Test is carried out on micro-reaction equipment, and operational condition is: 500 ℃ of temperature of reaction, agent-oil ratio 3.2, weight space velocity 16 hours
-1, the catalyzer loading amount is 5.0 grams.The octane value of gasoline is tested with chromatography.
Comparative Examples 1
The equilibrium catalyst CRP-1 or the RMG that do not add catalytic pyrolysis or voluminous gaseous olefin and stop bracket gasoline process, but conventional cracking catalyst CRC directly contacts with solar oil A were 500 ℃ of temperature, agent-oil ratio 3.2, weight hourly space velocity 1.6 hours
-1Condition under react, test-results is as shown in table 3.As can be seen from Table 3, C
2 =+ C
3 =+ C
4 =Yield only be 6.09 heavy %, Study of Gasoline method octane value (following brief note is RON), motor-method octane number (following brief note is MON) have only 90 and 80 respectively.
Embodiment 1
After catalytic pyrolysis equilibrium catalyst CRP-1 and conventional cracking catalyst CRC mixed by weight 0.1: 1, A contacted with solar oil, is 1.6 hours in 500 ℃ of temperature, agent-oil ratio 3.2, weight hourly space velocity
-1Condition under react, test-results is as shown in table 3.As can be seen from Table 3, C
2 =+ C
3 =+ C
4 =Yield be 8.82 heavy %, the RON of gasoline and MON are respectively 91.7,80.9.
Embodiment 2
After catalytic pyrolysis equilibrium catalyst CRP-1 and conventional cracking catalyst CRC mixed by weight 0.8: 1, A contacted with solar oil, 500 ℃ of temperature, agent-oil ratio 3.2, weight hourly space velocity 1.6 hours
-1Condition under react, test-results is as shown in table 3.As can be seen from Table 3, C
2 =+ C
3 =+ C
4 =Yield be 13.60 heavy %, RON and MON are respectively 92.0 and 81.0.
Embodiment 3
After the equilibrium catalyst RMG of voluminous gaseous olefin and stop bracket gasoline process and conventional cracking catalyst CRC mixed by weight 0.12: 1, A contacted with vacuum gas oil, 500 ℃ of temperature, agent-oil ratio 3.2, weight hourly space velocity 1.6 hours
-1Condition under react, test-results is as shown in table 4.As can be seen from Table 4, C
2 =+ C
3 =+ C
4 =Yield be 7.95 heavy %, RON and MON are respectively 91.5 and 81.0.
Embodiment 4
After the equilibrium catalyst RMG of voluminous gaseous olefin and stop bracket gasoline process and conventional cracking catalyst CRC mixed by weight 0.30: 1, A contacted with solar oil, 500 ℃ of temperature, agent-oil ratio 3.2, weight hourly space velocity 1.6 hours
-1Condition under react, test-results is as shown in table 4.As can be seen from Table 4, C
2 =+ C
3 =+ C
4 =Yield be 9.35 heavy %, RON and MON are respectively 91.7 and 81.2.
Embodiment 5
After the equilibrium catalyst RMG of voluminous gaseous olefin and stop bracket gasoline process and conventional cracking catalyst CRC mixed by weight 0.15: 1, A contacted with solar oil, 500 ℃ of temperature, agent-oil ratio 3.2, weight hourly space velocity 1.6 hours
-1Condition under react, test-results is as shown in table 4.As can be seen from Table 4, C
2 =+ C
3 =+ C
4 =Yield be 10.57 heavy %, RON and MON are respectively 91.9 and 81.5.
Embodiment 6
After catalytic pyrolysis equilibrium catalyst CRP-1 and conventional cracking catalyst CRC mixed by weight 0.05: 1, B contacted with solar oil, 500 ℃ of temperature, agent-oil ratio 3.2, weight hourly space velocity 1.6 hours
-1Condition under react, test-results is as shown in table 5.As can be seen from Table 5, C
2 =+ C
3 =+ C
4 =Yield be 6.78 heavy %, the RON of gasoline and MON are respectively 90.0 and 80.0.
Embodiment 7
After catalytic pyrolysis equilibrium catalyst CRP-1 and conventional cracking catalyst CRC mixed by weight 0.8: 1, B contacted with solar oil, 500 ℃ of temperature, agent-oil ratio 3.2, weight hourly space velocity 1.6 hours
-1Condition under react, test-results is as shown in table 5.As can be seen from Table 5, C in the liquefied gas
2 =+ C
3 =+ C
4 =Yield be 9.98 heavy %, the RON of gasoline and MON are respectively 91.0 and 80.5.
Comparative Examples 2
Compare with embodiment 6 or 7, do not add catalytic pyrolysis equilibrium catalyst CRP-1, but conventional cracking catalyst CRC directly contacts with solar oil B, 500 ℃ of temperature, agent-oil ratio 3.2, weight hourly space velocity 1.6 hours
-1Condition under react, test-results is as shown in table 5.As can be seen from Table 5, C in the liquefied gas
2 =+ C
3 =+ C
4 =Yield only be 5.33 heavy %, the RON of gasoline and MON have only 89.0 and 79.0 respectively.
Table 1
| Raw material | Solar oil A | Solar oil B |
| Density (20 ℃), gram per centimeter 3 | 0.8454 | 0.8170 |
| Kinematic viscosity (20 ℃), centistoke | 5.70 | 5.60 |
| Aniline point, ℃ | 72.2 | 80.1 |
| Boiling range, ℃ | 229～340 | 225～330 |
Table 2
| The equilibrium catalyst trade mark | CRC | CRP-1 | RMG |
| Zeolite type | REY | ZRP+USY | ZRP+USY+REY |
| Chemical constitution, heavy % | |||
| Aluminum oxide | 50 | 45 | 40 |
| Sodium oxide | 0.14 | 0.15 | 0.35 |
| Ferric oxide | 0.70 | 0.90 | 0.90 |
| Apparent density, kilogram/rice 3 | 880 | 930 | 760 |
| Pore volume, milliliter/gram | 100 | 111 | 107 |
| Specific surface area, rice 2/ gram | 0.11 | 0.23 | 0.27 |
| Abrasion index is when weighing % -1 | 2.0 | 2.0 | 0.7 |
| Size composition, heavy % | |||
| 0～40 micron | 21 | 29.3 | 14.8 |
| 40～80 microns | 63.8 | 63.9 | 64.2 |
| ＞80 microns | 15.2 | 6.8 | 21.0 |
Table 3
| Numbering | Comparative Examples 1 | Embodiment 1 | Embodiment 2 |
| Raw material | A | A | A |
| Catalyzer | |||
| CRP-1/CRC, weight ratio | 0 | 0.10 | 0.50 |
| ZRP content (accounting for reserve), heavy % | 0 | 1.4 | 6.7 |
| Reaction conditions | |||
| Temperature, ℃ | 500 | 500 | 500 |
| Agent-oil ratio | 3.2 | 3.2 | 3.2 |
| Weight hourly space velocity, hour -1 | 1.6 | 1.6 | 1.6 |
| Test-results | |||
| Transformation efficiency | 69 | 70 | 69 |
| Product distributes, heavy % | |||
| Reacted gas | 11.29 | 15.40 | 21.99 |
| C wherein 2 ＝ | 0.30 | 0.39 | 0.70 |
| C 3 ＝ | 3.03 | 4.85 | 7.49 |
| C 4 ＝ | 2.76 | 3.58 | 5.41 |
| Gasoline ( C5～216℃) | 51.02 | 47.81 | 41.12 |
| Diesel oil (＞216 ℃) | 31.23 | 30.40 | 30.77 |
| C 2 ＝+C 3 ＝+C 4 ＝ | 6.09 | 8.82 | 13.60 |
| Gasoline octane rating | |||
| RON | 90 | 91.7 | 92.0 |
| MON | 80 | 80.9 | 81.0 |
Table 4
| Numbering | Embodiment 3 | Embodiment 4 | Embodiment 5 |
| Raw material | A | A | A |
| Catalyzer | |||
| RMG/CRC, weight ratio | 0.12 | 0.30 | 0.45 |
| ZRP content (accounting for reserve), heavy % | 1.4 | 2.5 | 5.5 |
| Reaction conditions | |||
| Temperature, ℃ | 500 | 500 | 500 |
| Agent-oil ratio | 3.2 | 3.2 | 3.2 |
| Weight hourly space velocity, hour -1 | 1.6 | 1.6 | 1.6 |
| Test-results | |||
| Transformation efficiency | 72 | 71 | 73 |
| Product distributes, heavy % | |||
| Reacted gas | 14.34 | 17.01 | 20.19 |
| C wherein 2 ＝ | 0.36 | 0.42 | 0.53 |
| C 3 ＝ | 4.16 | 4.95 | 5.79 |
| C 4 ＝ | 3.43 | 3.98 | 4.25 |
| Gasoline (C 5～216℃) | 50.23 | 49.46 | 47.61 |
| Diesel oil (＞216 ℃) | 27.98 | 29.38 | 27.02 |
| C 2 ＝+C 3 ＝+C 4 ＝ | 7.95 | 9.35 | 10.57 |
| Gasoline octane rating | |||
| RON | 91.5 | 91.7 | 91.9 |
| MON | 81.0 | 81.2 | 81.5 |
Table 5
| Numbering | Embodiment 6 | Embodiment 7 | Comparative Examples 2 |
| Raw material | B | B | B |
| Catalyzer | |||
| CRP-1/CRC, weight ratio | 0.05 | 0.40 | 0 |
| ZRP content (accounting for reserve), heavy % | 0.7 | 4.3 | 0 |
| Reaction conditions | |||
| Temperature, ℃ | 500 | 500 | 500 |
| Agent-oil ratio | 3.2 | 3.2 | 3.2 |
| Weight hourly space velocity, hour -1 | 1.6 | 1.6 | 1.6 |
| Test-results | |||
| Transformation efficiency | 66 | 69 | 71 |
| Product distributes, heavy % | |||
| Reacted gas | 11.62 | 6.16 | 9.76 |
| C wherein 2 ＝ | 0.56 | 0.66 | 0.50 |
| C 3 ＝ | 3.65 | 5.67 | 2.77 |
| C 4 ＝ | 2.89 | 3.91 | 235 |
| Gasoline (C 5～216℃) | 41.65 | 41.43 | 33.23 |
| Diesel oil (＞216 ℃) | 33.72 | 30.78 | 28.85 |
| C 2 ＝+C 3 ＝+C 4 ＝ | 6.78 | 9.98 | 5.33 |
| Gasoline octane rating | |||
| RON | 90.0 | 91.0 | 89.0 |
| MON | 80.0 | 80.5 | 79.0 |
Claims (7)
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN00100398A CN1100117C (en) | 2000-01-21 | 2000-01-21 | Method for increasing liquefied gas yield and gasoline octane number |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN00100398A CN1100117C (en) | 2000-01-21 | 2000-01-21 | Method for increasing liquefied gas yield and gasoline octane number |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1307088A CN1307088A (en) | 2001-08-08 |
| CN1100117C true CN1100117C (en) | 2003-01-29 |
Family
ID=4575432
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN00100398A Expired - Fee Related CN1100117C (en) | 2000-01-21 | 2000-01-21 | Method for increasing liquefied gas yield and gasoline octane number |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN1100117C (en) |
Families Citing this family (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101760228B (en) * | 2008-12-25 | 2013-06-26 | 中国石油化工股份有限公司 | Catalytic conversion method for producing propylene and high-octane gasoline |
| CN101935266B (en) * | 2009-06-30 | 2013-07-31 | 中国石油化工股份有限公司 | Catalytic conversion method for preparing propylene and high-octane value gasoline |
| CN102794195B (en) * | 2012-08-28 | 2014-08-27 | 丁泳 | Catalyst suitable for enhancing gasoline octane number of fuel and lowering olefin content and application thereof |
| CN106701148B (en) * | 2015-07-17 | 2018-05-18 | 中国石油化工股份有限公司 | A kind of catalytic cracking process |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1085885A (en) * | 1992-10-22 | 1994-04-27 | 中国石油化工总公司 | The catalysis conversion method of petroleum hydrocarbon |
| CN1102431A (en) * | 1993-11-05 | 1995-05-10 | 中国石油化工总公司 | Catalytic conversion method of low-carbon olefines high-output |
| CN1160746A (en) * | 1996-03-21 | 1997-10-01 | 中国石油化工总公司 | Catalytic conversion method for improving low-quality gasoline octane number |
-
2000
- 2000-01-21 CN CN00100398A patent/CN1100117C/en not_active Expired - Fee Related
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1085885A (en) * | 1992-10-22 | 1994-04-27 | 中国石油化工总公司 | The catalysis conversion method of petroleum hydrocarbon |
| CN1102431A (en) * | 1993-11-05 | 1995-05-10 | 中国石油化工总公司 | Catalytic conversion method of low-carbon olefines high-output |
| CN1160746A (en) * | 1996-03-21 | 1997-10-01 | 中国石油化工总公司 | Catalytic conversion method for improving low-quality gasoline octane number |
Also Published As
| Publication number | Publication date |
|---|---|
| CN1307088A (en) | 2001-08-08 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN1031646C (en) | Method for Catalytic Conversion of Petroleum Hydrocarbons | |
| JP2935275B2 (en) | Production of light olefins by catalytic conversion of hydrocarbons | |
| US5601699A (en) | Method for cracking hydrocarbons | |
| KR101509826B1 (en) | Catalytic cracking catalyst composition having improved bottom conversion | |
| CN107974286A (en) | It is a kind of to produce low-carbon alkene and the catalytic cracking method of light aromatic hydrocarbons | |
| CN108659883B (en) | Method and system for gasoline desulfurization and aromatization | |
| JP3699782B2 (en) | Method for catalytic cracking of hydrocarbon-containing oil feedstock in the presence of catalyst | |
| CN1872957A (en) | Method for catalytic cracking petroleum hydrocarbons | |
| CN1100117C (en) | Method for increasing liquefied gas yield and gasoline octane number | |
| CN107971012A (en) | It is a kind of to produce low-carbon alkene and the catalytic cracking method of light aromatic hydrocarbons | |
| CN1076752C (en) | Catalytic conversion method for preparing propylene, isobutane and isoalkane-enriched gasoline | |
| CN102031147B (en) | Catalytic conversion method for producing diesel and propylene in high yield | |
| TW202200266A (en) | Catalytic cracking auxiliary, preparation method and application thereof capable of significantly improving C4 olefin yield and C4 olefin concentration in a liquefied gas | |
| CN101993328B (en) | Catalytic conversion combination method for producing propylene and high-quality fuel oil in high yield | |
| CN102031138B (en) | Catalytic conversion method for productive diesel and propylene | |
| CN101134916B (en) | Catalytic hydroprocessing adsorping desulfurization for hydrocarbon oil in fluidized reactor | |
| CN102051227B (en) | Catalytic conversion method for producing diesel and propylene in high yield | |
| CN103059992B (en) | Effective catalytic conversion method of petroleum hydrocarbon | |
| CN101935266A (en) | A catalytic conversion method for producing propylene and high-octane gasoline | |
| CN107974281A (en) | It is a kind of to produce low-carbon alkene and the catalytic cracking method of light aromatic hydrocarbons | |
| JP2018158282A (en) | Activation method of catalyst for fluidized catalytic cracking | |
| CN119909726B (en) | Catalytic composition for improving propylene concentration under high light liquid yield, preparation method thereof, catalyst and hydrocarbon oil catalytic conversion method | |
| CN1286952C (en) | Method for decreasing sulfur content of hydrocarbon | |
| CN102051226B (en) | Catalytic conversion method for diesel oil and propylene with high yield | |
| CN100351344C (en) | Catalytic conversion method for selective preparation of micromolecular olefin |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C06 | Publication | ||
| PB01 | Publication | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20030129 Termination date: 20180121 |
|
| CF01 | Termination of patent right due to non-payment of annual fee |