WO1995032167A1 - Alkylation d'hydrocarbures aromatiques et lit fluidise a circulation liquide/solide pour l'alkylation - Google Patents
Alkylation d'hydrocarbures aromatiques et lit fluidise a circulation liquide/solide pour l'alkylation Download PDFInfo
- Publication number
- WO1995032167A1 WO1995032167A1 PCT/CN1995/000040 CN9500040W WO9532167A1 WO 1995032167 A1 WO1995032167 A1 WO 1995032167A1 CN 9500040 W CN9500040 W CN 9500040W WO 9532167 A1 WO9532167 A1 WO 9532167A1
- Authority
- WO
- WIPO (PCT)
- Prior art keywords
- liquid
- solid
- catalyst
- reactor
- regenerator
- Prior art date
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Classifications
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C2/00—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms
- C07C2/54—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms by addition of unsaturated hydrocarbons to saturated hydrocarbons or to hydrocarbons containing a six-membered aromatic ring with no unsaturation outside the aromatic ring
- C07C2/64—Addition to a carbon atom of a six-membered aromatic ring
- C07C2/66—Catalytic processes
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/005—Separating solid material from the gas/liquid stream
- B01J8/0055—Separating solid material from the gas/liquid stream using cyclones
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
- B01J8/1845—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles with particles moving upwards while fluidised
- B01J8/1863—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles with particles moving upwards while fluidised followed by a downward movement outside the reactor and subsequently re-entering it
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
- B01J8/1881—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles with particles moving downwards while fluidised
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
- B01J8/24—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique
- B01J8/26—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique with two or more fluidised beds, e.g. reactor and regeneration installations
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/584—Recycling of catalysts
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
- Y10S—TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y10S585/00—Chemistry of hydrocarbon compounds
- Y10S585/919—Apparatus considerations
- Y10S585/921—Apparatus considerations using recited apparatus structure
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
- Y10S—TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y10S585/00—Chemistry of hydrocarbon compounds
- Y10S585/919—Apparatus considerations
- Y10S585/921—Apparatus considerations using recited apparatus structure
- Y10S585/924—Reactor shape or disposition
- Y10S585/925—Dimension or proportion
Definitions
- the invention relates to an alkylation process and a liquid-solid circulating fluidized bed used in the process, and more particularly, to an alkylation process of an aromatic hydrocarbon or a derivative thereof using a solid acid as a catalyst and the process Liquid-solid circulating fluidized bed continuous reaction-regeneration equipment used in
- Alkylation is one of the important reactions in the petrochemical industry.
- the product of alkylation reaction between benzene and propylene is the raw material for making phenol and acetone; isobutane and low-carbon hydrocarbons are alkylated.
- a blended gasoline component with a high octane number can be obtained; a surfactant can be prepared by performing alkylation reaction with ten to octadecene.
- the alkylation catalysts that were successfully developed in the early stage are liquid strongly acidic catalysts, such as hydrofluoric acid, aluminum chloride, zinc chloride, etc., because of the industrial use of such catalysts, the catalyst in the product has been separated, and the waste acid has been removed.
- a series of problems such as treatment, equipment corrosion, and the harmfulness of highly toxic substances to the human body, so people have turned to consider using solid acids instead of liquid acids as alkylation catalysts.
- the solid acidating agents involved in the alkylation process are: HX, HY, ZSM-5, USY and REHY zeolite molecular sieves, halogen-containing cation exchange resins, halogen-containing solid superacids, SOVM O-type solid superacids, SO / composite oxide type solid super strong acid, etc.
- the problems associated with the use of such solid acid catalysts are: during the alkylation reaction, due to the polymerization of olefins, coke deposition on the surface of the catalyst particles inevitably occurs, which in turn leads to a decrease in catalyst activity, especially for higher activity catalysts.
- the catalyst is more susceptible to a sharp decrease in activity during use.
- the solid acid catalyst can only operate with low activity under the condition of surface area carbon.
- people try to use something like Introducing methods such as Group VI elements and rare earth elements into the catalyst to suppress carbon deposition and prolong the life of the catalyst, but the effect is not obvious.
- the reaction-regeneration process whether performed in a fixed-bed reactor or a kettle reactor, is actually performed in a batch-type condition, and the reaction cycle depends on the deactivation rate of the catalyst.
- the reaction cycle depends on the deactivation rate of the catalyst.
- deactivating catalysts frequent alternating switching Obviously there are the following disadvantages: complicated operation; large equipment investment; unnecessary loss of raw material and regeneration liquid when switching; low production efficiency of intermittent operation; the most prominent disadvantage is that the entire reaction is in the activity of the catalyst In the state of gradual reduction, even in the state of low living for 4 lives.
- An object of the present invention is to provide an alkylation process of an aromatic hydrocarbon or a derivative thereof using a solid catalyst to realize a continuous reaction-regeneration process.
- Another object of the present invention is to provide a liquid-solid circulating fluidized bed apparatus capable of ensuring that the alkylation process is continuously performed with high conversion in the presence of a solid acid catalyst.
- FIG. 1 is a schematic diagram of a reaction-regeneration continuous alkylation process and a liquid-solid circulating fluidized bed used in the present invention.
- Figure 2 is a schematic diagram of the structure of a combined distributor arranged in a reactor and a regenerator.
- Figure 3 is a schematic diagram of the internal structure of the sedimentation backwashing tower.
- Fig. 4 is a test result of the catalyst activity coefficient in the liquid-solid circulating fluidized bed reactor provided by the present invention and the continuous stirred tank reactor of the existing branch technique.
- the reactant is brought into contact with a solid acid catalyst in a liquid-solid co-current up-flow reactor [1], and then the liquid is passed through a cyclone liquid-solid separator [2].
- Solid phase separation The separated catalyst to be recovered enters the liquid-solid co-current up-flow regenerator through the sedimentation backwashing tower [3], and then comes into contact with the regeneration liquid which is the same substance as the reactant arene or its derivative, and then swirls.
- the liquid-solid separator [5] separates the liquid-solid phase, and the separated catalyst is returned to the reactor [1] through the sedimentation backwash column [6], thereby completing the continuous reaction-regeneration process.
- the invention provides continuous reaction-regeneration in the presence of a solid acid catalyst.
- the structure of the liquid-solid circulating fluidized bed equipment is shown in Figure 1.
- the lower end of the reactor [1] communicates with the lower end of the settling backwash column [6];
- the liquid-solid co-current upward flow regenerator [4] which is arranged in parallel with the reactor and has a double feed port [11, 12] at the lower end
- the upper end of] is in communication with the cyclone liquid-solid separator [5], and the lower end of the regenerator [4] is in communication with the lower end of the sedimentation backwashing tower [3];
- the liquid-solid separator [2] is in communication with the reactor [1];
- the sedimentation backwashing tower [6] is in communication with the regenerator [4] through a cycl
- liquid-solid co-current up-flow reactor / regenerator refers to a vertically installed reactor / regenerator in which the reaction liquid / regeneration liquid and catalyst particles flow upward and come into contact simultaneously.
- opening ratio refers to the ratio of the total open area on the baffle or combined distributor of the settling backwash tower to the total area of the baffle / sieve plate, expressed as a percentage.
- void ratio refers to the ratio of the volume of liquid to the total volume of liquid and solids in a liquid-solid co-current up-flow reactor / regenerator.
- the continuous reaction-regeneration process is completed as shown in FIG. 1.
- the reactants mixed according to the reaction ratio are divided into two paths from the primary inlet [7] and the secondary inlet [7].
- 8] Pumped by a metering pump, the material stream entering from the primary inlet keeps the catalyst particles in a circulating bed state, and the material stream entering from the secondary inlet is used to change the resistance at the catalyst inlet to adjust the circulation of the catalyst.
- the material enters the liquid-solid co-current up-flow reactor [1] via the combined distributor [9], with a diameter of 0.05 to 0.8 in the reactor 68 ⁇ 0.
- the catalyst and liquid velocity of the catalyst to be produced is 0.5 to 5 times the terminal sedimentation rate of the catalyst particles, since
- the bottom-up flowing backwash liquid which is the same substance as the reactant aromatic hydrocarbon or its derivative, is contacted to wash off the adsorbed material on the surface of the catalyst to be prepared.
- the catalyst to be prepared enters the solid-liquid and flows up to the regenerator [4].
- the regeneration liquid which is the same substance as the reactant aromatic hydrocarbon or its derivative, is divided into two paths by the primary inlet [11] and the secondary inlet [12], which are pumped by the metering pump.
- the alkylation process of the aromatic hydrocarbon or its derivative provided by the present invention realizes a continuous reaction-regeneration solid acid-catalyzed alkylation process. Since the reaction-regeneration is performed in a circulating flow state, the catalyst is always guaranteed to be highly active. Down operation. This process is suitable for different alkylating agents, such as alkylating agents with five to twenty carbon atoms in the linear part, and it is also suitable for various types of solid acid catalysts.
- the reactants and the regeneration solution are divided into two paths into the device. Therefore, the total amount of materials in the reactor and the regenerator and the content of the catalyst can be controlled by adjusting the feed ratios of the two paths, thereby controlling the reaction. Conversion rate and regeneration efficiency of the catalyst to be produced.
- the backwashing liquid, regeneration liquid and washing liquid are all made of the same substance as the reactant arene or its derivative, which not only reduces the separation steps in the subsequent process, simplifies the process, but also avoids regeneration beyond the reactants. Contamination of the reaction system by liquids, etc.
- the process of the present invention can also be used in other similar heterogeneous catalytic reaction systems.
- the continuous reaction-regeneration process can be achieved, such as isoparaffin Reaction system of alkylation reaction with low-carbon olefins to generate high-octane gasoline blending components, the reaction is at o ⁇ ioo ° c, ⁇ ⁇
- the liquid-solid circulating fluidized bed equipment for performing reaction-regeneration in the presence of a solid acid catalyst according to the present invention includes six main parts: a liquid-solid co-current up-flow reactor [1], Flow type liquid-solid separator [2], ready-to-growth catalyst settling backwash column [3], liquid-solid co-current upflow regenerator [4], cyclone type liquid-solid separator [5], catalyst settling backwash column after regeneration [6].
- the upper end of the reactor [1] is in communication with the cyclone liquid-solid separator [2].
- the lower end of [1] is in communication with the lower end of the sedimentation backwashing tower [6]; the upper end of the regenerator [4] is in communication with the cyclone liquid-solid separator [5], and the lower end of the regenerator [4] is connected to the sedimentation backwashing tower [3] ]
- the lower end is connected; the sedimentation backwashing tower [3] is connected to the reactor through a cyclone liquid-solid separator [ 2 ] provided at the top of the tower
- the settling backwashing tower [6] communicates with the regenerator [4] through a cyclone liquid-solid separator [5] set on its top.
- the bottom of the reactor [1] and the regenerator [4] are respectively provided with two material inlets [7] and [8], [11] and [12] and a combined distributor [9], which is composed of tubes Type distributor [14] and porous sieve plate distributor [15], the structure of which is shown in Figure 2, the opening ratio of this distributor is 2 ⁇ : L5%, the opening ratio of porous sieve plate is 0 5 ⁇ 5%, the materials entering from the two inlets enter the reactor or regenerator through the tubes and between the tubes of the combined distributor, respectively.
- settling backwashing towers [3] and [6] there are combined internal components [16] provided to enhance liquid-solid contact.
- FIG. ⁇ ⁇ ⁇ 90 ⁇ To each other into 90. It can be combined at the corners, and other types of baffle plates other than corrugated baffle plates, such as flat plate and ridge baffle plates, can be used. There are holes of a certain size at the crests and troughs of the corrugated baffle for the flow of liquids and solids. .
- a liquid material inlet [18] is provided at the lower part of the settling backwashing tower [3] and [6] for the backwashing liquid and washing liquid to enter the tower.
- a control valve [19] is provided at the junction of the bottom of the settling backwash column and the reactor or regenerator.
- the liquid-solid circulating fluidized bed equipment realizes a continuous reaction-regeneration process of solid acid-catalyzed alkylation, and ensures that the catalyst always runs under high activity.
- the flow in the reactor is approximately flat flow, the conversion is high, the temperature of the reaction system is uniform and easy to control.
- the lower end of the reactor and the regenerator are provided with double inlets, the conversion rate of the reaction and the regeneration efficiency of the catalyst to be produced can be controlled by adjusting the respective flows of the two inlets.
- a cyclonic liquid-solid separator is selected in this equipment. The centrifugal effect provided by the inherent structure of the separator, coupled with the tangential entry of the material, makes the liquid-solid phase separation at high speed o
- the combined internal components are set in the settling backwashing tower, especially the corrugated baffle is used to make the backwashing liquid and washing liquid in the tower fully contact with the catalyst solid particles, which enhances the washing effect.
- the catalyst provides a surface that is as clean as possible.
- This example shows that the process of the present invention can maintain high conversion of reactants during long-term continuous operation.
- dodecene and benzyl undergo an alkylation reaction according to the process shown in FIG. 1.
- the inner diameter of the reactor and the regenerator are the same, the aspect ratio is 10: 1, the reaction temperature is 110 ⁇ 120 e C, the regeneration temperature is 135 ⁇ 145 ° C, and the pressure of the reactor and the regenerator is 4. 5 ⁇ 6. 0 9% ⁇
- the reactant and the liquid velocity of the regeneration liquid is 10 liters / hour, continuous operation for 200 hours, the export rate of dodecene has always remained 99.9% unchanged.
- Table 1 lists the product distribution (% by weight) of alkylbenzyl products obtained by this process and hydrofluoric acid as catalysts. According to the data in the table, it can be known that there are higher 2-substitutions in the products obtained by the process of the present invention. And 3-Substitute content. The increase of the content of 2-substituents will increase the biodegradability of the final washed product; the increase of the content of 2-substituents will increase the detergency of the final washed product, that is, obtained by alkylation using the process of the present invention The product distribution is unique.
- the catalyst's activity coefficient can have a very high value in the initial instant in the kettle reactor, the tendency of its rapid decline is extremely obvious; in contrast, in a liquid-solid circulating fluidized bed reactor Although the initial activity coefficient of the catalyst was only about 0.8, this value remained high and remained stable for a long time.
Description
Claims
Priority Applications (3)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
JP7529966A JPH10508825A (ja) | 1994-05-24 | 1995-05-18 | 芳香族化合物の連続アルキル化プロセスおよび該プロセスのための液−固循環流動床システム |
EP95918505A EP0765849B1 (en) | 1994-05-24 | 1995-05-18 | Aromatic hydrocarbons alkylation and liquid-solid circulating fluidized bed for alkylation |
US08/569,234 US5789640A (en) | 1994-05-24 | 1995-05-18 | Aromatic hydrocarbons alkylation and liquid-solid circulating fluidized bed for alkylation |
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
CN94105710A CN1043036C (zh) | 1994-05-24 | 1994-05-24 | 芳烃烷基化方法及其所用液固循环流化床设备 |
CN94105710.0 | 1994-05-24 |
Publications (1)
Publication Number | Publication Date |
---|---|
WO1995032167A1 true WO1995032167A1 (fr) | 1995-11-30 |
Family
ID=5032158
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
PCT/CN1995/000040 WO1995032167A1 (fr) | 1994-05-24 | 1995-05-18 | Alkylation d'hydrocarbures aromatiques et lit fluidise a circulation liquide/solide pour l'alkylation |
Country Status (5)
Country | Link |
---|---|
US (1) | US5789640A (zh) |
EP (1) | EP0765849B1 (zh) |
JP (1) | JPH10508825A (zh) |
CN (1) | CN1043036C (zh) |
WO (1) | WO1995032167A1 (zh) |
Families Citing this family (18)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JP3617183B2 (ja) * | 1996-05-08 | 2005-02-02 | トヨタ自動車株式会社 | 電気自動車の電源装置 |
US6642426B1 (en) * | 1998-10-05 | 2003-11-04 | David L. Johnson | Fluid-bed aromatics alkylation with staged injection of alkylating agents |
US6716344B1 (en) * | 2000-10-02 | 2004-04-06 | The University Of Western Ontario | Liquid-solids circulating fluidized bed |
US6399843B1 (en) | 2000-10-12 | 2002-06-04 | Uop Llc | Upflow oligomerization reaction process |
FI119432B (fi) * | 2000-12-19 | 2008-11-14 | Neste Oil Oyj | Menetelmä olefiinien konvertoimiseksi |
FR2886936B1 (fr) * | 2005-06-09 | 2007-08-03 | Inst Francais Du Petrole | Procede de production de phenylalcanes fonctionnant en lit mobile |
US20070264190A1 (en) * | 2006-05-09 | 2007-11-15 | Qinglin Zhang | Fixed-bed reactors and catalytic processes |
JP5604101B2 (ja) * | 2006-05-24 | 2014-10-08 | エクソンモービル・ケミカル・パテンツ・インク | モノアルキル化された芳香族化合物の製造 |
US20110110849A1 (en) * | 2008-04-29 | 2011-05-12 | Roland Siemons | Method of converting a raw material stream into a product stream using a fluidized bed and apparatus for use in said method |
FR2937634B1 (fr) * | 2008-10-27 | 2011-09-30 | Commissariat Energie Atomique | Procede de decontamination d'un effluent liquide comprenant un ou plusieurs elements chimiques radioactifs par traitement en lit fluidise |
US8747783B2 (en) * | 2009-06-24 | 2014-06-10 | Uop Llc | Acid alkylation system and process for controlling temperature in a settler |
US8124034B2 (en) * | 2009-06-24 | 2012-02-28 | Uop Llc | Alkylation unit and method of modifying |
JP5934339B2 (ja) † | 2011-04-15 | 2016-06-15 | ラディチ キミカ ソシエタ ペル アチオニ | ヘキサメチレンジアミンを製造するための改良された方法 |
FR2977809B1 (fr) * | 2011-07-12 | 2016-01-08 | Arkema France | Regeneration de catalyseur en continu dans un reacteur a lit fluidise |
CN105457566B (zh) * | 2014-09-05 | 2018-03-20 | 中国石油化工股份有限公司 | 一种流化床反应与再生装置及固体酸烷基化方法 |
CN105441116B (zh) * | 2014-09-05 | 2017-11-28 | 中国石油化工股份有限公司 | 一种固体酸烷基化反应方法 |
CN107974277B (zh) * | 2016-10-25 | 2020-03-24 | 中国石油化工股份有限公司 | 一种固体酸烷基化的设备和方法 |
EP3871763A4 (en) | 2018-10-22 | 2022-08-17 | China Petroleum & Chemical Corporation | AXIAL LIQUID-SOLID MOVING BED REACTION AND REGENERATION DEVICE AND PROCESS FOR ALKYLATION OF SOLIDS |
Citations (2)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US4992607A (en) * | 1989-03-20 | 1991-02-12 | Mobil Oil Corporation | Petroleum refinery process and apparatus for the production of alkyl aromatic hydrocarbons from fuel gas and catalytic reformate |
US5196172A (en) * | 1989-05-16 | 1993-03-23 | Engelhard Corporation | Apparatus for the fluid catalytic cracking of hydrocarbon feed employing a separable mixture of catalyst and sorbent particles |
Family Cites Families (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US5012021A (en) * | 1988-12-29 | 1991-04-30 | Uop | Process for the production of alkylaromatic hydrocarbons using solid catalysts |
US5489732A (en) * | 1994-10-14 | 1996-02-06 | Uop | Fluidized solid bed motor fuel alkylation process |
US5565090A (en) * | 1994-11-25 | 1996-10-15 | Uop | Modified riser-reactor reforming process |
-
1994
- 1994-05-24 CN CN94105710A patent/CN1043036C/zh not_active Expired - Fee Related
-
1995
- 1995-05-18 WO PCT/CN1995/000040 patent/WO1995032167A1/zh active IP Right Grant
- 1995-05-18 US US08/569,234 patent/US5789640A/en not_active Expired - Fee Related
- 1995-05-18 EP EP95918505A patent/EP0765849B1/en not_active Expired - Lifetime
- 1995-05-18 JP JP7529966A patent/JPH10508825A/ja active Pending
Patent Citations (2)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US4992607A (en) * | 1989-03-20 | 1991-02-12 | Mobil Oil Corporation | Petroleum refinery process and apparatus for the production of alkyl aromatic hydrocarbons from fuel gas and catalytic reformate |
US5196172A (en) * | 1989-05-16 | 1993-03-23 | Engelhard Corporation | Apparatus for the fluid catalytic cracking of hydrocarbon feed employing a separable mixture of catalyst and sorbent particles |
Non-Patent Citations (1)
Title |
---|
See also references of EP0765849A4 * |
Also Published As
Publication number | Publication date |
---|---|
EP0765849A1 (en) | 1997-04-02 |
US5789640A (en) | 1998-08-04 |
EP0765849B1 (en) | 1999-11-17 |
JPH10508825A (ja) | 1998-09-02 |
EP0765849A4 (en) | 1997-03-18 |
CN1043036C (zh) | 1999-04-21 |
CN1113906A (zh) | 1995-12-27 |
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