WO2004081149A2 - Selective hydrogenation of acetylenes and dienes in a hydrocarbon stream - Google Patents
Selective hydrogenation of acetylenes and dienes in a hydrocarbon stream Download PDFInfo
- Publication number
- WO2004081149A2 WO2004081149A2 PCT/US2004/006535 US2004006535W WO2004081149A2 WO 2004081149 A2 WO2004081149 A2 WO 2004081149A2 US 2004006535 W US2004006535 W US 2004006535W WO 2004081149 A2 WO2004081149 A2 WO 2004081149A2
- Authority
- WO
- WIPO (PCT)
- Prior art keywords
- reactor
- boiling point
- liquid
- acetylenes
- dienes
- Prior art date
Links
- 150000001993 dienes Chemical class 0.000 title claims abstract description 20
- 125000002534 ethynyl group Chemical class [H]C#C* 0.000 title claims abstract description 20
- 238000005984 hydrogenation reaction Methods 0.000 title claims description 10
- 239000004215 Carbon black (E152) Substances 0.000 title description 7
- 229930195733 hydrocarbon Natural products 0.000 title description 7
- 150000002430 hydrocarbons Chemical class 0.000 title description 7
- 239000007788 liquid Substances 0.000 claims abstract description 26
- 238000009835 boiling Methods 0.000 claims abstract description 25
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 claims abstract description 18
- YXFVVABEGXRONW-UHFFFAOYSA-N Toluene Chemical compound CC1=CC=CC=C1 YXFVVABEGXRONW-UHFFFAOYSA-N 0.000 claims abstract description 18
- 239000003054 catalyst Substances 0.000 claims abstract description 17
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims abstract description 14
- 150000001336 alkenes Chemical class 0.000 claims abstract description 13
- 239000000203 mixture Substances 0.000 claims abstract description 13
- 238000006243 chemical reaction Methods 0.000 claims abstract description 12
- 239000001257 hydrogen Substances 0.000 claims abstract description 12
- 229910052739 hydrogen Inorganic materials 0.000 claims abstract description 12
- 239000008096 xylene Substances 0.000 claims abstract description 5
- 150000003738 xylenes Chemical class 0.000 claims abstract description 5
- 125000004435 hydrogen atom Chemical class [H]* 0.000 claims abstract 3
- 238000000034 method Methods 0.000 claims description 12
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 6
- 229910052799 carbon Inorganic materials 0.000 claims description 6
- 239000000463 material Substances 0.000 claims description 6
- 238000004821 distillation Methods 0.000 abstract description 7
- 230000003134 recirculating effect Effects 0.000 abstract description 4
- 239000002245 particle Substances 0.000 abstract description 3
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 6
- 239000000047 product Substances 0.000 description 5
- KDLHZDBZIXYQEI-UHFFFAOYSA-N Palladium Chemical compound [Pd] KDLHZDBZIXYQEI-UHFFFAOYSA-N 0.000 description 4
- 239000007789 gas Substances 0.000 description 4
- 150000002431 hydrogen Chemical class 0.000 description 3
- 239000007791 liquid phase Substances 0.000 description 3
- VLKZOEOYAKHREP-UHFFFAOYSA-N n-Hexane Chemical compound CCCCCC VLKZOEOYAKHREP-UHFFFAOYSA-N 0.000 description 3
- OFBQJSOFQDEBGM-UHFFFAOYSA-N n-pentane Natural products CCCCC OFBQJSOFQDEBGM-UHFFFAOYSA-N 0.000 description 3
- 238000012856 packing Methods 0.000 description 3
- 238000010992 reflux Methods 0.000 description 3
- 238000000926 separation method Methods 0.000 description 3
- VXNZUUAINFGPBY-UHFFFAOYSA-N 1-Butene Chemical compound CCC=C VXNZUUAINFGPBY-UHFFFAOYSA-N 0.000 description 2
- VQTUBCCKSQIDNK-UHFFFAOYSA-N Isobutene Chemical compound CC(C)=C VQTUBCCKSQIDNK-UHFFFAOYSA-N 0.000 description 2
- RRHGJUQNOFWUDK-UHFFFAOYSA-N Isoprene Chemical compound CC(=C)C=C RRHGJUQNOFWUDK-UHFFFAOYSA-N 0.000 description 2
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 description 2
- PPBRXRYQALVLMV-UHFFFAOYSA-N Styrene Chemical compound C=CC1=CC=CC=C1 PPBRXRYQALVLMV-UHFFFAOYSA-N 0.000 description 2
- HSFWRNGVRCDJHI-UHFFFAOYSA-N alpha-acetylene Natural products C#C HSFWRNGVRCDJHI-UHFFFAOYSA-N 0.000 description 2
- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 description 2
- 229910052763 palladium Inorganic materials 0.000 description 2
- YWAKXRMUMFPDSH-UHFFFAOYSA-N pentene Chemical compound CCCC=C YWAKXRMUMFPDSH-UHFFFAOYSA-N 0.000 description 2
- 238000010791 quenching Methods 0.000 description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 2
- LIKMAJRDDDTEIG-UHFFFAOYSA-N 1-hexene Chemical compound CCCCC=C LIKMAJRDDDTEIG-UHFFFAOYSA-N 0.000 description 1
- KAKZBPTYRLMSJV-UHFFFAOYSA-N Butadiene Chemical compound C=CC=C KAKZBPTYRLMSJV-UHFFFAOYSA-N 0.000 description 1
- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 description 1
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 description 1
- 239000005977 Ethylene Substances 0.000 description 1
- URLKBWYHVLBVBO-UHFFFAOYSA-N Para-Xylene Chemical group CC1=CC=C(C)C=C1 URLKBWYHVLBVBO-UHFFFAOYSA-N 0.000 description 1
- QQONPFPTGQHPMA-UHFFFAOYSA-N Propene Chemical compound CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 description 1
- 150000000475 acetylene derivatives Chemical class 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 description 1
- 239000001273 butane Substances 0.000 description 1
- 230000006835 compression Effects 0.000 description 1
- 238000007906 compression Methods 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- AHAREKHAZNPPMI-UHFFFAOYSA-N hexa-1,3-diene Chemical compound CCC=CC=C AHAREKHAZNPPMI-UHFFFAOYSA-N 0.000 description 1
- NNPPMTNAJDCUHE-UHFFFAOYSA-N isobutane Chemical compound CC(C)C NNPPMTNAJDCUHE-UHFFFAOYSA-N 0.000 description 1
- 239000012263 liquid product Substances 0.000 description 1
- IVSZLXZYQVIEFR-UHFFFAOYSA-N m-xylene Chemical group CC1=CC=CC(C)=C1 IVSZLXZYQVIEFR-UHFFFAOYSA-N 0.000 description 1
- IJDNQMDRQITEOD-UHFFFAOYSA-N n-butane Chemical compound CCCC IJDNQMDRQITEOD-UHFFFAOYSA-N 0.000 description 1
- TVMXDCGIABBOFY-UHFFFAOYSA-N octane Chemical compound CCCCCCCC TVMXDCGIABBOFY-UHFFFAOYSA-N 0.000 description 1
- 229910003445 palladium oxide Inorganic materials 0.000 description 1
- JQPTYAILLJKUCY-UHFFFAOYSA-N palladium(ii) oxide Chemical compound [O-2].[Pd+2] JQPTYAILLJKUCY-UHFFFAOYSA-N 0.000 description 1
- 239000012188 paraffin wax Substances 0.000 description 1
- 239000001294 propane Substances 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 238000005057 refrigeration Methods 0.000 description 1
- 102200058451 rs80358203 Human genes 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C5/00—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms
- C07C5/02—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by hydrogenation
- C07C5/08—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by hydrogenation of carbon-to-carbon triple bonds
- C07C5/09—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by hydrogenation of carbon-to-carbon triple bonds to carbon-to-carbon double bonds
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C5/00—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms
- C07C5/02—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by hydrogenation
- C07C5/03—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by hydrogenation of non-aromatic carbon-to-carbon double bonds
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C5/00—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms
- C07C5/02—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by hydrogenation
- C07C5/03—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by hydrogenation of non-aromatic carbon-to-carbon double bonds
- C07C5/05—Partial hydrogenation
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C7/00—Purification; Separation; Use of additives
- C07C7/148—Purification; Separation; Use of additives by treatment giving rise to a chemical modification of at least one compound
- C07C7/163—Purification; Separation; Use of additives by treatment giving rise to a chemical modification of at least one compound by hydrogenation
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C7/00—Purification; Separation; Use of additives
- C07C7/148—Purification; Separation; Use of additives by treatment giving rise to a chemical modification of at least one compound
- C07C7/163—Purification; Separation; Use of additives by treatment giving rise to a chemical modification of at least one compound by hydrogenation
- C07C7/167—Purification; Separation; Use of additives by treatment giving rise to a chemical modification of at least one compound by hydrogenation for removal of compounds containing a triple carbon-to-carbon bond
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C2523/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00
- C07C2523/38—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00 of noble metals
- C07C2523/40—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00 of noble metals of the platinum group metals
- C07C2523/44—Palladium
Definitions
- the present invention relates to a process for selectively hydrogenating acetylenes and dienes in a hydrocarbon stream. More particularly the invention relates to the selective hydrogenation of acetylenes and dienes in a hydrocarbon stream containing hydrogen, olefins and smaller amounts of acetylenes and dienes using a downflow boiling point reactor.
- the vapor product stream from the quench system of a hydrocarbon steam cracker typically consists mainly of hydrogen, methane, C 2 -C 6 olefins and paraffins, C 2 -C 6 acetylenes and dienes, benzene, toluene, xylenes, and other C 6 + components.
- Separation and recovery of the products according to carbon number is generally accomplished in a sequential distillation system after the first separation of hydrogen from the methane in a high pressure cold box system.
- the design of the distillation system is complicated by the fact that the differences in relative volatility of the olefins, acetylenes, and dienes of the same carbon number are small making if difficult to produce the pure olefin products.
- One method of circumventing this problem is to first separate the carbon number fractions and then to selectively hydrotreat each fraction to convert the acetylene and/or diene to its corresponding olefin or paraffin.
- This so called “back end” approach requires a separate hydrotreating system for each carbon number fraction as well as the addition of a requisite amount of hydrogen to each system.
- An alternative method is to hydrotreat the feed stream before separation using the contained hydrogen as the source of hydrogen for the conversion.
- This so-called “front end” approach has the advantage , of removing a significant portion of the hydrogen from the feed stream to the cold box thereby reducing the size and refrigeration requirements of the cold box.
- the present invention provides a "front end" hydrotreating system that allows for effective control of the temperature within a bed of catalyst which is hydrogenating acetylenes and dienes in a stream containing hydrogen, methane, C 2 -C 6 olefins and paraffins, C 2 -C 6 acetylenes and dienes, benzene, toluene, xylenes, and other C 6 + components.
- the invention utilizes a downflow boiling point reactor wherein the heat of reaction is absorbed by the liquid in the reactor which produces a vapor. Besides the feed to the reactor there is a recirculating stream which is fed at a rate sufficient to ensure that the catalyst particles within the reactor are wetted.
- a third stream which is taken from a downstream distillation column, is fed to provide the make up mass corresponding to the mass evaporated in the reactor.
- the composition of the this third stream controls the steady state composition of the liquid flowing through the reactor.
- the composition of this stream may be controlled by selecting the point from the downstream distillation column from which the stream is drawn. The lower the draw point is in the column, the higher the boiling point of the components in the third stream.
- the steady state composition of the liquid flowing through the reactor along with the pressure determines the reactor temperature profile. In a "boiling point reactor" a liquid phase is always maintained, even if the reaction components would be vaporized by the exothermic heat of reaction. In any reaction where the reaction stream is likely to be vaporized, an inert higher boiling component may be added to maintain a liquid phase.
- FIG. 1 is aflowdiagram in schematic form of one embodiment of the invention.
- FIG.2 is graphical representation of the temperature profile in atypical reactor of the present invention.
- Catalysts which are useful for the selective hydrogenation of acetylenes and dienes include palladium oxide supported on alumina.
- One such catalyst contains 0.34 wt.% palladium supported on 1/8 inch spheres designated G68C and supplied by S ⁇ d-Chemie (formerly United Catalyst Inc.).
- Another catalyst comprises 0.5 wt.% palladium supported on 8-12 mesh spheres and designated E144SDU as supplied by Calcicat, Catalyst and Performance Chemicals Division, Mallinckrodt, Inc.
- E144SDU as supplied by Calcicat, Catalyst and Performance Chemicals Division, Mallinckrodt, Inc.
- the catalyst is supported in structured packing as disclosed in commonly owned U.S. Pat. No. 5,730,843.
- the catalyst may, however, be simply loaded into the reactor.
- selective hydrogenation of acetylenes and diolefins in a hydrocarbon stream containing significantly larger amounts (molar basis) of hydrogen and olefins than the acetylenes and diolefins is carried out in a downflow boiling point reactor.
- the downflow boiling point reactor shown as column 10 is a vertically disposed reactor containing the particulate catalyst supported in a structured packing at 12.
- the gaseous feed stream is fed via flow line 101 to the top of the column 10.
- liquid in flow line 104 which is a mixture of circulating stream in flow line 102 and stream in flow line 103 derived from distillation column 40 as more particularly described below.
- Gas and liquid streams flow concurrently downward through the column with the flow regime being gas continuous. The concurrent flow of gas and liquid eliminates the possibility of a runaway reaction.
- the reactor 10 is operated adiabatically so that the heat of reaction is accounted for by preferentially evaporating the lighter liquid phase components.
- Effluent from the reactor in flow line 105 is fed to vapor/liquid separator 20 where the vapor and liquid are separated.
- the heat content of the vapor in flow line 106 includes the heat of reaction generated in the reactor 10 while its mass rate is equal to the combined flows of the streams in flow lines 101 and 103 less slip stream 107 described below.
- Liquid in flow line 102 is fed back to the top of the reactor 10.
- the flow rate of the stream in flow line 102 is a variable and is maintained at least sufficient to ensure that the catalyst particles are fully wetted at all positions in the reactor 10.
- the stream in flow line 103 provides make up mass corresponding to the mass evaporated in the reactor that leaves the reactor system as part of the stream in flow line 106.
- the composition of the stream in flow line 103 controls the steady state composition of liquid flowing through the reactor 10. This is an important operating parameter that in combination with the reactor pressure determines the reactor temperature profile.
- a slip stream is taken by flow line 107 to control the liquid inventory in the vapor/liquid separator vessel 20.
- Column 40 is a C 5 /C 6 splitter. Feed to the column is the vapor from the separator 20 in flow line 106. It is heated by indirect heat exchange in exchanger 30 with the recirculating stream in flow line 103.
- the column 40 is designed to recover a vapor distillate fraction via flow line 108 which is essentially free of C 6 + components and a bottoms liquid product in flow line 109 which is essentially free of C 5 and lighter components.
- the overheads are taken via flow line 130 and passed through partial condenser 50 where the heavier components are condensed.
- the overheads are collected in receiver separator 60 where liquid hydrocarbon is withdrawn via flow line 120 and returned to the column 40 as reflux. Water is taken out via flow line 110. As noted distillate product is removed via flow line 108.
- the draw off position or tray of the recirculating stream in flow line 103 is an operating variable. Moving the take off point further down the column increases the higher boiling components in the stream. Minimum operating pressure for the reactor 10 at a fixed temperature profile is achieved when the draw off is from the bottom stage of the column 40.
- Feed to the system depicted in FIG. 1 is the vapor product from the quench tower of an olefins producing steam cracker after compression and acid gas (CO 2 and H 2 S) removal.
- the reactor is loaded with approximately 14,000 ft 3 structured packing loaded with hydrogenation catalyst. Bed dimensions are approximately 15 ft diameter by 70 ft long.
- Operating conditions for the reactor are: reactor top/bottom pressure 250/240 psia; liquid recycle rate (stream in flow line 102) 4,000,000 lbs./hr.; slip stream in flow line 1072243 lbs./hr.
- the disti Nl ation column 40 is a column configured with a 16.4 ft diameter 20 stage (theoreti cc al) top section and 10.5 ft 20 stage (theoretical) bottom section.
- Design condi itions for the distillation column 40 are: reflux ratio 0.18; reflux temperature 136°F, condenser pressure is 238 psia; column pressure drop is 2 psi; bottom stage side draw; decanter temperature 84°F. Heat and material balance results are given in TABLE I. Temperature profile across the reactor is given in FIG. 2.
Abstract
Description
Claims
Priority Applications (5)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
JP2006509063A JP2006522120A (en) | 2003-03-12 | 2004-03-04 | Selective hydrogenation of acetylenes and dienes in hydrocarbon streams. |
AU2004219723A AU2004219723A1 (en) | 2003-03-12 | 2004-03-04 | Selective hydrogenation of acetylenes and dienes in a hydrocarbon stream |
MXPA05009270A MXPA05009270A (en) | 2003-03-12 | 2004-03-04 | Selective hydrogenation of acetylenes and dienes in a hydrocarbon stream. |
CA002518260A CA2518260A1 (en) | 2003-03-12 | 2004-03-04 | Selective hydrogenation of acetylenes and dienes in a hydrocarbon stream |
EP04717376A EP1618082A2 (en) | 2003-03-12 | 2004-03-04 | Selective hydrogenation of acetylenes and dienes in a hydrocarbon stream |
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
US10/385,677 US6867338B2 (en) | 2002-03-15 | 2003-03-12 | Selective hydrogenation of acetylenes and dienes in a hydrocarbon stream |
US10/385,677 | 2003-03-12 |
Publications (2)
Publication Number | Publication Date |
---|---|
WO2004081149A2 true WO2004081149A2 (en) | 2004-09-23 |
WO2004081149A3 WO2004081149A3 (en) | 2005-01-13 |
Family
ID=32987306
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
PCT/US2004/006535 WO2004081149A2 (en) | 2003-03-12 | 2004-03-04 | Selective hydrogenation of acetylenes and dienes in a hydrocarbon stream |
Country Status (14)
Country | Link |
---|---|
US (2) | US6867338B2 (en) |
EP (1) | EP1618082A2 (en) |
JP (1) | JP2006522120A (en) |
KR (1) | KR20050106112A (en) |
CN (1) | CN100371305C (en) |
AR (1) | AR043554A1 (en) |
AU (1) | AU2004219723A1 (en) |
BR (1) | BRPI0400329A (en) |
CA (1) | CA2518260A1 (en) |
EG (1) | EG23539A (en) |
MX (1) | MXPA05009270A (en) |
PL (1) | PL378808A1 (en) |
RU (1) | RU2325429C2 (en) |
WO (1) | WO2004081149A2 (en) |
Cited By (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JP2008528684A (en) * | 2005-02-01 | 2008-07-31 | キャタリティック・ディスティレイション・テクノロジーズ | Processes and catalysts used in the selective hydrogenation of dienes and acetylenes. |
Families Citing this family (11)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US20040030207A1 (en) * | 2002-08-08 | 2004-02-12 | Catalytic Distillation Technologies | Selective hydrogenation of acetylenes |
US7022645B2 (en) * | 2003-08-04 | 2006-04-04 | Catalytic Distillation Technologies | Ni hydrogenation catalysts, manufacture and use |
JP4845172B2 (en) * | 2005-03-30 | 2011-12-28 | 月島機械株式会社 | Method and apparatus for adiabatic cooling crystallization of organic compounds |
US7408090B2 (en) * | 2005-04-07 | 2008-08-05 | Catalytic Distillation Technologies | Method of operating downflow boiling point reactors in the selective hydrogenation of acetylenes and dienes |
US8471082B2 (en) * | 2008-03-14 | 2013-06-25 | Catalytic Distillation Technologies | Process for converting methane to ethylene |
EP2223987A1 (en) * | 2009-02-17 | 2010-09-01 | ISP Marl GmbH | Purification of an aromatic fraction containing acetylenes by selective hydrogenation of the acetylenes |
US20120209042A1 (en) | 2011-02-10 | 2012-08-16 | Saudi Basic Industries Corporation | Liquid Phase Hydrogenation of Alkynes |
US9695096B2 (en) * | 2012-07-12 | 2017-07-04 | Lummus Technology Inc. | More energy efficient C5 hydrogenation process |
JP6298438B2 (en) * | 2014-11-28 | 2018-03-20 | 旭化成株式会社 | Process for producing hydrocarbons |
FR3045651B1 (en) * | 2015-12-22 | 2018-01-19 | IFP Energies Nouvelles | METHOD FOR SELECTIVE HYDROGENATION OF OLEFINIC LOADS WITH A MAIN REACTOR THRESHOLD AND A REDUCED SIZE REACTION REACTOR |
RU2673550C1 (en) * | 2018-05-15 | 2018-11-28 | Публичное Акционерное Общество "Нижнекамскнефтехим" | Method for coproduction of cyclohexane and hexane solvent |
Citations (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US20020022754A1 (en) * | 2000-06-28 | 2002-02-21 | Institut Francais Du Petrole | Process for hydrogenating cuts containing hydrocarbons, in particular unsaturated molecules containing at least two double bonds or at least one triple bond |
Family Cites Families (28)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US2918425A (en) * | 1958-03-27 | 1959-12-22 | Universal Oil Prod Co | Conversion process and apparatus therefor |
US3560167A (en) * | 1968-12-18 | 1971-02-02 | Air Prod & Chem | Upflow catalytic reactor for fluid hydrocarbons |
US3702237A (en) * | 1970-07-02 | 1972-11-07 | Universal Oil Prod Co | Hydrocarbon conversion apparatus |
US4126539A (en) * | 1977-12-05 | 1978-11-21 | Mobil Oil Corporation | Method and arrangement of apparatus for hydrogenating hydrocarbons |
US4194964A (en) * | 1978-07-10 | 1980-03-25 | Mobil Oil Corporation | Catalytic conversion of hydrocarbons in reactor fractionator |
US4171260A (en) * | 1978-08-28 | 1979-10-16 | Mobil Oil Corporation | Process for reducing thiophenic sulfur in heavy oil |
US4283271A (en) * | 1980-06-12 | 1981-08-11 | Mobil Oil Corporation | Manufacture of hydrocracked low pour lubricating oils |
US5190730A (en) * | 1982-11-17 | 1993-03-02 | Chemical Research & Licensing Company | Reactor for exothermic reactions |
US4484983A (en) * | 1983-05-23 | 1984-11-27 | Shell Oil Company | Distillation and vapor treatment process |
US4990242A (en) * | 1989-06-14 | 1991-02-05 | Exxon Research And Engineering Company | Enhanced sulfur removal from fuels |
US5011593A (en) * | 1989-11-20 | 1991-04-30 | Mobil Oil Corporation | Catalytic hydrodesulfurization |
US5409599A (en) * | 1992-11-09 | 1995-04-25 | Mobil Oil Corporation | Production of low sulfur distillate fuel |
US5714640A (en) * | 1994-01-21 | 1998-02-03 | Mobil Oil Corporation | Vapor pocket reactor |
US5510568A (en) * | 1994-06-17 | 1996-04-23 | Chemical Research & Licensing Company | Process for the removal of mercaptans and hydrogen sulfide from hydrocarbon streams |
US5554275A (en) * | 1994-11-28 | 1996-09-10 | Mobil Oil Corporation | Catalytic hydrodesulfurization and stripping of hydrocarbon liquid |
US5779883A (en) * | 1995-07-10 | 1998-07-14 | Catalytic Distillation Technologies | Hydrodesulfurization process utilizing a distillation column realtor |
US5961815A (en) * | 1995-08-28 | 1999-10-05 | Catalytic Distillation Technologies | Hydroconversion process |
US5597476A (en) * | 1995-08-28 | 1997-01-28 | Chemical Research & Licensing Company | Gasoline desulfurization process |
CA2244374C (en) | 1996-02-02 | 2005-04-12 | Exxon Research And Engineering Company | Selective hydrodesulfurization catalyst and process |
US5925799A (en) * | 1996-03-12 | 1999-07-20 | Abb Lummus Global Inc. | Catalytic distillation and hydrogenation of heavy unsaturates in an olefins plant |
US5807477A (en) * | 1996-09-23 | 1998-09-15 | Catalytic Distillation Technologies | Process for the treatment of light naphtha hydrocarbon streams |
US5837130A (en) * | 1996-10-22 | 1998-11-17 | Catalytic Distillation Technologies | Catalytic distillation refining |
US5925685A (en) * | 1996-11-18 | 1999-07-20 | Catalytic Distillation Technologies | Method for carrying out heterogeneous catalysis |
US5863419A (en) * | 1997-01-14 | 1999-01-26 | Amoco Corporation | Sulfur removal by catalytic distillation |
US5897768A (en) | 1997-02-28 | 1999-04-27 | Exxon Research And Engineering Co. | Desulfurization process for removal of refractory organosulfur heterocycles from petroleum streams |
US6083378A (en) * | 1998-09-10 | 2000-07-04 | Catalytic Distillation Technologies | Process for the simultaneous treatment and fractionation of light naphtha hydrocarbon streams |
US6413413B1 (en) * | 1998-12-31 | 2002-07-02 | Catalytic Distillation Technologies | Hydrogenation process |
US6416658B1 (en) * | 2000-10-19 | 2002-07-09 | Catalytic Distillation Technologies | Process for simultaneous hydrotreating and splitting of naphtha streams |
-
2003
- 2003-03-12 US US10/385,677 patent/US6867338B2/en not_active Expired - Lifetime
-
2004
- 2004-03-04 EP EP04717376A patent/EP1618082A2/en not_active Withdrawn
- 2004-03-04 KR KR1020057016922A patent/KR20050106112A/en not_active Application Discontinuation
- 2004-03-04 CA CA002518260A patent/CA2518260A1/en not_active Abandoned
- 2004-03-04 PL PL378808A patent/PL378808A1/en not_active Application Discontinuation
- 2004-03-04 CN CNB2004800064972A patent/CN100371305C/en not_active Expired - Fee Related
- 2004-03-04 WO PCT/US2004/006535 patent/WO2004081149A2/en active Application Filing
- 2004-03-04 RU RU2005131579/04A patent/RU2325429C2/en not_active IP Right Cessation
- 2004-03-04 MX MXPA05009270A patent/MXPA05009270A/en unknown
- 2004-03-04 AU AU2004219723A patent/AU2004219723A1/en not_active Abandoned
- 2004-03-04 JP JP2006509063A patent/JP2006522120A/en not_active Withdrawn
- 2004-03-09 EG EG2004030104A patent/EG23539A/en active
- 2004-03-10 BR BR0400329-2A patent/BRPI0400329A/en not_active IP Right Cessation
- 2004-03-11 AR ARP040100788A patent/AR043554A1/en unknown
- 2004-11-08 US US10/983,433 patent/US7368617B2/en active Active
Patent Citations (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US20020022754A1 (en) * | 2000-06-28 | 2002-02-21 | Institut Francais Du Petrole | Process for hydrogenating cuts containing hydrocarbons, in particular unsaturated molecules containing at least two double bonds or at least one triple bond |
Cited By (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JP2008528684A (en) * | 2005-02-01 | 2008-07-31 | キャタリティック・ディスティレイション・テクノロジーズ | Processes and catalysts used in the selective hydrogenation of dienes and acetylenes. |
Also Published As
Publication number | Publication date |
---|---|
RU2325429C2 (en) | 2008-05-27 |
KR20050106112A (en) | 2005-11-08 |
PL378808A1 (en) | 2006-05-15 |
RU2005131579A (en) | 2006-02-10 |
AR043554A1 (en) | 2005-08-03 |
EP1618082A2 (en) | 2006-01-25 |
CN100371305C (en) | 2008-02-27 |
US6867338B2 (en) | 2005-03-15 |
MXPA05009270A (en) | 2005-10-19 |
JP2006522120A (en) | 2006-09-28 |
CN1759083A (en) | 2006-04-12 |
EG23539A (en) | 2006-04-26 |
US20050090701A1 (en) | 2005-04-28 |
AU2004219723A1 (en) | 2004-09-23 |
US7368617B2 (en) | 2008-05-06 |
CA2518260A1 (en) | 2004-09-23 |
US20030233017A1 (en) | 2003-12-18 |
BRPI0400329A (en) | 2005-01-04 |
WO2004081149A3 (en) | 2005-01-13 |
Similar Documents
Publication | Publication Date | Title |
---|---|---|
US8227650B2 (en) | Process and catalyst for selective hydrogenation of dienes and acetylenes | |
US6169218B1 (en) | Selective hydrogenation of highly unsaturated compounds in hydrocarbon streams | |
KR101603392B1 (en) | Process for the production of olefins | |
US6858766B2 (en) | Process for selectively hydrogenating mixed phase front end C2-C10 greater unsaturated hydrocarbons | |
EP0733030A1 (en) | Selective hydrogenation of highly unsaturated compounds in hydrocarbon streams | |
TWI628273B (en) | Producing c5 olefins from steam cracker c5 feeds | |
US6867338B2 (en) | Selective hydrogenation of acetylenes and dienes in a hydrocarbon stream | |
TW200829535A (en) | Propylene production | |
EA023049B1 (en) | Process for producing ultra low benzene reformate using catalytic distillation | |
CA2089113C (en) | Selective hydrogenation of c5 streams | |
US6495732B1 (en) | Olefin isomerization process | |
US7408090B2 (en) | Method of operating downflow boiling point reactors in the selective hydrogenation of acetylenes and dienes | |
WO2003062178A1 (en) | Process for the utilization of refinery c4 streams | |
CN115504851A (en) | Process for removing olefins from normal paraffins in an isomerization effluent stream | |
JP4376908B2 (en) | Improved olefin plant recovery system using a combination of catalytic distillation and fixed bed catalytic process | |
CN117157266A (en) | Process for increasing the concentration of normal hydrocarbons in a light naphtha stream | |
CN117222611A (en) | Ethane separation using cryogenic heat exchanger |
Legal Events
Date | Code | Title | Description |
---|---|---|---|
AK | Designated states |
Kind code of ref document: A2 Designated state(s): AE AG AL AM AT AU AZ BA BB BG BR BW BY BZ CA CH CN CO CR CU CZ DE DK DM DZ EC EE EG ES FI GB GD GE GH GM HR HU ID IL IN IS JP KE KG KP KR KZ LC LK LR LS LT LU LV MA MD MG MK MN MW MX MZ NA NI NO NZ OM PG PH PL PT RO RU SC SD SE SG SK SL SY TJ TM TN TR TT TZ UA UG US UZ VC VN YU ZA ZM ZW |
|
AL | Designated countries for regional patents |
Kind code of ref document: A2 Designated state(s): BW GH GM KE LS MW MZ SD SL SZ TZ UG ZM ZW AM AZ BY KG KZ MD RU TJ TM AT BE BG CH CY CZ DE DK EE ES FI FR GB GR HU IE IT LU MC NL PL PT RO SE SI SK TR BF BJ CF CG CI CM GA GN GQ GW ML MR NE SN TD TG |
|
121 | Ep: the epo has been informed by wipo that ep was designated in this application | ||
WWE | Wipo information: entry into national phase |
Ref document number: 2006509063 Country of ref document: JP Ref document number: 3305/DELNP/2005 Country of ref document: IN |
|
WWE | Wipo information: entry into national phase |
Ref document number: 2004219723 Country of ref document: AU |
|
ENP | Entry into the national phase |
Ref document number: 2004219723 Country of ref document: AU Date of ref document: 20040304 Kind code of ref document: A |
|
WWP | Wipo information: published in national office |
Ref document number: 2004219723 Country of ref document: AU |
|
WWE | Wipo information: entry into national phase |
Ref document number: PA/a/2005/009270 Country of ref document: MX |
|
WWE | Wipo information: entry into national phase |
Ref document number: 2518260 Country of ref document: CA |
|
WWE | Wipo information: entry into national phase |
Ref document number: 20048064972 Country of ref document: CN Ref document number: 1020057016922 Country of ref document: KR |
|
WWE | Wipo information: entry into national phase |
Ref document number: 2005200500771 Country of ref document: RO |
|
WWE | Wipo information: entry into national phase |
Ref document number: 2004717376 Country of ref document: EP |
|
WWE | Wipo information: entry into national phase |
Ref document number: 2005131579 Country of ref document: RU |
|
WWP | Wipo information: published in national office |
Ref document number: 1020057016922 Country of ref document: KR |
|
WWP | Wipo information: published in national office |
Ref document number: 2004717376 Country of ref document: EP |