EP0856572A1 - Verfahren zur hydrierenden Entaromatisierung - Google Patents
Verfahren zur hydrierenden Entaromatisierung Download PDFInfo
- Publication number
- EP0856572A1 EP0856572A1 EP98101740A EP98101740A EP0856572A1 EP 0856572 A1 EP0856572 A1 EP 0856572A1 EP 98101740 A EP98101740 A EP 98101740A EP 98101740 A EP98101740 A EP 98101740A EP 0856572 A1 EP0856572 A1 EP 0856572A1
- Authority
- EP
- European Patent Office
- Prior art keywords
- catalyst
- aromatic hydrocarbons
- nickel
- stream
- content
- 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.)
- Withdrawn
Links
Classifications
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G45/00—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds
- C10G45/44—Hydrogenation of the aromatic hydrocarbons
- C10G45/46—Hydrogenation of the aromatic hydrocarbons characterised by the catalyst used
- C10G45/48—Hydrogenation of the aromatic hydrocarbons characterised by the catalyst used containing nickel or cobalt metal, or compounds thereof
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/10—Feedstock materials
- C10G2300/1096—Aromatics or polyaromatics
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/40—Characteristics of the process deviating from typical ways of processing
- C10G2300/4006—Temperature
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/40—Characteristics of the process deviating from typical ways of processing
- C10G2300/4012—Pressure
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
- C10G2400/02—Gasoline
Definitions
- the invention relates to a process for the hydrogenating dearomatization of aromatic hydrocarbons in the feed streams containing them, especially reformate streams.
- the invention further relates to the use of dearomatized streams thus obtained as a component in Fuels.
- the reformate produced by catalytic reforming of naphtha represents the most important source for the production of high octane gasoline
- the essential components of the reformate flow are aromatic Compounds such as benzene, toluene, xylene and ethylbenzene.
- the boiling range the hydrocarbon mixture is between 60 and 180 ° C.
- the saturated hydrocarbons and aromatic compounds contain the untreated reformate streams such as olefins and diolefins.
- the benzene content in reformate streams is between 2 and 8 Vol .-% depending on the reforming conditions, catalyst used and Feedstock.
- benzene is different in terms of octane number and boiling point Suitable as a gasoline fuel component is due to its carcinogenic Properties anticipate that new environmental regulations will become one worldwide reduction of the benzene content in petrol will. So is already in the United States of America according to the US Clean Air Act passed in 1990 the benzene content in Otto fuels a maximum of 1% by volume.
- Another possibility for further processing of the benzene-rich light reformate gasoline is the alkylation of the benzene by olefins (eg propylene) contained in refinery cracking gases to give substituted aromatics.
- olefins eg propylene
- the resulting mixture is hardly suitable as a gasoline fuel component due to the too high boiling point of the substituted C 9+ aromatics formed.
- An additional disadvantage is the insufficient availability of such olefins for this purpose in every refinery.
- Another option for further processing of the benzene-rich light reformate gasoline consists in the catalytic hydrogenating dearomatization.
- the resulting benzene-free light reformate gasoline has a corresponding high naphthen content and can therefore without affecting the the resulting octane number is then flashed back into heavy reformate gasoline will.
- AU-B-83524/91 discloses a process in which a light reformate gasoline is produced using hydrogen over a catalyst, consisting of a mixture of elements from VIII. And III. Group of the periodic table, preferably Pt / Ni impregnated on Al 2 O 3 , is dearomatized in the gas phase at 5 to 25 bar and 150 to 350 ° C.
- FR-A-2 693 648 describes a similar dearomatization process on a catalyst consisting of an Al 2 O 3 support onto which platinum, rhenium and chloride are impregnated.
- EP-A1-0 552 072 discloses a process for the dearomatization of gasoline fractions, the gasoline fraction in one hydrogenation stage and subsequent is treated in an isomerization step.
- the hydrogenation catalyst contains Nickel, platinum or palladium on aluminum oxide.
- the isomerization catalyst includes platinum supported on 80% mordenite and 20% alumina.
- US 5,246,567 relates to a process for the hydrogenation of benzene in light petroleum fractions, being an isomerization stage with a hydrogenation stage is combined.
- the isomerization is carried out in the presence of a Platinum group catalyst performed.
- the product obtained with another stream containing benzene mixed and hydrogenated, with a metal of group VIII of the Periodic table is used on an inorganic oxide support.
- This object is achieved by a process for hydrogenating dearomatization from aromatic hydrocarbons to aromatic hydrocarbons containing feed streams, in which such aromatic hydrocarbons containing feed stream on a nickel-containing precipitation catalyst at a temperature of 50 to 300 ° C, a pressure of 20 to 80 bar and a catalyst load of 1 to 6 kg / (lxh) in the presence of free hydrogen is hydrogenated.
- nickel-containing precipitation catalysts such as are also known from EP-A 0 672 452, a very effective hydrating Allow dearomatization, being hydrogenated with this catalyst under high reformate load and medium pressure and medium temperature conditions is carried out.
- EP-A1-0 672 452 does not show that a highly effective hydrogenation of aromatic hydrocarbons at high catalyst loads medium temperature and pressure level is possible. Especially with the hydrogenating dearomatization of benzene-rich light reformate gasoline the nickel-containing precipitation catalysts have a very high activity.
- the nickel precipitation catalysts used according to the invention are in EP-A1-0 672 452. These are catalysts that essentially 65 to 80% nickel, calculated as nickel oxide, 10 to 25 % Silicon calculated as silica, 2 to 10% zirconium calculated as zirconium oxide and 0 to 10% aluminum, calculated as aluminum oxide included with the proviso that the sum of the content of silicon and Aluminum is at least 15% (percentages in% by weight, based to the total mass of the catalyst) by adding an acid aqueous solution of nickel, zirconium and, if desired, aluminum salts to a basic aqueous solution of silicon and if desired Aluminum compounds with a pH of at least 6.5 lowered and then by adding further basic solution to pH values is set from 7 to 8, isolating the solid so precipitated, Drying, molding and calcining are available.
- the catalysts used according to the invention preferably contain 70 to 78% nickel, calculated as nickel oxide, 10 to 20% silicon, calculated as Silicon dioxide, 3 to 7% zirconium, calculated as zirconium oxide and 2 up to 10% aluminum, calculated as aluminum oxide with the proviso that the sum of silicon and aluminum, calculated as oxides, at least Is 15%.
- Catalysts are preferably used which only have nickel as catalytic contain active metal.
- those catalysts that are free of Noble metals such as platinum and palladium can be used.
- the catalysts can contain promoters in amounts of up to 10%. These are compounds such as CuO, TiO 2 , MgO, CaO, ZnO and B 2 O 3 . However, catalysts which do not contain any promoters are preferred.
- the catalysts according to the invention are prepared from aqueous ones acidic solutions of nickel, zirconium and optionally aluminum salts out.
- Organic and inorganic salts such as acetates, Sulfates, carbonates, but preferably nitrates of the metals mentioned in Consideration.
- the total content of metal salts is generally 30 to 40% by weight. Since the later precipitation of the metals from the solution is practical done quantitatively, the concentration of the individual components depends on the Solution only from the content of the catalyst to be produced in this component from.
- the aqueous solution is preferably added by adding a mineral acid Nitric acid adjusted to a pH below 2.
- This solution is, advantageously with stirring, in an aqueous basic Solution, the silicon compounds and, if desired, aluminum compounds contains, registered.
- This solution contains, for example, alkali metal hydroxide or preferably soda, usually in amounts of 15 to 40 wt .-%, based on the solution.
- the pH is generally around over 10.
- SiO 2 can also be used as the silicon compound.
- the silicon content of the solution is expediently 0.5 to 4% by weight.
- the solution may contain aluminum compounds in the form of oxidic solids, although it is preferred to add aluminum salts only to the acidic solution.
- the acidic addition to the basic solution is generally carried out at 30 to 100 ° C., preferably at 60 to 80 ° C. It is usually carried out over a period of 0.5 to 4 hours.
- catalysts which contain promoters are desired, it is expedient to one of the solutions described soluble metal salts as precursors for add the promoters, co-precipitate these metals and with the so obtained To further process the precipitate.
- the promoters can also be added as solids in the precipitation solution.
- the precipitated product is isolated, for example by filtration. In the This is usually followed by a washing step, in particular where appropriate Alkali metal ions and nitrate ions entrained during the precipitation be washed out.
- the solid thus obtained is then dried, for which, depending on the amount of dry goods, a drying cabinet, for example or a spray dryer can be used. Generally is the drying temperature 100 to 200 ° C. Before the next step if desired, the solid can use the above promoters be added.
- the dried product is then preferably calcined, which is usually at temperatures of 300 to 700 ° C, preferably 320 to 450 ° C, over a period of 0.5 to 8 hours.
- the calcined solid is added to the intended use Shaped bodies, for example by extrusion into strands or by Tableting.
- the calcined solid is known per se Peptizing agents such as nitric acid or formic acid in amounts of in generally 0.1 to 10% by weight, based on the solid to be molded, added.
- Graphite e.g. Graphite can be used.
- the so Moldings obtained are usually at temperatures from 300 to 700 ° C, preferably 350 to 500 ° C, over a period of 1 to 8 Hours calcined.
- the feed streams preferably used in the process according to the invention contain about 12 to about 30% by weight of aromatic hydrocarbons, especially benzene.
- the preferred feed streams are reformate streams, in particular light reformate gasoline flows with a boiling range from 35 to 100 ° C.
- a catalyst which is 70 to 80 is preferably used in the process %
- the use of the hydrogenation stage according to the invention is also suitable in Combination with one or more upstream distillation, extraction and / or Extractive distillation stages to increase the content aromatic hydrocarbons. Suitable methods are as above specified.
- the dearomatized streams preferably contain after the hydrogenation maximum 0.05% by weight of aromatic hydrocarbons.
- the dearomatized Streams can be used as a component in petrol engine fuels will.
Landscapes
- Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
- Catalysts (AREA)
Abstract
Description
- eine hocheffektive Hydrierung der aromatischen Kohlenwasserstoffe erfolgt
- die Oktanzahl des behandelten Gemisches im wesentlichen nicht beeinträchtigt wird
- ein stabiler, preiswerter Katalysator eingesetzt wird
- das Verfahren in einfacher Weise in vorhandene Raffinerie-Anlagen eingebaut werden kann
- hohe Katalysatorbelastungen möglich sind bei mittlerem Temperatur- und Druckniveau.
Hydrierverfahrensparameter | ||
Bereich | bevorzugter Bereich | |
Temperatur | 50 - 300°C | 70 - 200°C |
Druck | 20 - 80 bar | 25 - 40 bar |
Belastung | 1-6 kg/(l x h) | 2-4 kg/(l x h) |
Wasserstoffzufuhr | 0,1-1 Nm3/kg | 0,2-0,5 Nm3/kg |
Rückführung, Frischeinlauf | 1 - 10 kg/kg | 1 - 3 kg/kg |
- Temperatur: T = 100°C
- Wasserstoffdruck: P = 30 bar
- Katalysatorbelastung: 6 kg/(lKat x h)
- Wasserstoffzufuhr: 0,24 Nm3/kgBenzin
- Rückführung/Frischeinlauf: 2 kg/kg
Einsatz | Ni-Fällkat. (erfindungsgemäß) | Edelmetall- Tränkkatalysator (Vergleich) | |
Benzol (Gew.-%) | 12,6 | 0,005 | 6,5 |
Cyclohexan (Gew.-%) | 0,21 | 13,5 | 6,9 |
Methylcyclopentan (Gew.-%) | 2,53 | 2,9 | 2,9 |
Research-Octanzahl | 76,8 | 70,3 | nicht ermittelt |
Claims (8)
- Verfahren zur hydrierenden Entaromatisierung von aromatischen Kohlenwasserstoffen in aromatische Kohlenwasserstoffe enthaltenden Speiseströmen, dadurch gekennzeichnet, daß ein solche aromatischen Kohlenwasserstoffe enthältender Speisestrom an einem nickelhaltigen Fällkatalysator bei einer Temperatur von 50 bis 300°C, einem Druck von 20 bis 80 bar und einer Katalysatorbelastung von 1 bis 6 kg/(lxh) in Gegenwart von freiem Wasserstoff hydriert wird.
- Verfahren nach Anspruch 1, dadurch gekennzeichnet, daß der Speisestrom an einem nickelhaltigen Fällkatalysator bei einer Temperatur von 70 und 200°C, einem Druck von 25 bis 40 bar und einer Katalysatorbelastung von 2 bis 4 kg/(lxh) in Gegenwart von freiem Wasserstoff hydriert wird.
- Verfahren nach Anspruch 1 oder 2, dadurch gekennzeichnet, daß als Speisestrom ein solcher mit einem Gehalt von 2 bis 30 Gew.-% an aromatischen Kohlenwasserstoffen, bezogen auf den Speisestrom, verwendet wird.
- Verfahren nach einem der Ansprüche 1 bis 3, dadurch gekennzeichnet, daß der Speisestrom ein Reformatstrom ist.
- Verfahren nach Anspruch 1, dadurch gekennzeichnet, daß der Katalysator 65 bis 80 % Nickel, 10 bis 25 % Silicium, 2 bis 10 % Zirkonium, 0 bis 10 % Aluminium enthält - alle Komponenten als Oxide berechnet und Prozentangaben in Gew.-%, bezogen auf die Gesamtmasse des Katalysators - mit der Maßgabe, daß die Summe aus dem Gehalt an Silicium und Aluminium mindestens 15 % beträgt.
- Verfahren nach Anspruch 4, dadurch gekennzeichnet, daß der Gehalt des Speisestroms an aromatischen Kohlenwasserstoffen vor der Hydrierung durch eine oder mehrere vorgeschaltete Destillations-, Extraktions- und/oder Extraktionsdestillationsstufen erhöht wird.
- Verfahren nach einem der vorstehenden Ansprüche, dadurch gekennzeichnet, daß der Gehalt an aromatischen Kohlenwasserstoffen im entaromatisierten Strom nach der Hydrierung maximal 0,05 Gew.-%, bezogen auf den entaromatisierten Strom, beträgt.
- Verwendung eines entaromatisierten Stromes, wie er nach einem der vorstehenden Ansprüche erhalten wird, als Komponente in Treibstoffen für Ottomotoren.
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
DE19704128 | 1997-02-04 | ||
DE19704128A DE19704128A1 (de) | 1997-02-04 | 1997-02-04 | Verfahren zur hydrierenden Entaromatisierung |
Publications (1)
Publication Number | Publication Date |
---|---|
EP0856572A1 true EP0856572A1 (de) | 1998-08-05 |
Family
ID=7819248
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
EP98101740A Withdrawn EP0856572A1 (de) | 1997-02-04 | 1998-02-02 | Verfahren zur hydrierenden Entaromatisierung |
Country Status (5)
Country | Link |
---|---|
EP (1) | EP0856572A1 (de) |
JP (1) | JPH10330765A (de) |
KR (1) | KR19980071028A (de) |
CN (1) | CN1201772A (de) |
DE (1) | DE19704128A1 (de) |
Families Citing this family (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
CN1190623C (zh) | 2002-10-14 | 2005-02-23 | 吕金龙 | 一种收缩折叠式灯罩 |
Citations (5)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
FR2216342A1 (de) * | 1973-02-02 | 1974-08-30 | Basf Ag | |
US4251394A (en) * | 1978-08-25 | 1981-02-17 | Exxon Research & Engineering Co. | Coprecipitated copper-nickel-silica catalysts, preparation and use thereof |
DE3629631A1 (de) * | 1986-08-30 | 1988-03-03 | Basf Ag | Verfahren zur herstellung von medizinischen weissoelen und medizinischen paraffinen |
EP0290100A1 (de) * | 1987-05-08 | 1988-11-09 | Unilever N.V. | Hydrierungskatalysator |
EP0672452A1 (de) * | 1994-03-15 | 1995-09-20 | BASF Aktiengesellschaft | Nickelhaltige Hydrierkatalysatoren |
-
1997
- 1997-02-04 DE DE19704128A patent/DE19704128A1/de not_active Withdrawn
-
1998
- 1998-02-02 EP EP98101740A patent/EP0856572A1/de not_active Withdrawn
- 1998-02-03 JP JP10022203A patent/JPH10330765A/ja not_active Withdrawn
- 1998-02-03 KR KR1019980002962A patent/KR19980071028A/ko not_active Application Discontinuation
- 1998-02-04 CN CN98106405A patent/CN1201772A/zh active Pending
Patent Citations (5)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
FR2216342A1 (de) * | 1973-02-02 | 1974-08-30 | Basf Ag | |
US4251394A (en) * | 1978-08-25 | 1981-02-17 | Exxon Research & Engineering Co. | Coprecipitated copper-nickel-silica catalysts, preparation and use thereof |
DE3629631A1 (de) * | 1986-08-30 | 1988-03-03 | Basf Ag | Verfahren zur herstellung von medizinischen weissoelen und medizinischen paraffinen |
EP0290100A1 (de) * | 1987-05-08 | 1988-11-09 | Unilever N.V. | Hydrierungskatalysator |
EP0672452A1 (de) * | 1994-03-15 | 1995-09-20 | BASF Aktiengesellschaft | Nickelhaltige Hydrierkatalysatoren |
Also Published As
Publication number | Publication date |
---|---|
DE19704128A1 (de) | 1998-08-06 |
CN1201772A (zh) | 1998-12-16 |
KR19980071028A (ko) | 1998-10-26 |
JPH10330765A (ja) | 1998-12-15 |
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Inventor name: POLANEK, PETER, DR. Inventor name: DILLING, STEPHAN Inventor name: WALTER, MARC, DR. Inventor name: VICARI, MAXIMILIAN, DR. |
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