CN1212669A - Aluminium promoted hydrogenation of alkylation sludge for aluminium chloride recovery - Google Patents
Aluminium promoted hydrogenation of alkylation sludge for aluminium chloride recovery Download PDFInfo
- Publication number
- CN1212669A CN1212669A CN97192747.2A CN97192747A CN1212669A CN 1212669 A CN1212669 A CN 1212669A CN 97192747 A CN97192747 A CN 97192747A CN 1212669 A CN1212669 A CN 1212669A
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- China
- Prior art keywords
- aluminum chloride
- aluminium
- trimethylmethane
- catalyzer
- sludge
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01F—COMPOUNDS OF THE METALS BERYLLIUM, MAGNESIUM, ALUMINIUM, CALCIUM, STRONTIUM, BARIUM, RADIUM, THORIUM, OR OF THE RARE-EARTH METALS
- C01F7/00—Compounds of aluminium
- C01F7/48—Halides, with or without other cations besides aluminium
- C01F7/56—Chlorides
-
- 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
- C07C2/56—Addition to acyclic hydrocarbons
- C07C2/58—Catalytic processes
- C07C2/60—Catalytic processes with halides
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C2527/00—Catalysts comprising the elements or compounds of halogens, sulfur, selenium, tellurium, phosphorus or nitrogen; Catalysts comprising carbon compounds
- C07C2527/06—Halogens; Compounds thereof
- C07C2527/125—Compounds comprising a halogen and scandium, yttrium, aluminium, gallium, indium or thallium
- C07C2527/126—Aluminium chloride
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- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Life Sciences & Earth Sciences (AREA)
- Geology (AREA)
- Inorganic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Catalysts (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Low-Molecular Organic Synthesis Reactions Using Catalysts (AREA)
Abstract
The recovery of aluminum chloride from deactivated alkylation catalyst complexes by hydrogenation using hydrogen gas (22) and an aluminum catalyst is disclosed. Using aluminum to catalyze the hydrogenation allows the reaction to proceed at a lower temperature and pressure while reducing the amount of hydrogen chloride present in the reactor (8) thus reducing the corrosiveness and cost of the aluminum chloride recovery. Methods for batch, batchwise-continuous, and continuous aluminum chloride recovery are disclosed.
Description
Background technology
1. invention field
The present invention relates to a kind of intermittence, semicontinuous and continuation method that from inactivation alkylation catalyst mixture, reclaims aluminum chloride by the low corrosion hydrogenation that uses Al catalysts.Specifically, the present invention relates under the condition that has hydrogen to exist, use the hydrogenation of aluminium powder catalyzer to the compound sludge of aluminum chloride and olefin(e) compound; Aluminium powder also as reaction reagent from reaction mixture, to remove hydrochloric acid to reduce the cost of corrodibility and hydrogenation step.
2. the description of prior art
In the prior art, using the homogeneous phase mixture catalysis hydrocarbon conversion reactions based on aluminum chloride, is known as alkylated reaction and isomerization reaction.Use solubility aluminum alkyls muriate to use sulfuric acid to compare with routine with the alkylating method of hydrochloric acid as the alkylation of the Catalyst Production gasoline on basis, more effective on cost, to more favourable on the environment, for example, the U.S. Patent application 08/093 of Sherman, disclosed Catalyst And Method here is incorporated herein by reference in 463.In this method, when alkylated reaction when finishing, homogeneous catalyst is degraded to not too active state, forms isolating sludge phase.Purpose of the present invention is exactly to reclaim aluminum chloride with the cyclic production soluble catalyst from this sludge.
Can reclaim aluminum chloride by under high temperature (200 ℃) and high pressure (3000psig), sludge being carried out hydrogenation, but, the aluminum chloride that produces in hydrogenation process and the combination of hydrochloric acid at high temperature have severe corrosive to carbon steel reactor, make hydrogenation step expensive especially.Erosion rate can reduce by the amount that reduces temperature of reaction and pressure or the existence of minimizing hydrochloric acid.Though can use these two kinds of known hydrogenation catalysts of rhodium and palladium to reduce temperature of reaction and pressure,, these catalyzer are expensive.Have now found that, under the condition that has hydrogen to exist, metallic aluminium (more cheap reagent) is effective hydrogenation catalyst for the aluminum alkyls muriate of these homogeneous, high binding (bound) hydrocarbon content for basic catalyzer, with compare without catalyzer, can promote to discharge aluminum chloride and paraffinic by product down at lower temperature (150 ℃) and pressure (1500psig).Metallic aluminium also purified use in the alkylation process or hydrogenation process in the excessive hydrochloric acid that produces, therefore, greatly reduce the corrosion of reactor.
Prior art comprises the multiple method that reclaims spent catalyst from alkylation process, still, does not have a kind of aluminium that is to use to come the hydrogenation of catalysis based on the catalyzer of aluminum alkyls muriate.For example, US2,517,692 disclose use hydrochloric acid and alkene and the aluminium aluminum halide catalyst as reaction reagent regeneration of deactivated from sludge.Do not implement hydrogenation, consumed aluminium, aluminium and hydrochloric acid reaction have produced more aluminum chloride.With respect to the present invention, this method is non-catalytic, only is to have produced aluminum chloride.Similarly, US3,846,334 relate to and use aluminium and hydrochloric acid and benzene, rather than hydrogen regeneration sludge to be producing " reactivate mixture ", and aluminum chloride not.The present invention uses hydrogen rather than the aromatic hydrocarbons reagent aluminum chloride of regenerating.In addition, US3,476,825 disclose the use aluminium powder and hydrochloric acid produces aluminum chloride on the spot, are not from the sludge regenerated catalyst.In an independent step, hydrogen is used for regenerated catalyst, but does not have aluminium.
Use other examples of aluminium to comprise US4,017,584, aluminium with the hydrogenchloride pre-treatment with under being no more than 100 ℃ temperature from the sludge mixture disproportionation aluminum chloride.Different with the present invention who carries out shortening, do not use hydrogen.Aluminium consumes by stoichiometric quantity in reaction.For from sludge, discharging per 3 moles of aluminum chloride, just there is 1 moles, of aluminum per mole of titanium metal to be converted into aluminum chloride.In the present invention, aluminium plays katalysis in hydrogenation step, only owing to system in the reaction of any clean excessive hydrochloric acid be consumed, hydrogenchloride is owing to exist the alkylation catalyst composite activating agent more than stoichiometric quantity to cause that these activators also are released in hydrogenation process.When being used for high hydrocarbon (hydrocarbon of about 46% weight) with based on the muriatic catalyzer of aluminum alkyls the time, patent 584 disclosed methods do not produce aluminum chloride, this focus of the present invention just.US1,582,131 disclose a kind of on-catalytic hydrogenation of aluminum chloride catalyst residue and have passed through the method that aluminum chloride is reclaimed in distillation.US2,211,207 disclose a kind of method of hydrotreating in the presence of heavy metal halide, wherein do not point out with aluminium as catalyzer to reclaim aluminum chloride.
Do not point out in the above-mentioned patent to use aluminium powder as catalyzer to reclaim aluminum chloride, this is the application's problem just.
Summary of the invention
According to the present invention, from discontinuous method based on recovery aluminum chloride the catalyzer sludge of aluminum alkyls muriate, comprise: under the condition that hydrogen exists, under 1500psig or lower pressure and 200 ℃ or lower temperature, described sludge was mixed about 4 hours or the shorter time with metallic aluminium.The present invention also comprises from the semicontinuous and continuation method based on recovery aluminum chloride the catalyzer sludge of aluminum alkyls muriate, comprise: under 1500psig or lower pressure and 200 ℃ or lower temperature, described sludge is mixed in hydrogenation zone with metallic aluminium, Trimethylmethane and hydrogen.
The accompanying drawing summary
Fig. 1 is the synoptic diagram of one embodiment of the invention.
Detailed description of the preferred embodiments
Fig. 1 is the schematic diagram of the semicontinuous and continuation method of recovery aluminium chloride of the present invention, is used for the olefin alkylation process of fuel. Usually, the method comprises: an alkylation 10, alkylate, iso-butane and sludge compound from alkylation process 12 enter defecator 14 by the road from this unit, it is adapted to pass through pipeline 16 and discharges alkylates and iso-butane further to process in the process outside the scope of the invention, and make sludge by the road 20 enter hydrogenation unit 18 with hydrogen reaction, hydrogen and iso-butane 22 enter hydrogenation unit by the road, catalyst aluminium is present in hydrogenation unit 18, replenishes at set intervals on demand. Carrying out with hydrogenation reaction, aluminium chloride discharges from the sludge compound, described aluminium chloride is dissolved in the described iso-butane, 26 leave hydrogenation unit and enter separative element 24 by the road, wherein, hydrogen 28 is discharged by the road, deliver to outside the scope of the invention and be for further processing, the iso-butane logistics that contains aluminium chloride 30 is returned alkylation 10 by the road, the iso-butane that replenishes by the road 32, the alkylation catalyst activator 34 also joins in the alkyl unit by the road, they before entering alkylation with described aluminium chloride be compounded to form binding hydrocarbon homogeneous phase, high take the catalyst of alkyl aluminum chloride as the basis, be used for alkylation process with the alkene of introducing alkylation from pipeline 36.
The present invention relates to use intermittence, the semicontinuous and continuation method based on the catalyzer sludge of aluminum alkyls muriate recovery aluminum chloride of the catalytic hydrogenation reaction of aluminium from homogeneous, high binding hydrocarbon.The alkylation catalyst that the present invention relates to is formed by catalyst precursor aluminum chloride and the reaction of a kind of paraffinic hydrocarbons.Add promotor then.Advantageously, paraffinic hydrocarbons is a Trimethylmethane, and promotor is a 1-chlorobutane, also can work in native system although contain any light paraffins of tertiary carbon atom.In the prior art, with respect to " binding aluminum chloride " level (the binding aluminum chloride of about 84% weight of about 64%-), alkylation catalyst based on aluminum chloride trends towards having low " binding hydrocarbon " level (the binding hydrocarbon of about 36% weight of about 16%-), and the catalyzer that forms catalyzer sludge mixture of the present invention has high relatively " binding hydrocarbon " level (the binding hydrocarbon of about 70% weight of about 43%-is generally the binding hydrocarbon of about 50% weight).Can believe that the difference on this composition is US4,017,584 disclosed catalyst recovery method is separating the invalid major cause of aluminum chloride from this sludge mixture.
According to U.S. Patent application No.08/093,463, even under low acid concentration, the catalyzer based on the aluminum alkyls muriate of wherein disclosed homogeneous, high binding hydrocarbon content is effective, can produce the dominant hydrocarbon of high-octane rating isoparaffin with Trimethylmethane with 2-butylene with as other olefin alkylation of propylene, 1-butylene and 2-amylene.Aging with catalyzer, it become be insoluble to paraffinic hydrocarbons-as Trimethylmethane or representational alkylate-the sludge mixture.Then, when making it in settling tank transfixion, can precipitate, may separate because of gravity, then, be sent to hydrogenation unit of the present invention and be used for processing of the present invention with the hydrocarbon phase of alkylation process.Preferably, hydrogenation unit is an intermittence, semicontinuous or successive stirring reactor.By stirring or inducing turbulence to cause stirring, help the contact between catalyzer, hydrogen and the sludge mixture, and from catalyzer, spread out of heat to avoid " focus " and runaway reaction.Stirring in semicontinuous and successive processes can promote by introduce Trimethylmethane/hydrogen stream in hydrogenation unit.
Al catalysts in the hydrogenation process should be purer relatively, and preferred purity is 99%, and to avoid producing other metal chloride, these metal chlorides can be incorporated in the alkylation system with the round-robin aluminum chloride catalyst.The form of catalyzer should make the catalyzer of unit weight have maximum surface area.In stirred reactor, the aluminium of effective form comprises powder and netted, preferred powder.
In intermittent process, the present invention advantageously comprises following steps:
A. with about 6: ratio mixed sludge mixture and aluminium that 1-is about 7: 1;
B. carry out under the condition that the described hydrogen that is blended in the about 1500psig of 500psig-that has an appointment exists;
C. under about 125 ℃-Yue 200 ℃ temperature, carry out;
D. about 4 hours of about 2-;
E. make the reactant cooling then with precipitation aluminum chloride.
Preferably, the ratio of sludge mixture-Al catalysts is about 6: 1 in step (a).Preferred Al catalysts is a powder type.Advantageously, the hydrogen pressure in the step (b) is the about 1500psig of about 1000psig-.Hydrogen pressure in the preferred steps (b) is about 1500psig.Hydrogen is input reactor continuously, also can manually keep hydrogen pressure and keep not having hydrogen effusion reactor.Advantageously, the temperature of reaction in the step (c) is about 140 ℃-Yue 180 ℃.Temperature of reaction in the preferred steps (c) is about 150 ℃.The reaction times of preferred steps (d) is about 3 hours.
In semicontinuous method, the present invention advantageously comprises following steps:
A. alkylate, Trimethylmethane and sludge mixture are sent to the settling tank from alkylation zone, the sludge mixture is precipitated out from alkylate;
B. sludge regularly is sent to hydrogenation zone from settling tank;
The sludge mixture is contacted with catalyzer aluminium under the condition that the hydrogen of the about 1500psig of 500psig-that has an appointment and Trimethylmethane exist;
D. under about 125 ℃-Yue 200 ℃ temperature, carry out;
E. about 4 hours of about 2-;
Thereby f. form aluminum chloride;
G. with the aluminum chloride continuous-dissolution in described Trimethylmethane; And
H. discharge aluminum chloride-Trimethylmethane solution from hydrogenation zone, and be recycled to alkylation zone.
Preferably, Al catalysts is powder or screen cloth form.Advantageously, the hydrogen pressure in the step (c) is the about 1500psig of about 1000psig-.Hydrogen pressure in the preferred steps (c) is about 1500psig.Advantageously, the temperature of reaction in the step (d) is about 140 ℃-Yue 180 ℃.Temperature of reaction in the preferred steps (d) is about 150 ℃.The reaction times of preferred steps (e) is about 3 hours.The stirring of preferred reaction provides by stirring Trimethylmethane, sludge mixture and catalyzer aluminium in hydrogenation zone.
In continuation method, the present invention advantageously comprises following steps:
A. alkylate, Trimethylmethane and sludge mixture are sent to the settling tank from alkylation zone, the sludge mixture is precipitated out from alkylate;
B. continuously the sludge mixture is sent to hydrogenation zone from settling tank;
The sludge mixture is contacted with catalyzer aluminium under the condition that the hydrogen of the about 1500psig of 500psig-that has an appointment and Trimethylmethane exist;
D. under about 125 ℃-Yue 200 ℃ temperature, carry out;
Thereby e. form aluminum chloride;
F. with the aluminum chloride continuous-dissolution in described Trimethylmethane; And
G. discharge aluminum chloride-Trimethylmethane solution from hydrogenation zone, and be recycled to alkylation zone.
Preferred Al catalysts is powder or screen cloth form.Advantageously, the hydrogen pressure in the step (b) is the about 1500psig of about 1000psig-.Hydrogen pressure in the preferred steps (b) is about 1500psig.Advantageously, the temperature of reaction in the step (c) is about 140 ℃-Yue 180 ℃.Temperature of reaction in the preferred steps (c) is about 150 ℃.The stirring of preferred reaction provides by stirring Trimethylmethane, sludge mixture and catalyzer aluminium in hydrogenation zone.
The hydrogenation products of sludge mixture is aluminum chloride and and paraffinic hydrocarbons.After aluminum chloride discharges from the sludge mixture in a successive processes, aluminum chloride is dissolved in the Trimethylmethane, be transferred to outside the hydrogenator then, then and as the activator of 1-chlorobutane and additional Trimethylmethane mix the formation active catalyst, return and be input in the alkylation reactor to produce more alkylate.Use method of the present invention, the rate of recovery of aluminum chloride is near 100%, and this is because the sludge mixture is insoluble, and remains in the hydrogenator and be removed up to all aluminum chloride.Catalyzer with the production of circulation aluminum chloride is the same effective in producing high research octane number (RON) (RON) alkylate with the catalyzer that is formed by the aluminum chloride of newly buying from the market.Two kinds of catalyzer can both reach the RON more than 94.
Embodiment 1
This embodiment has illustrated the catalytic hydrogenation reaction of intermittence, aluminium of sludge mixture.This process is to carry out in the Parr of 35mL stirred-tank reactor.The mixture of 18g sludge mixture and 3g aluminium powder is put into reactor, and in the presence of the hydrogen of 1500psig, be heated to 150 ℃, stirred (700rpm) 3 hours simultaneously.Reactor cooling is to ambient temperature overnight.After the mixture cooling, sludge (brown liquid) has changed into the white crystal of entrained liquids fully.By the analysis of infrared spectra and aluminium and chlorine, find that crystal is an aluminum chloride.The analytical results of aluminium and chlorine is as follows.
| Element | Reclaim solid, wt% | Pure AlCl 3, calculated value, wt% |
| Aluminium content | 20.6 | ?20.3 |
| Cl content | 78.0 | ?80.0 |
Claims (35)
1. method that reclaims aluminum chloride from the sludge mixture that the alkylated reaction of aluminum chloride-catalyzed obtains comprises:
Form the mixture of sludge mixture and catalyzer aluminium; With
This mixture and aluminium are reacted under the condition that has hydrogen to exist, form aluminum chloride.
2. the process of claim 1 wherein that hydrogen provides with gaseous state, its pressure is the about 1500psig of about 500psig-.
3. the method for claim 2, wherein, the about 1500psig of the about 1000psig-of hydrogen pressure.
4. the method for claim 3, wherein, the about 1500psig of hydrogen pressure.
5. the process of claim 1 wherein that reactions steps is to carry out under about 125 ℃-Yue 200 ℃ temperature.
6. the method for claim 5, wherein, temperature of reaction is about 140 ℃-Yue 180 ℃.
7. the method for claim 6, wherein, temperature of reaction is about 150 ℃.
8. the process of claim 1 wherein about 4 hours of the about 2-of reactions steps.
9. the method for claim 8, wherein, reactions steps was carried out about 3 hours.
10. the process of claim 1 wherein that so the aluminum chloride that forms can be removed from reaction mixture.
11. the process of claim 1 wherein that aluminum chloride is removed by being dissolved in the Trimethylmethane.
12. the method for claim 10, wherein, so the aluminum chloride that forms is by cooling off described reaction mixture and the aluminum chloride precipitation being removed.
13. the method for claim 10 comprises the step of the aluminum chloride that recovery is so removed.
14. the method for claim 1 is intermittently carried out.
15. the method for claim 14, wherein, sludge mixture and catalyzer aluminium are with about 6: the ratio that 1-is about 7: 1 mixes.
16. the method for claim 15, wherein, sludge mixture and catalyzer aluminium mix with about 6: 1 ratio.
17. the method for claim 1 is carried out continuously.
18. the method for claim 1, semicontinuous carrying out.
19. the process of claim 1 wherein that described catalyzer aluminium is powder type.
20. the process of claim 1 wherein that described catalyzer aluminium is web form.
21. the process of claim 1 wherein that described catalyzer aluminium is the aluminium of purity at least 99%.
22. the process of claim 1 wherein that described sludge mixture contains aluminum chloride and olefin(e) compound.
23. the process of claim 1 wherein that described sludge mixture is from the olefin alkylation reaction that uses based on the catalyzer of homogeneous phase aluminum chloride.
24. the method for claim 23, wherein, described catalyzer based on homogeneous phase aluminum chloride contains the binding hydrocarbon of 46% weight of having an appointment and the binding aluminum chloride of about 54% weight.
25. the process of claim 1 wherein, speed of response be the about 3 weight sludge mixtures of about 2-/hour/weight catalyzer aluminium.
26. the process of claim 1 wherein that reactant is by continuously stirring.
27. the method for claim 5, wherein, reaction mixture during it is heated by continuously stirring.
28. the method for claim 17 may further comprise the steps:
Alkylate, Trimethylmethane and sludge mixture are sent to the settling tank from alkylation zone, the sludge mixture is precipitated out from alkylate;
Continuously described sludge is sent to hydrogenation zone from described settling tank;
Described sludge mixture is contacted with catalyzer aluminium under the condition that hydrogen and Trimethylmethane existence are arranged;
Form aluminum chloride;
With described aluminum chloride continuous-dissolution in described Trimethylmethane; And
Discharge aluminum chloride-Trimethylmethane solution from described hydrogenation zone.
29. the method for claim 18 may further comprise the steps:
Alkylate, Trimethylmethane and sludge mixture are sent to the settling tank from alkylation zone, the sludge mixture is precipitated out from alkylate;
Described sludge mixture regularly is sent to hydrogenation zone from settling tank;
Described sludge mixture is contacted with catalyzer aluminium under the condition that hydrogen and Trimethylmethane existence are arranged;
Form aluminum chloride;
With described aluminum chloride continuous-dissolution in described Trimethylmethane; And
Discharge aluminum chloride-Trimethylmethane solution from described hydrogenation zone.
30. the method for claim 28, wherein, described aluminum chloride-Trimethylmethane solution circulated turns back to described alkylation zone.
31. the method for claim 29, wherein, described aluminum chloride-Trimethylmethane solution circulated turns back to described alkylation zone.
32. the method for claim 28, wherein, described catalyzer aluminium is the screen cloth form.
33. the method for claim 29, wherein, described catalyzer aluminium is the screen cloth form.
34. the method for claim 28 is included in continuously stirring reactant and reaction product in the hydrogenation zone.
35. the method for claim 29 is included in continuously stirring reactant and reaction product in the hydrogenation zone.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| US08/775,522 US6004519A (en) | 1995-01-09 | 1997-01-02 | Aluminum promoted hydrogenation of alkylation sludge for aluminum chloride recovery |
| US08/775,522 | 1997-01-02 |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN1212669A true CN1212669A (en) | 1999-03-31 |
Family
ID=25104686
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN97192747.2A Pending CN1212669A (en) | 1997-01-02 | 1997-12-20 | Aluminium promoted hydrogenation of alkylation sludge for aluminium chloride recovery |
Country Status (8)
| Country | Link |
|---|---|
| EP (1) | EP0889851A4 (en) |
| CN (1) | CN1212669A (en) |
| AU (1) | AU5726798A (en) |
| BR (1) | BR9707905A (en) |
| EA (1) | EA000720B1 (en) |
| NO (1) | NO984012D0 (en) |
| PE (1) | PE76899A1 (en) |
| WO (1) | WO1998029340A1 (en) |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS59172617A (en) * | 1983-03-22 | 1984-09-29 | Olympus Optical Co Ltd | Microscope equipped with automatic control type optical lighting system |
Family Cites Families (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US1405734A (en) * | 1919-03-22 | 1922-02-07 | Gulf Refining Co | Manufacture of aluminum chloride |
| US1582131A (en) * | 1925-05-19 | 1926-04-27 | Standard Oil Co | Method of recovering alpha metallic halide from hydrocarbon sludges |
| US2416049A (en) * | 1942-10-05 | 1947-02-18 | Phillips Petroleum Co | Regeneration of spent catalyst |
| IT946067B (en) * | 1971-11-17 | 1973-05-21 | Sir Soc Italiana Resine Spa | IMPROVEMENTS IN THE ALKYLATION PROCEDURES |
| US4017584A (en) * | 1975-05-06 | 1977-04-12 | Societa' Italiana Resine S.I.R.. S.p.A. | Process for the recovery of aluminum trichloride |
-
1997
- 1997-12-20 BR BR9707905A patent/BR9707905A/en not_active Application Discontinuation
- 1997-12-20 EA EA199800787A patent/EA000720B1/en not_active IP Right Cessation
- 1997-12-20 CN CN97192747.2A patent/CN1212669A/en active Pending
- 1997-12-20 AU AU57267/98A patent/AU5726798A/en not_active Abandoned
- 1997-12-20 EP EP97953540A patent/EP0889851A4/en not_active Withdrawn
- 1997-12-20 WO PCT/US1997/024154 patent/WO1998029340A1/en not_active Application Discontinuation
- 1997-12-29 PE PE1997001172A patent/PE76899A1/en not_active Application Discontinuation
-
1998
- 1998-09-01 NO NO984012A patent/NO984012D0/en not_active Application Discontinuation
Also Published As
| Publication number | Publication date |
|---|---|
| EP0889851A1 (en) | 1999-01-13 |
| NO984012L (en) | 1998-09-01 |
| EP0889851A4 (en) | 2000-05-03 |
| EA000720B1 (en) | 2000-02-28 |
| BR9707905A (en) | 1999-07-27 |
| PE76899A1 (en) | 1999-08-16 |
| AU5726798A (en) | 1998-07-31 |
| NO984012D0 (en) | 1998-09-01 |
| EA199800787A1 (en) | 1999-04-29 |
| WO1998029340A1 (en) | 1998-07-09 |
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