CN1882521A - Preparation method of branched aliphatic alcohols using combined process streams from a hydrogenation unit and a dehydrogenation-isomerization unit - Google Patents

Abstract

Systems and methods to produced branched aliphatic alcohols are described. Systems may include a hydrogenation unit, a dehydrogenation-isomerization unit, a hydroformylation unit and/or combinations thereof. Methods for producing branched aliphatic alcohols may include isomerization of olefins in a process stream. The isomerized olefins may be hydroformylated to produce aliphatic alcohols. After hydroformylation of the aliphatic alcohols, unreacted components from the hydroformylation process may be separated from the aliphatic alcohols products. The unreacted components from the hydroformylation process may be recycled back into the main process stream or sent to other processing units. Addition of multiple streams to the units may be performed to control reaction conditions in the units.

Description

Use prepares the method for branched aliphatic alcohols from the combined process streams of hydrogenation unit and dehydrogenation-isomerization unit

The cross reference of related application

The application requires the rights and interests of the U.S. Provisional Application No.60/511562 of submission on October 15th, 2003.

Technical field

The present invention relates generally to the System and method for of preparation fatty alcohol.More particularly, embodiment described herein relates to the system and method that uses hydrogenation unit and dehydrogenation-isomerization unit to prepare branched aliphatic alcohols.

Background technology

Fatty alcohol is a kind of important compound, and it can be used for multiple application, perhaps changes into other compound (as tensio-active agent, sulfuric ester).Tensio-active agent can be used for multiple application (as washing composition, soap, recovery of oil).

The structure of fatty alcohol is formed the performance that can influence the tensio-active agent produced by this fatty alcohol and/or washing composition (as water-soluble, biodegradable and cold water washing).The for example water-soluble straight chain degree of the aliphatic series part of fatty alcohol that is subjected to influences.When the straight chain degree of aliphatic series part increased, the wetting ability of the fatty alcohol tensio-active agent avidity of water (promptly to) can descend.Therefore, the water-soluble and/or scourability of fatty alcohol tensio-active agent can descend.Side chain is incorporated into the cold water-soluble and/or the detergency that can increase the fatty alcohol tensio-active agent in the aliphatic series part of fatty alcohol tensio-active agent.Yet if the side chain in the aliphatic series part of fatty alcohol tensio-active agent comprises the quaternary carbon of comparatively high amts, the biological degradability of this fatty alcohol tensio-active agent may reduce.The side chain that introducing has a minimum quantity quaternary carbon can increase the cold water-soluble and/or the detergency of this alcohol tensio-active agent in the aliphatic series part of fatty alcohol tensio-active agent, keeps the biodegradability of this washing composition simultaneously.

The aliphatic series part that is used to prepare the fatty alcohol of tensio-active agent can comprise that one or more aliphatic alkyls are as side chain.The aliphatic alkyl that can form side chain in the aliphatic series part can comprise methyl, ethyl, propyl group or senior alkyl.When aliphatic part branching, may there be quaternary carbon and tertiary carbon.The quantity of quaternary carbon and tertiary carbon may be derived from the branched pattern in the aliphatic series part.Wording as used herein " percent of aliphatic quaternary carbon atoms " is meant the carbon atom that does not have any hydrogen atom of bonding.

The method for preparing branched primary alcohol compositions has been described: people's such as Singleton US 5849960, be entitled as " highly branched primary alcohol compositions and biodegradable washing composition prepared therefrom (Highly Branched Primary Alcohol Compositions, andBiodegradable Detergents Made Therefrom) " in following document; With people's such as Singleton US 6150322, be entitled as " highly branched primary alcohol compositions and biodegradable washing composition prepared therefrom (Highly Branched Primary Alcohol Compositions andBiodegradable Detergents Made Therefrom) ".

Summary of the invention

In one embodiment, can become the method for paraffinic hydrocarbons to produce fatty alcohol by comprising hydrogenated olefins.The raw materials technology logistics that enters hydrogenation unit can comprise that average carbon number is normal olefine and the paraffinic hydrocarbons of 7-18.In one embodiment, the raw materials technology logistics that enters hydrogenation unit can comprise that average carbon number is normal olefine and the paraffinic hydrocarbons of 10-17.Term as used herein " carbon number " is meant intramolecular the total number of carbon atoms.In some embodiments, enter the raw materials technology logistics of hydrogenation unit derived from fischer-tropsch process.

In hydrogenation unit, can be hydrogenated the formation paraffinic hydrocarbons to small part alkene in the feed stream.The logistics of gained paraffinic feed can be fed in the dehydrogenation-isomerization unit.Can be formed alkene by dehydrogenation to the small part paraffinic hydrocarbons in the feed stream.Dehydrogenation-isomerization unit also can make to small part gained alkene with to the small part isomerisation of olefin in the feed stream Already in.The alkene that is produced by dehydrogenation-isomerization unit can be produced fatty alcohol by hydroformylation.Can have the branched aliphatic structure to the small part fatty alcohol.

In dehydrogenation-isomerization unit, in feed stream, can be formed alkene by dehydrogenation to the small part paraffinic hydrocarbons.Already in the alkene in the feed stream also can isomerization in dehydrogenation-isomerization unit to small part gained alkene with to small part.Isomerization process changes into branched olefin with normal olefine (as nonbranched alkene).This isomerizing olefins can be by hydroformylation to produce fatty alcohol.After hydroformylation alkene, from the unreacted components of hydroformylation technology can with the fatty alcohol product separation.Paraffinic hydrocarbons in the logistics after separation and unreacting olefin are capable of circulation to be got back in the dehydrogenation-isomerization unit.

It is about 0.7-2.5 that processing condition in dehydrogenation-isomerization unit can make the average side chain number of each olefin hydrocarbon molecules of gained branched olefin.Branched olefin can include but not limited to methyl and/or ethyl branched olefin.Isomerization process can produce contain less than about 0.5% season the class aliphatic carbon atom branched olefin.Dehydrogenation-isomerization unit can comprise the catalyzer with two kinds of functions: make paraffin dehydrogenation become alkene and make olefin isomerization change into branched olefin.

In one embodiment, dehydrogenation-isomerization unit can comprise a plurality of districts.A plurality of districts can comprise first reaction zone and second reaction zone.First reaction zone can be a dehydrogenation zone.Second reaction zone can be an isomerization zone.The hydrocarbon stream that contains alkene and paraffinic hydrocarbons can enter dehydrogenation zone.Can be dehydrogenated alkene to the small part paraffinic hydrocarbons and produce the logistics be rich in alkene in hydrocarbon stream.The logistics that is rich in alkene can be led in the isomerization zone.In isomerization zone, in being rich in olefin stream, can be isomerizated into branched olefin to small part alkene.Branched olefin can change into fatty alcohol by hydroformylation.After the hydrogenation of olefins formylation, paraffinic hydrocarbons and unreacted olefins stream can with the fatty alcohol product separation that is produced.Can get back in the dehydrogenation-isomerization unit and/or direct in the logistics that enters in the dehydrogenation-isomerization unit by the guiding of near small part paraffinic hydrocarbons and unreacted olefins stream, thus endless chain alkane and unreacted olefins stream.

In one embodiment, dehydrogenation-isomerization unit can comprise stacked bed configuration.Stacking bed dehydrogenation catalyst and the isomerization catalyst that comprises hydrocarbon stream.Can be dehydrogenated alkene to the small part paraffinic hydrocarbons and produce the logistics be rich in alkene in hydrocarbon stream.The logistics that is rich in alkene can be led in the isomerization zone.In isomerization zone, in the rich olefins logistics, can be isomerizated into branched olefin to small part alkene.Branched olefin can change into fatty alcohol by hydroformylation.After the hydrogenation of olefins formylation, paraffinic hydrocarbons and unreacted olefins stream can with the fatty alcohol product separation that is produced.Can get back in the dehydrogenation-isomerization unit and/or direct in the logistics that enters in the dehydrogenation-isomerization unit by the guiding of near small part paraffinic hydrocarbons and unreacted olefins stream, thus endless chain alkane and unreacted olefins stream.

In some embodiments, but sulfation forms aliphatic sulfate to the small part fatty alcohol.In some embodiments, aliphatic sulfate can contain branched-alkyl.

In some embodiments, but to the fatty alcohol alkoxyization that small part produced, the formation alkoxyl alcohol.In some embodiments, alkoxyl alcohol can contain branched-alkyl.In some embodiments, can be formed the branching pentadecanol ethoxylate by ethoxylation to branched aliphatic alcohols that small part produced.But sulfation forms the alkoxyl group sulfuric ester to the small part alkoxyl alcohol.In some embodiments, the alkoxyl group sulfuric ester can contain branched-alkyl.

Description of drawings

Based on the detailed description of following relevant embodiment and with reference to the accompanying drawings, advantage of the present invention will be more obvious to one skilled in the art, wherein:

Fig. 1 has described the system that uses hydrogenation unit and dehydrogenation-isomerization unit to produce fatty alcohol

The synoptic diagram of embodiment.

Thereby Fig. 2 has described the synoptic diagram of the embodiment of the system that uses hydrogenation unit, dehydrogenation-isomerization unit to separate branched olefin and normal olefine and paraffinic hydrocarbons production branched aliphatic alcohols with separating unit.

Fig. 3 A-B has described the synoptic diagram of the embodiment of the system that uses hydrogenation unit and two-region dehydrogenation-isomerization unit to produce branched aliphatic alcohols.

Fig. 3 has described the synoptic diagram that use has the embodiment of the hydrogenation unit of stackeding bed catalyst structure and the system that dehydrogenation-isomerization unit is produced branched aliphatic alcohols.

Although the present invention admits of various improvement and alternative form, show specific embodiments of the present invention by the mode that exemplifies in the accompanying drawings, and will describe these specific embodiments in detail at this.Be to be understood that accompanying drawing and describe in detail not to be intended to limit the invention to disclosed particular form that on the contrary, the present invention covers spirit of the present invention and interior all improvement, equivalence and the alternative form of scope that drops on the claims definition.

Embodiment

Can use fischer-tropsch process by the synthetic hydrocarbon product of synthetic gas (being the mixture of hydrogen and carbon monoxide).Can be by partial combustion oil (as coal, hydrocarbon), by the reformation Sweet natural gas or by the partial oxidation Sweet natural gas, thus derive the acquisition synthetic gas.Fischer-tropsch process is catalytically converted into synthetic gas the product mixture that contains stable hydrocarbon, unsaturated hydrocarbons and a small amount of oxygenated products.Can use products production fuel (as gasoline, diesel oil), lubricating oil and wax from fischer-tropsch process.

Also can use the fischer-tropsch process-stream to prepare the commercial product of economically valuable.For example normal olefine is the commercial product that can be used for producing tensio-active agent.Use the part process-stream to produce the economic worth that normal olefine can increase the fischer-tropsch process logistics.

Tensio-active agent derived from branched olefin can have the performance that is different from derived from the tensio-active agent of normal olefine.For example compare, can have solubleness and/or improved scourability in the water of increase derived from the tensio-active agent of branched olefin with tensio-active agent derived from normal olefine.Yet, the biodegradable performance of tensio-active agent can be subjected to the branching partial memory of tensio-active agent the quaternary carbon atom influence.By the tensio-active agent of the branched olefin of quaternary carbon atom preparation with minimum quantity can have with by the similar biodegradable energy of normal olefine deutero-tensio-active agent.Produce the economic worth that branched olefin can increase this logistics by the fischer-tropsch process logistics.In some embodiments, can use isomerization catalyst that normal olefine is changed into the branched olefin that quaternary carbon atom is counted minimum.Increase can be increased the economic worth of this process-stream by the content of fischer-tropsch process logistics deutero-branched olefin.

Increase the method that increases the economic worth of this process-stream by the process-stream deutero-branched olefin amount that contains a certain amount of alkene thereby below described.This method can be used for the product stream in other source of fischer-tropsch process logistics and hydrocarbonaceous.

The hydrocarbon feed stream composition can comprise paraffinic hydrocarbons and alkene.To the small part hydrocarbon stream can be by having at least 4 carbon atoms and the linear paraffins and the alkene of 18 carbon atoms are formed at the most.Can obtain hydrocarbon feed stream by fischer-tropsch process or by ethylene oligomerization technology.Can select Fischer-Tropsch catalyst and reaction conditions, the specific mixture of product is provided in reaction product stream.For example can select Fischer-Tropsch catalyst and reaction conditions, to increase the content of logistics internal olefin content and reduction paraffinic hydrocarbons and oxygenate.Perhaps, but selecting catalyst and reaction conditions, with the content that increases paraffinic hydrocarbons in the logistics and reduce alkene and the content of oxygenate.

Employed catalyzer can be Mo, W, group VIII compound or its combination in fischer-tropsch process.The group VIII compound includes but not limited to iron, cobalt, ruthenium, rhodium, platinum, palladium, iridium and osmium.Can prepare Mo, W and group VIII compound compositions with the free metal form.In some embodiments, Mo, W and group VIII compound compositions can form alloy.In some embodiments, Mo, W and group VIII compound compositions can form oxide compound, carbide or other compound.In other embodiments, Mo, W and group VIII compound compositions can form salt.Iron-based and cobalt-base catalyst are at the industrial Fischer-Tropsch catalyst that is used as.Ruthenium catalyst tends to be beneficial to the dystectic waxy substance of formation under condition of high voltage.Synthetic Fischer-Tropsch catalyst can comprise molten pig.In some embodiments, the molten pig Fischer-Tropsch catalyst can comprise promotor (as potassium on silica supports, alumina supporter or silica-alumina carriers or oxide compound).Also can in Fischer-Tropsch catalyst, use the cobalt metal.Under the situation of the combination of selecting carrier, promotor and other metal suitably, can reconcile the composition of cobalt catalyst with the required hydrocarbon materials of preparation enrichment.Other catalyzer for example iron-cobalt alloy-catalyst is known because of its selectivity of producing alkene.The catalyzer and the composition that prepare hydrocarbon materials by fischer-tropsch process are normally known.

Although reference is the fischer-tropsch logistics, any logistics of alkene and stable hydrocarbon all may be suitable.Multiple fischer-tropsch logistics can contain the alkene of 5-80%, and all the other are the stable hydrocarbon that contain paraffinic hydrocarbons and other compound.

In some embodiments, by cracking paraffin or olefin oligomerization, obtain to contain the feed stream of alkene and paraffinic hydrocarbons.Commercial olefin product by the ethylene oligomerization preparation is commercially available by Chevron Phillips Chemical Company, Shell Chemical Company (with NEODENE ) and British Petroleum in the U.S..In following document, described by cracking paraffin produce alpha-olefin and paraffinic feed logistics: Sie US 4579986, be entitled as " method (Process For The Preparation Of Hydrocarbon s) for preparing hydrocarbon "; With people's such as Ansorge U.S. Patent application No.10/153955, be entitled as " preparing the method for normal olefine and the purposes that described normal olefine prepares straight chain alcohol (Process For ThePreparation of linear Olefins and Use Thereof To Prepare LinearAlcohols) ".In following document, described the detailed process for preparing normal olefine by ethene: Mason US 3676523, be entitled as " preparation of alpha-olefin (Alpha-OlefinProduction) "; The US 3686351 of Mason, be entitled as " preparation of alpha-olefin (Alpha-Olefin Production) "; The US 3737475 of Mason, be entitled as people such as " preparation of alpha-olefin (Alpha-Olefin Production) " and Kister US 4020121, be entitled as " oligomerization system (Oligomerization Reaction System) ".Most of above-mentioned technologies are all produced alpha-olefin.The industrial more high-grade linear internal (as the chloro dechlorination of paraffinic hydrocarbons, the dehydrogenation of paraffinic hydrocarbons, the isomerization of alpha-olefin) of producing.

In one embodiment, handle feed stream and produce the hydrocarbon stream that contains branched olefin.Can use various technology that these branched olefins are changed into branched aliphatic alcohols.Feed stream can have the paraffinicity of scope between about 50-90wt% of feed stream.In some embodiments, feed stream can have the paraffinicity greater than about 90wt% paraffinic hydrocarbons.This feed stream also can comprise alkene.Olefin(e) centent can be between about 10-50wt% in the feed stream.In other embodiments, the olefin(e) centent of feed stream can be greater than 90wt% alkene.

The composition of feed stream can comprise that the average carbon number scope is the hydrocarbon of 4-30.In one embodiment, the average carbon number scope of the hydrocarbon in feed stream can be 4-24.In other embodiments, the average carbon number scope in feed stream can be 4-18.The average carbon number scope of the hydrocarbon in feed stream can be 7-18.In some embodiments, the average carbon number scope of the hydrocarbon in feed stream can be 10-17.In some embodiments, the average carbon number scope of the hydrocarbon in feed stream can be 10-13.In other embodiments, the average carbon number scope of the hydrocarbon in feed stream can be 14-17.

Branched-chain alkene can change into branched aliphatic alcohol (as branched-chain primary alcohol) by hydroformylation technology." hydroformylation " as used herein is meant by carbonylation and hydrogenation process by olefin production alcohol.Can use other technology by the olefin production fatty alcohol.Example by other technology of olefin production fatty alcohol includes but not limited to hydration, oxidation and hydrolysis, sulfation and hydration and epoxidation and hydration.The composition of alcohol product stream can comprise that the average carbon number scope is the fatty alcohol of 5-31.In one embodiment, the average carbon number scope of fatty alcohol can be 7-20 in the pure product stream.In some embodiments, the average carbon number scope of fatty alcohol can be 11-18 in the pure product stream.In some embodiments, the average carbon number scope of fatty alcohol can be 11-14 in the pure product stream.In other embodiments, the average carbon number scope of fatty alcohol can be 15-18 in the pure product stream.

In some embodiments, first hydrocarbon stream can contain undesired compound (as oxygenate and diolefine), and these undesired compounds can reduce the catalyst selectivity of producing in the employed technology of fatty alcohol.Can remove undesired compound by hydrogenation first hydrocarbon stream.In some embodiments, the hydrogenation of first hydrocarbon stream can produce the hydrocarbon stream that contains greater than about 90% paraffinic hydrocarbons.But the dehydrogenation of hydrogenant hydrocarbon stream produces the alkenes logistics.The position of employed catalyzer may command olefinic double bonds in dehydrogenating technology.In some embodiments, the alkenes logistics can comprise that wherein the alkene greater than 70% is the alkene of the alpha-olefin of straight chain carbon skeleton structure.In other embodiments, the alkenes logistics can comprise can being the alkene of internal olefin more than or equal to 50% existing olefin hydrocarbon molecules wherein.

As among Fig. 1 at shown in the system 100, can first hydrocarbon stream be incorporated in the hydrogenation unit 110 by first pipeline 112.First hydrocarbon stream comprises alkene and paraffinic hydrocarbons.In hydrogenation unit 110, in first hydrocarbon stream, can be hydrogenated to paraffinic hydrocarbons to small part alkene, produce second hydrocarbon stream.

Reaction conditions in the may command hydrogenation unit 110 makes alkene and diolefine hydrogenation and removes oxygenate.The operating temperature range of hydrogenation unit 110 can be about 100-300 ℃.In some embodiments, operating temperature range can be about 150-275 ℃.In other embodiments, operating temperature range can be about 175-250 ℃.The working pressure scope can be about 5atm (506kPa)-150atm (1520kPa).In some embodiments, the working pressure scope can be about 10atm (1013kPa)-50atm (5065kPa).

Can use the catalyst bed structure (as fluidized-bed, moving-bed, slurry phase bed or fixed bed) of any kind to carry out hydrogenation process.In some embodiments, can use fixed-bed structure.In fixed bed system, hydrogen can be fed in the hydrogenation section with the gas hourly space velocity that about 100 standards rise gas/rise catalyzer/hour (NL/L/hr)-1000NL/L/hr.In some embodiments, with the gas hourly space velocity supply of hydrogen of about 250-5000NL/L/hr." rising gas/rise catalyzer/hour be the gas space velocity of unit representation with standard " as used herein is the volume (unit liter) of gas under the standard conditions of 0 ℃ and 760mmHg.

Hydrogenation catalyst is normally known and can be commercially available by a large amount of compositions.In some embodiments, hydrogenation catalyst can comprise the VIB of the periodic table of elements and one or more metals of VII family.In some embodiments, metal can include but not limited to molybdenum, tungsten, cobalt, nickel, ruthenium, iridium, osmium, platinum and palladium.Hydrogenation catalyst can comprise that refractory oxide or silicate are as tackiness agent.

Hydrogenation condition and catalyzer are disclosed in following document: people's such as Eilers EP0583836, be entitled as " method (Process For The Preparation ofHydrocarbon Fuels) for preparing hydrocarbon fuel "; With people's such as Eilers EP 0668342, be entitled as " preparation method of lubricating base oil (Lubricating Base Oi1 Preparation Process) ".Hydrogenation condition and catalyzer are also disclosed in following document: people's such as Gosselink US5371308, be entitled as " preparation method of light alkene (Process For The PreparationOf Lower Olefins) ".

In some embodiments, second hydrocarbon stream that contains paraffinic hydrocarbons and alkene can be incorporated in the dehydrogenation-isomerization unit.Dehydrogenation-isomerization unit alternative two independently unit (as isomerization unit and dehydrogenation unit).Dehydrogenation-isomerization unit can make paraffin dehydrogenation become alkene and isomerization gained alkene and/or be present in the interior initial alkene of hydrocarbon stream and become branched olefin.In one embodiment, catalyzer can be with the hydrocarbon dehydrogenation-isomerization in second hydrocarbon stream.In some embodiments, catalyzer can be a single catalyst.In some embodiments, catalyzer can be the mixture of two kinds of catalyzer (as dehydrogenation catalyst and isomerization catalyst).In other embodiments, be positioned at the not same district of a dehydrogenation-isomerization unit or two kinds of independent catalyzer of stacked bed configuration and can carry out the dehydroisomerization metallization processes." dehydrogenation-isomerization catalyzer " as used herein can be one or more catalyzer.

In some embodiments, dehydrogenation-isomerization unit can have several entrances of admitting the different process logistics.Process-stream can come from other processing unit and/or storage element.The example of process-stream includes but not limited to the thinner hydrocarbon stream and/or derived from other hydrocarbon stream that contains alkene and paraffinic hydrocarbons of other technology." entering in the dehydrogenation-isomerization unit " as used herein is meant that process-stream enters in the dehydrogenation-isomerization unit by one or more entrances.

Second hydrocarbon stream that contains the mixture of alkene and paraffinic hydrocarbons can be incorporated in the dehydrogenation-isomerization unit 114 by second pipeline 116.In dehydrogenation-isomerization unit 114, in second hydrocarbon stream, can be hydrogenated to alkene to the small part paraffinic hydrocarbons.But isomerization is to small part gained alkene with to the small part alkene in the feed stream Already in, to produce the 3rd hydrocarbon stream.Isomerization process changes into branched-chain alkene with normal olefine (being nonbranched alkene).

The catalyzer that is used for dehydrogenation-isomerization second hydrocarbon stream can be based on the zeolite catalyst with one or more metals or metallic compound modification.In dehydrogenation-isomerization unit 114, handle in second hydrocarbon stream the employed catalyzer of alkene effectively the normal olefine in the Skeletal Isomerization Process logistics become alkene, the average side chain number of each olefin hydrocarbon molecules chain of described alkene is greater than about 0.7.In some embodiments, the average side chain scope of counting of each olefin hydrocarbon molecules chain can be about 0.7-2.5.In some embodiments, the average side chain scope of counting of each olefin hydrocarbon molecules chain can be about 0.7-2.2.In other embodiments, the average side chain scope of counting of each olefin hydrocarbon molecules chain can be about 1.0-2.2.

The dehydrogenation-isomerization catalyzer can contain and has at least one crystallography free access diameter greater than about 4.2 dusts and less than the zeolite of the passage of about 7 dusts (at room temperature measure)." channel diameter or size " as used herein is meant effective channel diameter or the size that is used to spread.May there be the passage of free access diameter greater than about 7 dusts in this zeolite.This catalyzer can contain the free diameter of at least one crystallography at the feeder connection place greater than about 4.2 dusts and less than the passage of about 7 dusts.This catalyzer may not have the passage that surpasses these range limit 7 dusts at the ingress diameter.Have diameter and can be easy to generate undesirable alkene byproduct (as aromizing, low dimerization, alkylation, coking) greater than the zeolite of the passage of about 7 dusts.In some embodiments, zeolite may not contain along the passage of the free diameter of x or y plane greater than about 4.2 dusts.Little channel size can prevent to diffuse into and/or diffuse out access opening after alkene is by branching.Zeolite can have the free diameter range of at least one passage greater than about 4.2 dusts and less than the passage of about 7 dusts.

In one embodiment, olefin hydrocarbon molecules is because the other end that its high carbon chain lengths causes entering zeolite channels internal diffusion process and leaves passage.When alkene when the zeolite, the theoretical branching speed that observed branching speed may be when each olefin hydrocarbon molecules of supposition all passes passage is not corresponding.Most of alkene can partly permeate by passage, and its penetration distance is the chain portion of branching in passage effectively, draws from this passage after isomerization subsequently.In the embodiment of producing the fatty alcohol method, the olefin hydrocarbon molecules in hydrocarbon stream can mainly have the terminal branching of alkene carbon backbone chain and towards minute subcenter be substantially straight chain structure (as at the carbon at center at least 25% not by branching).

In some embodiments, the zeolite catalyst structure can contain along the x of [001] view and two free diameters in plane of y greater than about 4.2 dusts and less than the passage of about 7 dusts.Zeolite with regulation channel size can be called as intermediate value or center-aisle zeolite, and (or folding 12-T unit) encircles channel architecture and have the ring channel architecture (if any) that is less than or equal to 9-T unit (aperture) in another view typically to have 10-T unit in a view.To the number of channels in the zeolite or orientation (as intersection or interconnection at any angle parallel, non-interconnection) without limits.

Channel size is that the example of the zeolite of about 4.2 dusts-7.0 dust comprises molecular sieve, ferrierite, A1PO-31, SAPO-11, SAPO-31, SAPO-41, FU-9, NU-10, NU-23, ZSM-12, ZSM-22, ZSM-23, ZSM-35, ZSM-48, ZSM-50, ZSM-57, SUZ-4A, MeAPO-11, MeAPO-31, MeAPO-41, MeAPSO-11, MeAPSO-31 and MeAPSO-41, MeAPSO-46, ELAPO-11, ELAPO-31, ELAPO-41, ELAPSO-11, ELAPSO-31 and ELAPSO-41, lomontite, cancrinite, offretite, the Hydrogen stilbite, magnesium or calcium type mordenite and handkerchief water chalcomorphite.The homologous structure of the zeolite framework of known other title can be regarded as of equal value.By people such as Flanigen at New Developments in Zeolite ScienceTechnology, 1986, Kodansha Ltd. has described the skeleton of zeolite in " the AluminophosphateMolecular Sieves and the Periodic Table " of Tokyo Japan.

Multiple natural zeolite, for example the feature of ferrierite, heulandite and stilbite can be hole dimension diameter for or be slightly less than the one dimension pore structure of about 4.2 dusts.In following document, described the passage in the natural zeolite has been changed into method than major path: the US 4795623 of Evans, be entitled as " the time efficient method (Time Effective Method ForPreparing Ferrierite) of preparation ferrierite "; With the US 4942027 of Evans, be entitled as " method (Method for Preparing Ferrierite) for preparing ferrierite ".Can remove associating basic metal or alkaline-earth metal by common known method (as ammonium ion exchange, carry out roasting after optional, obtain being substantially the zeolite of Hydrogen), the passage in the natural zeolite is changed into have required zeolite than the major path size.Can enlarge channel diameter with alternative associating basic metal of Hydrogen or alkaline-earth metal.In some embodiments, natural zeolite (as the mordenite of some form) can have the channel size greater than 7 dusts.Can reduce channel size by substituting bigger ion (as bigger alkaline-earth metal) with basic metal.

In some embodiments, zeolite can have the isotypic framework structure of ferrierite.The outstanding constitutional features of the ferrierite of finding by the x-radiocrystallography may be at the intraskeletal parallel channels of silico-aluminate.Parallel channels can have elliptic cross-section.Zeolite with ferrierite isotypic framework structure has been described: people's such as Seddon EP 55529, be entitled as " zeolite (Zeolites) " in following document; With the EP 103981 of Whittam, be entitled as " zeolite (Zeolites) ".Zeolite with ferrierite homotype skeleton has also been described: people's such as Plank US 4016245, be entitled as " method (Process For PreparingA Crystalline Aluminosilicate) for preparing crystal aluminosilicate " in following document; People's such as Morimoto US 4578259, be entitled as " crystalline zeolite and preparation method thereof (Crystalline Zeolite And Method OfPreparing Same) "; With people's such as Young US 4375573, be entitled as " with the selectivity preparation and the reaction (Selective Production AndReaction of P-Disubstituted Aromatics Over Zeolite ZSM-48) of the dibasic aromatic hydrocarbons of zeolite ZSM-48 contraposition ".

In one embodiment, Hydrogen ferrierite (H-ferrierite) can be regarded as unidimensional basically.The H-ferrierite can have the passage of runs parallel.The H-ferrierite has the oval-shaped passageway that free diameter is 4.2 dusts * 5.4 dusts along the x and the y plane of [001] view.This passage can be enough big, so that the permission normal olefine enters and the isoolefine of methyl-branched spreads through this passage or diffuse out this passage.This passage can form to postpone coke enough for a short time.The method for preparing various H-ferrierites has been described: people's such as Pasquale US5985238, be entitled as " method (Process For PreparingFerrierite) for preparing ferrierite " in following document; People's such as Nanne US 4251499, be entitled as " method (Process For The Preparation of Ferrierite) for preparing ferrierite "; The US4795623 of Evans, be entitled as the time efficient method (Time EffectiveMethod For Preparing Ferrierite) of ferrierite " preparation "; With the US 4942027 of Evans, be entitled as " method (Method For Preparing Ferrierite) for preparing ferrierite ".

In some embodiments, the dehydrogenation-isomerization catalyzer can make up with the refractory oxide that serves as adhesive material.Suitable refractory oxide includes but not limited to natural clay (as wilkinite, montmorillonite, attapulgite and kaolin), aluminum oxide, silicon-dioxide, silica-alumina, hydrated aluminum oxide, titanium oxide, zirconium white or its mixture.

The example of alumina adhesive can include but not limited to pseudobochmite, γ and bayerite alumina.Alumina adhesive can be commercially available (as the VERSAL  aluminum oxide of LaRoche Chemicals preparation and the CATAPAL  aluminum oxide of Sasol preparation).In one embodiment, when extruding the preparation catalyzer, the alumina powder of high degree of dispersion can be used as alumina adhesive.The alumina powder of high degree of dispersion has the dispersity greater than 50% in acid content is the aqueous acidic dispersion liquid of 0.4mg angelic acid (acetate)/g powder.The aluminum oxide of this high degree of dispersion can be by the CATAPAL  aluminum oxide of Sasol preparation as an example.

The weight ratio scope of zeolite and adhesive material can be about 10: 90 to about 99.5: 0.5.In some embodiments, this weight ratio scope can be about 75: 25 to about 99: 1.In other embodiments, the weight ratio scope of zeolite and adhesive material can be about 80: 20 to about 98: 2.In some embodiments, the weight ratio scope of zeolite and adhesive material can be about 85: 15 to about 95: 5.

In some embodiments, can adopt one or more monocarboxylic acids and/or mineral acid to prepare the dehydrogenation-isomerization catalyzer.Except monocarboxylic acid and/or mineral acid, also can use at least a organic acid (" poly carboxylic acid ") with at least two carboxylic acid groups.Monocarboxylic acid can have replacement or the unsubstituted alkyl that contains 1-20 carbon atom.Alkyl can be aliphatic series, ring-type or aromatic hydrocarbyl.Example with monocarboxylic acid of 1-20 carbon atom includes but not limited to acetate, formic acid, propionic acid, butyric acid, caproic acid, oxyacetic acid, lactic acid, hydroxybutyric acid, hydroxycyclopent acid, Whitfield's ointment, amygdalic acid, phenylformic acid and lipid acid.Representative examples of mineral pigments includes but not limited to nitric acid, phosphoric acid, sulfuric acid and hydrochloric acid.

In some embodiments, poly carboxylic acid can be to have two or more organic acids that are connected to the carboxylic acid group on the hydrocarbon fragment by carbon-carbon bond.This connection can be on the segmental any part of hydrocarbon.Poly carboxylic acid can have the hydrocarbon fragment less than 10 carbon atoms.The hydrocarbon fragment can be aliphatic series, ring-type or aromatic hydrocarbon fragment.For having two oxalic acid by the carboxylic acid group of carbon-carbon bond connection, the hydrocarbon fragment can have 0 carbon atom.Polycarboxylic example includes but not limited to tartrate, citric acid, oxysuccinic acid, oxalic acid, hexanodioic acid, propanedioic acid, tetrahydroxyadipic acid, 1,2-ring pentane dicarboxylic acid, toxilic acid, fumaric acid, methylene-succinic acid, phthalic acid, terephthalic acid, phenylmalonic acid, hydroxyl phthalic, Dihydroxyfumaric acid, tricarballylic acid, benzene-1,3,5-tricarboxylic acid, isocitric acid, glactaric acid and saccharic acid.Poly carboxylic acid can be any isomer of above-mentioned acid.In some embodiments, poly carboxylic acid can be any stereoisomer of above-mentioned acid.In one embodiment, can use poly carboxylic acid with at least two carboxylic acid groups and at least one hydroxyl.In one embodiment, citric acid, tartrate and oxysuccinic acid can be used as poly carboxylic acid.

Be incorporated into metal in the dehydrogenation-isomerization catalyzer and can be under in the presence of oxygen promotion coke oxidation and make the metal of paraffin dehydrogenation greater than about 250 ℃ temperature." metal " as used herein is the nulling oxidation state and/or the metal of high oxidation state (as metal oxide) more." coke " as used herein is meant by the product of more macromolecular thermal destruction one-tenth than small molecules.

Employed metal can be transition metal and rare earth metal in the dehydrogenation-isomerization catalyzer.The metal of promotion coke oxidation includes but not limited to transition metal and/or its combination of periodictable IB, VB, VIB, VIIB, VIII family.In some embodiments, can in the dehydrogenation-isomerization catalyzer, use Pd, Pt, Ni, Co, Mn, Ag, Cr and/or its combination.In other embodiments, metal oxide is such as but not limited to the compound of oxidation coke in chromic oxide, ferric oxide, precious metal or its mixture useful as catalysts.

The amount of metal scope of being introduced can for about 5/1000000ths parts (" ppm ") to about 15wt%.In some embodiments, the amount ranges of metal can for about 5ppm to about 10wt%.In some embodiments, the amount ranges of metal can for about 5ppm to about 5wt%.

With other metallographic phase ratio that is incorporated in zeolite and/or the tackiness agent, precious metal (as platinum and/or palladium) can use with less metal consumption." precious metal " as used herein is meant the metal that comprises platinum, palladium, iridium, ruthenium, osmium and rhodium.In some embodiments, the amount ranges of precious metal is benchmark with the metal, and about 5ppm that can be final catalyzer is to about 2wt%.In some embodiments, the amount ranges of precious metal is benchmark with the metal, can be about 5-1000ppm of final catalyzer.In other embodiments, the amount ranges of precious metal is benchmark with the metal, can be about 5-3000ppm of final catalyzer.In some embodiments, the amount ranges of employed precious metal is benchmark with the metal in the dehydrogenation-isomerization catalyzer, can be about 5-2000ppm of final catalyzer.Be enough to promote to regenerate and do not have the noble metal dosage scope of deterioration catalyst performance can be about 30-100ppm.The platinum of higher dosage and/or palladium (as greater than about 2wt%) can have negative impact to catalyzer (as isomerization activity, the selectivity of work-ing life, alkene).

In one embodiment, can mix one or more metallic compounds in (as grinding) zeolite powder and alumina powder and water and the catalyzer.The gained mixture can form pellet.Compare with the catalyzer for preparing by dipping, can have superior isomerisation of olefin performance by the catalyzer that grinds preparation.Term as used herein " grinding " is meant that mixing wherein adds the powder of enough water, forms the heavy-gravity paste and wherein mixes to be accompanied by and shear paste simultaneously.Can use commercially available shredder, for example Lancaster Mix Muller and Simpson Mix Muller.

In some embodiments, can be by extruding the formation pellet.One or more peptization acid (as nitric acid, acetate, citric acid or its mixture) can join in this mixture, and can use optional extrusion aid, derivatived cellulose (as METHOCEL  F4M, i.e. Vltra tears is by Dow Chemical Company preparation) for example.Can determine the consumption of employed peptization acid by normal experiment, to provide plasticity extrudable material.Term as used herein " pellet " is meant the cementing material of Any shape or form.

In some embodiments, for example platinum and/or palladium can join in the zeolite catalyst after granulation precious metal.Can use common metal introducing method well known by persons skilled in the art (as dipping, precious metal ion exchange and grinding altogether), produce the effective catalyst that can be used for the dehydrogenation-isomerization paraffinic hydrocarbons.But add the dehydrogenation reaction of precious metal auxiliary chain alkane in the catalyzer.Can be at the content of reduction is produced in dehydrogenation-isomerization unit season class aliphatic carbons.Alkene ¹H NMR analyzes the isomerisation degree that can show at the hydrocarbon stream internal olefin. ¹H NMR analyzes the alkene structures that can distinguish wide region.

In one embodiment, in each olefin hydrocarbon molecules, a chain average that is present in the branched olefin compositions that is produced can be greater than 0.7.In some embodiments, in each olefin hydrocarbon molecules, a chain average that is present in the branched olefin compositions is about 0.7-2.5.In some embodiments, in each olefin hydrocarbon molecules, a chain average that is present in the branched olefin compositions is about 0.7-2.2.In some embodiments, in each olefin hydrocarbon molecules, a chain average that is present in the branched olefin compositions is about 1.0-2.2.Can be by being controlled at applied processing condition in the dehydrogenation-isomerization unit, the degree of branching of control product.For example high reaction temperature and lower material flow can cause the higher degree of branching.Methyl branch can account for about 20-99% of the total number of branches that exists in the olefin hydrocarbon molecules.In some embodiments, methyl branch can account for total number of branches in the olefin hydrocarbon molecules greater than about 50%.In some embodiments, the ethyl branch number in olefin hydrocarbon molecules can account for total number of branches less than about 30%.In other embodiments, ethyl branch (if the words that exist) number can be about 0.1-2% of total number of branches.Side chain except methyl or ethyl (if the words that exist) can be less than about 10% of total number of branches.

The percent of aliphatic quaternary carbon atoms that is present in the branched olefin compositions can be less than about 2% of existing carbon atom.In one embodiment, existing percent of aliphatic quaternary carbon atoms number is less than about 1% of existing carbon atom.For biological degradability important use wherein, the percent of aliphatic quaternary carbon atoms number can be less than about 0.5% of existing carbon atom.In one embodiment, the percent of aliphatic quaternary carbon atoms number is less than about 0.3% of existing carbon atom.In other embodiments, the percent of aliphatic quaternary carbon atoms number that exists in branched olefin compositions is about 0.01-0.3% of existing carbon atom.

The 3rd hydrocarbon stream can and be transferred in other processing unit (for example hydroformylation unit, separating unit, alkylation) by the 3rd pipeline 118 outflow dehydrogenation-isomerization units 114.Can flow out dehydrogenation-isomerization units 114 and be incorporated in the hydroformylation unit 120 by the 3rd pipeline 118 to small part the 3rd hydrocarbon stream.In hydroformylation unit 120, in the 3rd hydrocarbon stream, can change into alcohol to small part alkene.Can form the hydroformylation reaction logistics to the small part unreacted components to pure and mild the 3rd hydrocarbon stream that small part produced.Roasting contains the pellet of precious metal in 250-700 ℃ the temperature range.In some embodiments, the maturing temperature scope can be about 300-600 ℃.In some embodiments, the maturing temperature scope can be about 450-525 ℃.

Can be in dehydrogenation-isomerization unit 114, making to become alkene to the small part paraffin dehydrogenation and make to the various conditions of small part gained isomerisation of olefin, the dehydrogenation-isomerization catalyzer is contacted with second hydrocarbon stream.In dehydrogenation-isomerization unit 114, range of reaction temperature can be about 300-700 ℃.In some embodiments, range of reaction temperature can be about 350-550 ℃.The total pressure scope of dehydrogenation-isomerization unit 114 can be about 0.010atm (1kPa)-25.0atm (2534kPa) in reaction process.In one embodiment, the total pressure scope of dehydrogenation-isomerization unit 114 can be about 0.010atm (1kPa)-15.0atm (1520kPa) in reaction process.In other embodiments, the total pressure scope of dehydrogenation-isomerization unit 114 can be about latm (101kPa)-5.0atm (507kPa) in reaction process.In order to prevent coking, can be with hydrogen with the second hydrocarbon stream charging.Can be feed hydrogen and paraffinic hydrocarbons under about 0.1-20 in hydrogen and the molar ratio range that is present in the paraffinic hydrocarbons in second hydrocarbon stream.In some embodiments, the molar ratio range of hydrogen and paraffinic hydrocarbons can be about 1-10.

Can select the residence time in the dehydrogenation-isomerization unit 114, so that paraffin conversion becomes the conversion of olefines rate can keep below 40mol%.In one embodiment, the transformation efficiency scope is 5-30mol%.By keeping low transformation efficiency, but minimum side reactions (as the formation and the cyclization of diene).Can increase olefin conversion by changing reaction conditions (as temperature, the residence time), as long as keep side reaction to be lower than the acceptable limit.Compare with the paraffinic feed that arrives dehydrogenation-isomerization unit, the alkene that is produced in dehydrogenation-isomerization unit 114 can have the higher degree of branching.Should be appreciated that the concentration of olefin that is produced by dehydrogenation-isomerization unit 114 can be subjected to alkene and the thermodynamics equilibrium limit of paraffinic hydrocarbons under temperature of reaction.Can be controlled in the isomerisation of olefin condition in the dehydrogenation-isomerization unit 114, so that the carbonatoms before isomerisation conditions and afterwards in the alkene is basic identical.

The branched olefin that produces in dehydrogenation-isomerization unit 114 can comprise methyl, ethyl and/or longer carbon chain branches.Can carry out the isomerizing olefins composition hydrogen nuclear magnetic resonance ( ¹H NMR) analyzes.Branched olefin can comprise season and/or uncle's aliphatic carbons.In some embodiments, can minimum close.Combined stream can enter in the hydrogenation unit 110 by first pipeline 112, continues this technology, to produce fatty alcohol.In some embodiments, normal olefine and paraffin stream can be introduced directly in the hydrogenation unit 110.

Can be delivered to the logistics of small part branched olefin by branched olefin pipeline 128, and in other treating processes, use and/or storage on the spot.In some embodiments, can flow out separating units 122 and be incorporated in the 3rd pipeline 118 by branched olefin pipeline 128 to the logistics of small part branched olefin.In other embodiments, can flow out separating unit 122 and be introduced directly in the hydroformylation unit to the logistics of small part branched olefin.

Can and enter in the hydroformylation unit 120 by the 3rd pipeline 118 outflow dehydrogenation-isomerization units with reference to figure 1, the three hydrocarbon stream.Hydroformylation unit 120 can have several entrances of admitting additional process-stream to introduce." entering the unitary logistics of hydroformylation " as used herein is defined as process-stream and enters in the hydroformylation unit by one or more entrances.The example of this process-stream includes but not limited to the additional logistics, thinner hydrocarbon stream from dehydrogenation-isomerization unit 114, the gas that contains alkene and paraffinic hydrocarbons and/or other hydrocarbon stream that is obtained by other technology.

In hydroformylation technology,,, conversion of olefines is become aldehyde, alcohol or its combination by making to small part alkene and carbon monoxide and hydrogen reaction according to oxidizing process (Oxo process)." oxidizing process " as used herein is meant in the presence of metal catalyst (as cobalt catalyst), and alkene and carbon monoxide and hydrogen reaction produce to contain than raw material olefin and Duo the alcohol of a carbon atom.In other hydroformylation technology, use " improved oxidizing process "." improved oxidizing process " as used herein is meant and uses phosphine, phosphorous acid ester, arsine or the cobalt of pyridine ligand modification or the oxidizing process of rhodium catalyst.In following document, described modified oxidized Preparation of catalysts and use: Slaugh US 3231621, be entitled as " catalytic hydroformylation reaction speed of response (Reaction Rates In Catalytic Hydroformylation) "; People's such as Slaugh US 3239566, be entitled as " hydrogenation of olefins formylation (Hydroformylation OfOlefins) "; People's such as Slaugh US 3239569, be entitled as " hydrogenation of olefins formylation (Hydroformylation Of Olefins) "; People's such as Slaugh US 3239570, be entitled as " hydrogenation of olefins formylation (Hydroformylation Of Olefins) "; People's such as Slaugh US 3239571, be entitled as " hydrogenation of olefins formylation (Hydroformylation Of

In one embodiment, optionally can from the 3rd hydrocarbon stream, separate alkene by this area common known technology (as distillation, molecular sieve, extraction, absorption, adsorption/desorption and/or film).Be separated to small part branched olefin and normal olefine and paraffinic hydrocarbons and can increase the concentration that enters the branched olefin in the hydroformylation unit.In addition, be separated to the ratio that small part branched olefin and normal olefine and paraffinic hydrocarbons can influence the straight chain that produced in the hydroformylation unit and branched-chain alkene.

Can be with reference to figure 2, the three hydrocarbon streams by separating pipeline 124 outflow dehydrogenation-isomerization units 114 and entering in the separating unit 122.Separating unit 122 can produce two logistics at least: branched olefin logistics and normal olefine and paraffin stream.In separating unit 122, the 3rd hydrocarbon stream can be used for branched olefin and/or normal olefine and contact with the organic and/or inorganic molecule sieve (as zeolite or urea) in the appropriate aperture of paraffinic hydrocarbons with having.Subsequently, desorb from molecular sieve (as solvent desorption) can produce at least two logistics (as branched olefin logistics and normal olefine and paraffin stream) to the small part branched olefin and/or to small part normal olefine and paraffinic hydrocarbons.

Separating unit 122 can comprise that the fixed bed that contains sorbent material is used to separate the 3rd hydrocarbon stream, to produce branched olefin and paraffin stream and normal olefine and paraffin stream.Separation temperature scope in the separating unit 122 can be about 100-400 ℃.In some embodiments, the separation temperature scope can be about 180-380 ℃.Can in the pressure range of about 2atm (202kPa)-7atm (710kPa), carry out the separation in the separating unit 122.In some embodiments, can carry out the pre-treatment of the 3rd hydrocarbon stream, poison to prevent sorbent material.The example of adsorption/desorption technology be to use Sorbex  isolation technique Molex technology (UOP technology, UOP, Des Plaines, IL).Adsorption/desorption technology has been described: people's such as Sohn US 6225518, be entitled as " separation method of alkene (Olefinic Hydrocarbon Separation Process) " in following document; People's such as Kantner US 5292990, be entitled as " being used for the isolating zeolite compositions of alkene (Zeolite Compositions For Usein Olefinic Separations) "; With people's such as McCulloch US 5276246, be entitled as " method (Process For Separating Normal Olefins From Non-NormalOlefins) of separating positive alkene and non-positive alkene ".

Can near small part normal olefine and paraffin stream be transported to other processing unit and/or store on the spot.In one embodiment, can in first pipeline 112, organize Olefins by normal olefine and alkane circulation pipeline 126 and first hydrocarbon stream to small part normal olefine and paraffin stream) "; People's such as Mason US 3400163, be entitled as " two heterocycles secondary and tertiary phosphine (Bicyclic Heterocyclic Sec-And Tert-Phosphines) "; People's such as Van Winkle US 3420898, be entitled as " alkene single hop hydroformylation become alcohol (Single StageHydroformylation Of Olefins To Alcohols) "; People's such as Van Winkle US 3440291, be entitled as " alkene single hop hydroformylation become alcohol (Single StageHydroformylation Of Olefins To Alcohols) "; People's such as Slaugh US3448157, be entitled as " hydrogenation of olefins formylation (Hydroformylation Of Olefins) "; People's such as Slaugh US 3488158, be entitled as " hydrogenation of olefins formylation (HydroformylationOf Olefins) "; People's such as Morris US 3496203, be entitled as " uncle's organic phosphine cobalt carbonylcomplex (Tertiary Organophosphine-Cobalt-Carbonyl Complexes) "; People's such as Morris US 3496204, be entitled as " uncle's organic phosphine cobalt carbonylcomplex (TertiaryOrganophosphine-Cobalt-Carbonyl Complexes) "; People's such as Van Winkle US 3501515, be entitled as " two heterocycle tertiary phosphine cobalt carbonylcomplexes (BicyclicHeterocyclic Tertiary Phosphine-Cobalt-Carbonyl Complexes) "; People's such as Mason US 3527818, be entitled as " the oxo alcohol (OxoAlcohols Using Catalysts Comprising Ditertiary Phosphines) that use contains the catalyzer of two tertiary phosphines "; U.S. Patent application No.10/075682, be entitled as " prepare branched olefin method, use this branched olefin to prepare the method and the tensio-active agent (A Process ForPreparing A Branched Olefin; A Method Of Using The BranchedOlefin For Making A Surfactant, and a Surfactant) of tensio-active agent "; With U.S. Patent application No.10/167209, be entitled as " preparation height straight chain alcohol method for compositions (Process for the Preparation Of A Highly Linear AlcoholComposition) ".Pure preparation: Othmer " chemical industry technology encyclopedia (Encyclopedia of Chemical Technology) " also described, 2000, the 4 editions in following document; " preparation of monohydroxy-alcohol, application and chemistry (MonohydricAlcohols with Wickson; Manufacture, Applications and Chemistry) " Ed.Am.Chem.Soc.1981.

The hydroformylation catalysts that is used for hydroformylation unit 120 can comprise the metal of periodictable group VIII.The example of group VIII metal comprises cobalt, rhodium, nickel, palladium or platinum.The group VIII metal can be used as complex compound.Complex compound can be and part bonded group VIII metal.The example of part includes but not limited to phosphine, phosphorous acid ester, arsine,  or pyridine ligand.The example of hydroformylation catalysts includes but not limited to cobalt carbonyl catalyst, cobalt-phosphine ligand catalyst, rhodium-phosphine ligand catalyst or its combination.

In hydroformylation unit 120, can use continuous, semicontinuous or batch technology, the alkene in hydroformylation the 3rd hydrocarbon stream.Under the situation of continuous operation mode, liquid hourly space velocity degree scope can be about 0.1-10h ^-1When with batch process operation hydroformylation unit 120, the reaction times can be changed to about 10 hours or even longer from about 0.1 hour.

Range of reaction temperature in the hydroformylation unit 120 can be about 100-300 ℃.In some embodiments, but in the hydroformylation unit use range be about 125-250 ℃ temperature of reaction.Pressure range in the hydroformylation unit 120 can be about latm (101kPa)-300atm (30398kPa).In one embodiment, can use the pressure of about 20atm (2027kPa)-150atm (15199kPa).With respect to the alkene consumption for the treatment of hydroformylation, catalyst consumption can change.The typical molar ratio range of the alkene in catalyzer and the 3rd hydrocarbon stream can be about 1: 1000 to about 10: 1.In some embodiments, can use about 1: 10 to about 5: 1 ratio.In one embodiment, dilute stream can be joined in the hydroformylation unit 120, with the control reaction conditions.Dilute stream can comprise the solvent that does not disturb required reaction basically.The example of this solvent includes but not limited to alcohol, ether, acetonitrile, tetramethylene sulfone and paraffinic hydrocarbons.

In hydroformylation unit 120, can realize at least 90% and even at least 92% monohydroxy-alcohol selectivity.In addition, conversion of olefines become fatty alcohol the transformation efficiency scope can for about 50wt% to greater than about 95wt%.In some embodiments, conversion of olefines becomes the transformation efficiency of fatty alcohol can be greater than 75wt%.In some embodiments, conversion of olefines becomes the transformation efficiency of fatty alcohol can be greater than about 99wt%.

Can realize from the logistics of hydroformylation reaction product, separating the fatty alcohol that is produced by common known method.In one embodiment, the separation of fatty alcohol comprises and makes the fatty alcohol that is produced carry out that the distillation first time, saponification, washing are handled and distillation for the second time.

The hydroformylation reaction mixture stream passes can enter separator 130 by the 3rd pipeline 132.In separator 130, can carry out the first step distilation steps (as flash distillation or short-path distillation) to the logistics of hydroformylation reaction product.In one embodiment, can use short-path distillation to produce two logistics at least: bottoms and overhead stream.In some embodiments, can be circulated back in the hydroformylation unit 120 by bottoms circulation line 134 to the small part bottoms.Overhead stream can include but not limited to paraffinic hydrocarbons, unreacting olefin and thick fatty alcohol product.

In one embodiment, can carry out saponification to overhead stream and handle, remove any acid and the ester that are present in this logistics.Can under agitation, overhead stream be contacted with the oxyhydroxide alkalescence aqueous solution (as sodium hydroxide or potassium hydroxide), thereby carry out saponification by under heating up.Can be 10: 1 to 1: 1 times by ratio, overhead stream be contacted with the oxyhydroxide alkalescence aqueous solution of 0.5-10%, thereby carry out saponification at thick alcohol/water.The consumption of employed hydroxide bases can be depending on the estimated value of existing ester and acid.

Can intermittently or carry out the saponification of overhead stream continuously.Can carry out the one or many saponification to overhead stream handles.The saponification reaction temperature can be about 40-99 ℃.In one embodiment, the saponification temperature scope can be about 60-95 ℃.Can in the saponification reaction process, carry out mixing of overhead stream and alkaline water layer.Can use currently known methods to carry out separating of overhead stream and alkaline water layer.Can wash overhead stream at after separating, to remove existing any sodium salt.Can use common known technology (as fractionation) to separate overhead stream, to produce two logistics at least: thick pure product stream and paraffinic hydrocarbons and unreacted olefins stream." fractionation " as used herein is meant distillating liquid and collects the liquid distillate of being determined by boiling point subsequently.Paraffinic hydrocarbons and unreacted olefins stream can be recycled, be transported in other unit and carry and/or sale for processing, storage on the spot, long-range (offsite).

In some embodiments, thick fatty alcohol product stream can contain undesired byproduct (as aldehyde, hemiacetal).Can be by thick pure product stream be carried out the hydrofining treatment step, thus remove byproduct, produce the fatty alcohol product stream." hydrofining " as used herein is meant the hydrogenation that carries out under gentle relatively condition.Can use conventional hydrogenation process to carry out hydrofining.Conventional hydrogenation process can comprise makes thick raw polyol pass through suitable hydrogenation catalyst bed with hydrogen stream.The fatty alcohol product stream can comprise the fatty alcohol that produces greater than about 50wt%.In some embodiments, the fatty alcohol product stream can comprise the fatty alcohol that produces greater than 80wt%.In other embodiments, the fatty alcohol product stream can comprise the fatty alcohol that produces greater than 95wt%.The fatty alcohol product stream can comprise the branched aliphatic primary alconol.Gained fatty alcohol in the fatty alcohol product stream can be by 136 market sales of product pipeline, long-range conveying, store on the spot and/or be used for other processing unit.

The composition of fatty alcohol product stream can comprise that the average carbon number scope is the hydrocarbon of 8-19.In one embodiment, the average carbon number scope of hydrocarbon can be 10-17 in the fatty alcohol product stream.In some embodiments, the average carbon number scope of feed stream can be 10-13.In other embodiments, the average carbon number scope of feed stream can be 14-17.In some embodiments, the branched primary alcohol product can be used as the precursor for preparing anion surfactant, comprising aliphatic sulfate and alkoxyl group sulfuric ester and alkoxyl alcohol.

Compare with the alkene precursor, fatty alcohol can have slightly high aliphatic side chain number and slightly high quaternary carbon number.In some embodiments, aliphatic side chain can comprise methyl and/or ethyl branch.In other embodiments, aliphatic side chain can comprise the aliphatic side chain of methyl, ethyl and Geng Gao.In some embodiments, the quaternary carbon atom number in the fatty alcohol product can be less than 0.5%.In other embodiments, the quaternary carbon atom number in the fatty alcohol product can be less than 0.3%.Can pass through ¹The branching of H NMR assay determination alcohol product.Can pass through ¹³C NMR measures the quaternary carbon atom number.At people's such as Singleton US 6150322, be entitled as and described the quaternary carbon atom measured in the branched aliphatic alcohols in " highly branched primary alcohol compositions and biodegradable washing composition prepared therefrom (Highly Branched Primary Alcohol Compositionsand Biodegradable Detergents Made Therefrom) " ¹³C NMR method.

In some embodiments, can in second pipeline 116, make up the generation combined stream by the 5th pipeline 138 and second hydrocarbon stream to small part paraffinic hydrocarbons and unreacted olefins stream.Can said composition stream be incorporated in the dehydrogenation-isomerization unit 114 by second pipeline 116.But isomerization becomes branched olefin to small part alkene in combined stream.In some embodiments, be introduced directly in the dehydrogenation-isomerization unit 114 by one or more entrances to small part paraffinic hydrocarbons and unreacted olefins stream.Can be used as a logistics and be circulated back in the dehydrogenation-isomerization unit 114 owing to contain the paraffinic hydrocarbons of paraffinic hydrocarbons and unreacting olefin and unreacted olefins stream, so this technology can be more effective, causes higher ultimate production.Higher output increases the overall yield of fatty alcohol.

In some embodiments, can be incorporated in the hydrogenation unit 110 by the 5th pipeline 138 to small part paraffinic hydrocarbons and unreacted olefins stream.In some embodiments, can in pipeline 112, make up by the 5th pipeline 138 and first hydrocarbon stream to small part paraffinic hydrocarbons and unreacted olefins stream.Said composition stream can enter in the hydrogenation unit 110 and continue this technology, to produce fatty alcohol.

In some embodiments, can be adjusted in alkene and paraffinic hydrocarbons concentration in the hydroformylation unit 120 according to the source that enters the olefin stream in the hydroformylation unit.Can add the 4th hydrocarbon stream in the upstream of hydroformylation unit 120, produce combined stream.In other embodiments, the 4th hydrocarbon stream can be introduced directly in the hydroformylation unit 120 by one or more points.The 4th hydrocarbon stream can be incorporated in the 3rd pipeline 118 by the 6th pipeline 140, produces combined stream.Said composition stream can enter in the hydroformylation unit 120 by the 3rd pipeline 118, continues this technology, produces fatty alcohol.

The 4th hydrocarbon stream can be from the source identical with first hydrocarbon stream.In some embodiments, the 4th hydrocarbon stream can be the hydrocarbon stream that comprises alkene, paraffinic hydrocarbons and/or hydrocarbon solvent derived from other source.The 4th hydrocarbon stream can comprise alkene and paraffinic hydrocarbons.In some embodiments, the average carbon number scope of hydrocarbon is 7-18 in the 4th hydrocarbon stream.In some embodiments, the content of paraffinic hydrocarbons can be between about 60-90wt% in the 4th hydrocarbon stream.In other embodiments, the content of paraffinic hydrocarbons can be greater than about 90wt% in the 4th hydrocarbon stream.

In some embodiments, with respect to total hydrocarbon content, the olefin(e) centent scope of the 4th hydrocarbon stream is about 1-99%.In some embodiments, the olefin(e) centent of the 4th hydrocarbon stream can be between about 45-99wt%.In other embodiments, the concentration of olefin in the 4th hydrocarbon stream can be greater than about 80wt%.

In some embodiments, dehydrogenation-isomerization unit 114 can be divided into a plurality of districts, with control reaction temperature and/or prevent undesired side reaction (forming and/or cyclization as diene).As among Fig. 3 A at as described in the system 200, first hydrocarbon stream that contains paraffinic hydrocarbons and unreacting olefin can be incorporated in the hydrogenation unit 110 by first pipeline 112.Hydrogenation of olefin can be carried out as previously described, to produce second hydrocarbon stream in hydrogenation unit 110.Second hydrocarbon stream can flow out hydrogenation unit 110 and enter dehydrogenation-isomerization unit 114 by second pipeline 116.Dehydrogenation-isomerization unit 114 can be divided into a plurality of districts.Described a plurality of district can include but not limited to first reaction zone, zone of transition and second reaction zone.In first reaction zone 210, in second hydrocarbon stream, can be dehydrogenated alkene to the small part paraffinic hydrocarbons, produce olefin stream.This process-stream can flow in second reaction zone 212 then.In second reaction zone 212, in process-stream, can be isomerizated into branched olefin to small part alkene, to produce the 3rd hydrocarbon stream.

In first reaction zone 210, the optional catalyst type of dehydrogenation catalyst from wide region.For example catalyzer can be based on the metal or the metallic compound that are deposited on the porous support.This metal or metallic compound can be selected from but be not limited to chromic oxide, ferric oxide and precious metal.

The Preparation of catalysts technology that is used to carry out dehydrogenation step and is used to carry out associated separation steps is known in the art.For example in following document, described the preparation catalyzer and carried out the suitable procedure of dehydrogenation step: people's such as Vora US 5012021, be entitled as " using solid catalyst to produce the method (Process For the Production of Alkyl AromaticHydrocarbons Using Solid Catalysts) of alkylaromatic hydrocarbon "; People's such as Moore US 3274287, be entitled as " conversion process of hydrocarbon and catalyzer (Hydrocarbon Conyersion Process andCatalyst) "; People's such as Abell US 3315007, be entitled as " with noble metal catalyst dehydrogenation stable hydrocarbon (Dehydrogenation of Saturated Hydrocarbons OverNoble-Metal Catalyst) "; People's such as Abell US 3315008, be entitled as " with noble metal catalyst dehydrogenation stable hydrocarbon (Dehydrogenation of SaturatedHydrocarbons Over Noble-Metal Catalyst) "; The US 3745112 of Rausch, be entitled as " homodisperse hydrocarbon conversion catalyst of platinum-Xi and method (Platinum-TinUniformly Dispersed Hydrocarbon Conversion Catalyst andProcess) "; People's such as Imai US 4506032, be entitled as " dehydrogenation catalyst composition (Dehydrogenation Catalyst Composition) "; With people's such as Imai US4430517, be entitled as " method of dehydrogenating (DehydrogenationProcess Using a Catalytic Composition) that uses catalytic composition ".

Range of reaction temperature in first reaction zone 210 can be about 300-600 ℃.In some embodiments, the range of reaction temperature in first reaction zone 210 can be about 450-550 ℃.Total pressure scope in first reaction zone 210 can be about 0.010atm (1kPa)-25.0atm (2534kPa).In some embodiments, the total pressure scope in first reaction zone 210 can be about 0.010atm (1kPa)-15.0atm (1520kPa).In some embodiments, hydrogen can be with the unreacted second hydrocarbon stream charging, so that prevent coking.Can be under about 0.1-20 in the molar ratio range of hydrogen and paraffinic hydrocarbons, feed hydrogen and the paraffinic hydrocarbons that is present in unreacted second hydrocarbon stream.In one embodiment, the molar ratio range of hydrogen and paraffinic hydrocarbons can be about 1-10.

Can be chosen in the residence time in first reaction zone 210, make paraffin conversion become the conversion of olefines rate to be lower than about 50mol%.In some embodiments, paraffin conversion becomes the conversion of olefines rate can be maintained at about in the 10-20mol% scope.By keeping low transformation efficiency, can prevent side reaction (forming and cyclization) as diene.In some embodiments, olefin stream can flow out first reactor 210, and the zone of transition of flowing through 214 also enters second reaction zone 212.Zone of transition 214 can comprise interchanger 216.Interchanger 216 can reduce the temperature of alkenes logistics.In one embodiment, described in Fig. 3 B, first reaction zone 210 in dehydrogenation-isomerization unit 114 and second reaction zone 212 can be unit independently, and interchanger 216 is between these two unit.

After in the alkenes logistics enters second reaction zone 212, become branched olefin to the small part isomerisation of olefin, produce the 3rd hydrocarbon stream.Can pass through ¹The composition and the degree of branching of H NMR assay determination the 3rd hydrocarbon stream.In one embodiment, olefin stream can flow out first reaction zone 210 and directly enter second reaction zone 212, becomes branched olefin to the small part isomerisation of olefin in this olefin stream.

Olefin isomerization is changed into identical that the employed catalyzer of branched olefin can be with described in the following document: the US 5648584 of Murray, be entitled as " method (Process for Isomerizing Linear Olefins to Isoolefins) that isomerizating straight-chain becomes isoolefine " and people such as Murray US 5648585, be entitled as " method (Process for Isomerizing Linear Olefins to Isoolefins) that isomerizating straight-chain becomes isoolefine ".

In one embodiment, in second reaction zone 212, contact with zeolite catalyst by making to the small part olefin stream, thus the normal olefine in isomerization second hydrocarbon stream.Zeolite catalyst can have crystallography free access diameter range greater than 4.2 dusts to less than at least one passages of about 7 dusts.Zeolite catalyst can have enough big oval aperture, spreads so that allow that normal olefine enters with branched olefin to small part.The aperture of zeolite catalyst also can be enough little, forms to postpone coke.

Temperature in second reaction zone 212 can be for about 200-500 ℃, so that isomerise linear olefinic hydrocarbons becomes branched olefin.In some embodiments, the temperature in first reaction zone and second reaction zone is basic identical.In these embodiments, do not require the use interchanger.Yet typically, the temperature of reaction of second reaction zone 212 is lower than the temperature of reaction of first reaction zone.Use temperature that interchanger reduces the logistics of leaving first reaction zone to suitable temperature at the second reaction zone internal reaction.The dividing potential drop scope of hydrocarbon can be about 0.1atm (10kPa)-10atm (1013kPa) in second reaction zone.

In some embodiments, the 3rd hydrocarbon stream can flow out second reaction zone and enter separating unit.At as described in Fig. 1, in separating unit, branched olefin can separate with paraffinic hydrocarbons with normal olefine as the front.With reference to figure 3A, the 3rd hydrocarbon stream can and enter in the hydroformylation unit 120 by the 3rd pipeline 118 outflow second reaction zones 212.As among Fig. 1 at as described in the system 100, in the 3rd hydrocarbon stream, can be produced the hydroformylation reaction logistics by hydroformylation to small part alkene.Can use common known method, the logistics of near small part hydroformylation reaction is separated into bottoms and overhead stream.Thick fatty alcohol product stream can produce paraffinic hydrocarbons and unreacted olefins stream and fatty alcohol product stream as being further purified as described in system 100.The fatty alcohol product stream can comprise branched aliphatic alcohols (as the branched aliphatic primary alconol).The fatty alcohol product stream can be recycled, be transported in other processing unit, sell and/or be transported in the storage vessel.

The hydroformylation reaction mixture stream passes can enter in the separator 130 by the 4th pipeline 132.In separator 130, can use the front at system's 100 described technology, produce at least three logistics: bottoms, paraffinic hydrocarbons and unreacted olefins stream and fatty alcohol product stream.Can be circulated back in the hydroformylation unit by bottoms circulation line 134 to the small part bottoms.Can and/or store on the spot with other process-stream Combined Cycle, conveying to small part paraffinic hydrocarbons and unreacted olefins stream.Can carry the fatty alcohol product streams by product pipeline 136, with storage on the spot, commercial distribution, long-range conveying and/or be used for other processing unit.

In one embodiment, to small part paraffinic hydrocarbons and unreacted olefins stream can be by the 5th pipeline 138 and the combination of second hydrocarbon stream, generation combined hydrocarbon stream.This combined hydrocarbon stream can enter first reaction zone 210 and experience the dehydroisomerization metallization processes and hydroformylation technology, produces fatty alcohol.By endless chain alkane and unreacted olefins stream, the productive rate of maximizing product.In one embodiment, paraffinic hydrocarbons and unreacted olefins stream can directly enter in the dehydrogenation-isomerization unit 114 by one or more entrances.

In some embodiments, as the front at as described in the system 100, can be according to the source that enters the unitary olefin stream of hydroformylation, be adjusted in the alkene in the hydroformylation unit 120 and the concentration of paraffinic hydrocarbons.Can be incorporated in the 3rd pipeline 118 by the 6th pipeline 140 near small part the 4th hydrocarbon streams in the upstream of hydroformylation unit 120.Combined stream can be incorporated in the hydroformylation unit 120 by the 3rd pipeline 118.In combined stream to small part alkene can be by hydroformylation, to produce fatty alcohol.In one embodiment, the 3rd hydrocarbon stream can be introduced directly in the hydroformylation unit 120 by one or more entrances.

Can use the concentration of olefin of the 4th hydrocarbon stream optimization in hydroformylation unit 120, make its concentration be enough to maximize the hydroformylation of alkene.In addition, the 4th hydrocarbon stream can be optimized the ratio of straight chain and branched-chain aliphatic group in fatty alcohol.The 4th hydrocarbon stream can be but be not limited to contain the hydrocarbon stream of alkene, paraffinic hydrocarbons and/or hydrocarbon solvent.

In one embodiment, can be with the catalyzer in the stacked bed configuration form use dehydrogenation-isomerization unit 114.The stacked bed configuration tolerable uses one or more catalyzer in reactor.Make the catalyzer of paraffin dehydrogenation and make the catalyzer of isomerisation of olefin can improve the selectivity of catalyzer and/or technology.The stacked bed configuration of dehydrogenation-isomerization unit 114 has been described at system 300 in Fig. 3.The operational condition of this stacked bed configuration can be with above identical at described two-region system of system 200.Second hydrocarbon stream can enter dehydrogenation zone 310 by second pipeline 116.

Employed dehydrogenation catalyst can have non-acid performance in stacked bed configuration.Term as used herein " nonacid " is meant and demonstrates the very catalyzer of ossiculum frame isomerization activity.Dehydrogenation catalyst can comprise precious metal, IVA family component, basic metal or alkaline earth metal component, halogen component and/or porous carrier materials.

In some embodiments, precious metal can be dispersed in the whole dehydrogenation catalyst.With the element is that benchmark calculates, and the amount ranges of precious metal can be about 0.01-5wt% of final dehydrogenation catalyst.In some embodiments, dehydrogenation catalyst comprises the platinum of about 0.1-1wt%.Can be before introducing other catalyst component, by technology known in the art (as co-precipitation, gelling altogether, ion-exchange, dipping, by gas phase or from the atom source deposition), precious metal is incorporated in the catalytic composite materials.In some embodiments, can in the process of introducing other catalyst component, precious metal be incorporated in the catalytic composite materials.In other embodiments, can after introducing other catalyst component, precious metal be incorporated in the catalytic composite materials.In some embodiments, can pass through solution or suspension impregnation solid support material, introduce precious metal with the decomposable compound of precious metal.For example can platinum be added on the catalytic carrier by the aqueous solution of blending platinum and Platinic chloride.In other embodiments, optional component (as nitric acid) can be joined in the dipping solution, to assist precious metal in the final catalyst matrix material, to disperse or to fix.

IVA family component can comprise germanium, tin, lead or its combination.In some embodiments, IVA family component can be present in the catalyzer with the oxidation state that is higher than precious metal.IVA family component can exist with oxide form.In some embodiments, IVA family component can combine with solid support material.In some embodiments, IVA family component can combine with other catalyst component.In other embodiments, IVA family component can be dispersed in the whole catalyzer.With the element is that benchmark calculates, and IVA family component can be about 0.01-5wt% of final catalyst composite.In some embodiments, catalyzer comprises the tin of about 0.2-2wt%.

Can before introducing other catalyst component,, IVA family component be incorporated in the catalytic composite materials according to common known method (as co-precipitation, gelling altogether, ion-exchange and dipping).In some embodiments, can in the process of introducing other catalyst component, introduce IVA family component.In other embodiments, can after introducing other catalyst component, introduce IVA family component.In some embodiments, can introduce the tin component by being total to gelling with porous carrier materials.Can tin be incorporated in the alumina supporting material by mixing soluble tin compounds (as tin protochloride or tin chloride) and alumina hydrosol.Jelling agent (as vulkacit H) can be joined in tin-alumina hydrosol mixture.Tin-alumina hydrosol mixture can splash in the oil bath, forms salic and ball tin.In other embodiments, can adopt the solution or the suspension (as being dissolved in the interior germanium tetrachloride of alcohol) of the decomposable compound of germanium, the germanium component is impregnated in the solid support material.In other embodiments, can be by the plumbous component of the solution impregnation of lead nitrate in water.

In some embodiments, basic metal or alkaline earth metal component can be included in the dehydrogenation catalyst.Basic metal and alkaline earth metal component can include but not limited to caesium, rubidium, potassium, sodium, lithium, barium, strontium, calcium and magnesium or its mixture.Basic metal or alkaline earth metal component can be present in the oxidation state that is higher than precious metal in the final catalyst matrix material.Basic metal or alkaline earth metal component can exist with oxide form.In some embodiments, basic metal or alkaline-earth metal can combine with solid support material.In some embodiments, basic metal or alkaline-earth metal can combine with other catalysis dehydrogenation component.

In other embodiments, basic metal or alkaline earth metal component can be dispersed in the whole catalytic composite materials.With the element is that benchmark calculates, and the amount ranges of basic metal or alkaline earth metal component can be about 0.01-15wt% of final catalytic composite materials.In other embodiments, dehydrogenation catalyst comprises the potassium of about 1-3wt%.In some embodiments, the atomic ratio of basic metal or alkaline earth metal component and precious metal can be greater than at least about 10.

Can before introducing other catalyst component,, basic metal or alkaline earth metal component be incorporated in the catalytic composite materials according to common known method (as co-precipitation, gelling altogether, ion-exchange or dipping).In some embodiments, can in the process of introducing other catalyst component, introduce basic metal or alkaline earth metal component.In other embodiments, can after introducing other catalyst component, introduce basic metal or alkaline earth metal component.For example adopt the solution of saltpetre, the potassium component is impregnated in the solid support material.The atomic ratio of basic metal or alkaline earth metal component and precious metal can be at least about 10.In some embodiments, the atomic ratio scope of basic metal or alkaline earth metal component and noble metal component can be about 15-25.

Employed porous carrier materials can comprise having about 25-500m in dehydrogenation catalyst ²The porous of the high surface area of/g absorbs carrier.The fusing point of this porous carrier materials can be higher than employed condition in dehydrogenation zone.The example of solid support material includes but not limited to mordenite and/or faujusite, spinel or its combination of gac, coke, charcoal, silicon-dioxide, silica gel, silicon carbide, synthetic preparation and/or naturally occurring clay and silicate, refractory inorganic oxide, crystalline zeolite silico-aluminate, natural existence or synthetic preparation.In some embodiments, solid support material can be γ-or η-aluminum oxide.In some embodiments, clay and silicate can be through acid treatment or without acid treatment (as attapulgite, potter's clay, diatomite (diatomaceous earth), Fuller's earth, kaolin, diatomite (kieselguhr), pottery, china clay, the refractory brick of pulverizing, alumina).The example of infusible inorganic oxide comprises aluminum oxide, titanium dioxide, zirconium dioxide, chromic oxide, beryllium oxide, vanadium oxide, cerium oxide, hafnia, zinc oxide, magnesium oxide, boron oxide, Thorotrast, silica-alumina, silica-magnesia, chromic oxide-aluminum oxide, aluminum oxide-boron oxide and silicon-dioxide-zirconium white.In some embodiments, zeolite aluminosilicate can be a Hydrogen.In other embodiments, zeolite aluminosilicate can be can with the form of metallic cation exchange.The example of spinel includes but not limited to MgAl ₂O ₄, FeAl ₂O ₄, ZnAl ₂O ₄, CaAl ₂O ₄And have formula MO-Al ₂O ₃Other similar compound, wherein M is that valence state is 2 metal.

In some embodiments, can prepare employed alumina supporting material in dehydrogenation catalyst in any suitable manner by synthetic or naturally occurring starting material.Can form alumina supporting material with any required shape (as sphere, ball, cake, extrudate, powder, particle).Can use the alumina supporter of any granularity.In some embodiments, can use sphere.Particle diameter can be about 1/16 inch.In some embodiments, can use less than about 1/32 inch particle diameter.

In some embodiments, can prepare alumina balls by aluminum metal being changed into aluminium dioxide colloidal sol.Can be by making aluminum metal and suitable peptization acid and water reaction, preparation alumina sol.Gained alumina sol and jelling agent can be splashed in the oil bath, form the spheroidal particle of alumina gel.Can use known technology (as by ageing, drying and roasting), the gained alumina gel is changed into γ-or η-alumina supporting material.

In other embodiments, can form extrudable composition by grinding alumina powder and water and suitable peptizing agent (as nitric acid), thus preparation aluminum oxide right cylinder.Can be by the die head extrusion compositions of suitable dimension, cutting then forms the extrudate particle.The alumina supporting material that can prepare other shape by ordinary method.After making the alumina particle moulding, can carry out drying and roasting.Can in preparation process, carry out intermediate treatment (as the solution washing of water or ammonium hydroxide) to alumina supporter.

Dehydrogenation catalyst can comprise halogen component.Halogen component can include but not limited to fluorine, chlorine, bromine, iodine or its mixture.Halogen component can exist with the bonded state with porous carrier materials.In some embodiments, halogen component can be dispersed in the whole catalytic composite materials.With the element is that benchmark calculates, and the scope of halogen component can be about 0.2-15wt% of final catalytic composite materials.In some embodiments, dehydrogenation catalyst contains the chlorine of the 1-3wt% that has an appointment.

In some embodiments, be that benchmark calculates with the element, catalyst composition can comprise the halogen component at least about 0.2wt%.Halogen component in the catalyzer can improve the activity that catalyzer makes the hydrocarbon dehydrogenation.In some embodiments, in the dehydrogenating technology process, active halogen component can be suppressed at the formation of carbon on the catalyzer.The advantage of catalyst composition can be to suppress undesirable isomerization or cracking side reaction.In some embodiments, content of halogen can increase the acidity of catalyzer.Can from dehydrogenation catalyst, remove excessive halogen by using the decatize dehydrogenation catalyst, thereby reduce acidity.

Can in any suitable manner halogen component be incorporated in the catalytic composite materials.Can before the preparation solid support material, introduce halogen.In some embodiments, can in the process of introducing other catalyst component, introduce halogen.In other embodiments, can after introducing other catalyst component, introduce halogen.In some embodiments, the alumina sol carrier can contain halogen, this halogen can constitute in the final catalyst composite to the small part content of halogen.In some embodiments, can introduce to solid support material in the process of other catalyst component, halogen component or its part are being joined (as using Platinic chloride platinum-impregnated component) in the catalyst composite.In other embodiments, can contact with halogen, halogen component or its part are joined in the catalyst composite by making catalyzer.In some embodiments, can be before or after other catalyst component to be introduced solid support material, compound, solution, suspension or dispersion (example hydrochloric acid) to contain halogen join halogen in the catalyzer.In some embodiments, can catalyzer be contacted with the compound that contains halogen, solution, suspension or dispersion liquid, introduce halogen component or its part by in process catalyst regeneration step subsequently.In regeneration step, in hydrocarbon conversion process, use in the process of catalyzer, the carbon that is deposited on the catalyzer with the coke form can burn from catalyzer.The precious metal that can reallocate on catalyzer is similar to the regenerated catalyst of live catalyst so that performance characteristic to be provided.Can in the carbon burning step process or in the precious metal redistribution process, add halogen component (as catalyzer is contacted with hydrogen chloride gas).In some embodiments, can pass through to add halogen or halogen-containing compound, solution, suspension or dispersion liquid (as propylene dichloride) in the feed stream of hydrocarbon, thereby halogen component is joined in the catalyst composite.In other embodiments, can in the operating process of dehydrogenation unit, halogen component be joined in the recycle gas.

In some embodiments, be that benchmark calculates with the element, dehydrogenation catalyst can comprise that scope is the sulphur component of about 0.01-10wt% of final catalytic composition.The sulphur component can be incorporated in the catalytic composite materials in any suitable manner.In some embodiments, can in the presence of hydrogen, under the temperature in about 10-540 ℃ scope, under anhydrous condition, sulphur or sulfocompound (as hydrogen sulfide or low molecular weight thiol) be contacted with catalyst composition.In some embodiments, hydrogen can be about 100 with the ratio of sulphur.

In some embodiments, dehydrogenation catalyst also can contain other additional component or its mixture, these components or alone or synergistically as catalyst modifier, to improve activity of such catalysts, selectivity or stability.The example of catalyst modifier includes but not limited to antimony, arsenic, beryllium, bismuth, cadmium, calcium, chromium, cobalt, copper, gallium, gold, indium, iron, lithium, manganese, molybdenum, nickel, rhenium, scandium, silver, tantalum, thallium, titanium, tungsten, uranium, zinc and zirconium.Can in the dehydrogenation catalyst preparation process, in any suitable manner catalyst modifier be joined in the solid support material.In other embodiments, can after the dehydrogenation catalyst preparation, add catalyst modifier in any suitable manner.In some embodiments, can before introducing other catalyst component, add catalyst modifier in any suitable manner in catalytic composite materials.In some embodiments, can in the process of introducing other catalyst component, add catalyst modifier.In other embodiments, can after introducing other catalyst component, add catalyst modifier.At people's such as Imai US4506032, be entitled as the description that can find relevant dehydrogenation catalyst in " dehydrogenation catalyst composition (Dehydrogenation CatalystComposition) ".

The alkenes logistics can be led in the isomerization zone 312.In some embodiments, what may need is to cool to isomerization zone 312 from dehydrogenation zone 310, to prevent alkenes logistics cracking when entering isomerization zone.Cold hydrogen can be incorporated in the dehydrogenation zone 310 by gas tube 314, with the temperature in the control dehydrogenation zone 310.In isomerization zone 312, in the alkenes logistics, can be isomerizated into branched olefin to small part alkene, to produce the 3rd hydrocarbon stream.

In some embodiments, isomerization catalyst can be with described identical at the isomerisation of olefin in the system 200.At the US 5510306 of Murray, be entitled as the description that can find relevant isomerization catalyst in " method (Process For Isomerizing Linear Olefins toIsoolefins) that isomerise linear olefinic hydrocarbons becomes isoolefine ".In some embodiments, the precious metal of about 0.01-5wt% can be joined in the isomerization catalyst that is used for stacked bed configuration, to increase the dehydrogenation activity of zeolite catalyst.Can use common metal introducing method (as dipping, precious metal ion exchange, grinding altogether), precious metal (as platinum, palladium) is incorporated in the zeolite, can be used for the effective catalyst of dehydrogenation-isomerization paraffinic hydrocarbons with generation.

The 3rd hydrocarbon stream can and enter in the hydroformylation unit 120 by the 3rd pipeline 118 outflow isomerization zone 312.As described at system 100, in the 3rd hydrocarbon stream can be to small part alkene by hydroformylation, produce the hydroformylation reaction logistics.Can use common known method, the logistics of near small part hydroformylation reaction is separated into bottoms and overhead stream.Can and separate overhead stream as purifying as described at system 100, produce paraffinic hydrocarbons and unreacted olefins stream and thick fatty alcohol product stream.Thick fatty alcohol product stream can be as being further purified as described in system 100, to produce the fatty alcohol product stream.The hydroformylation reaction mixture stream passes can enter separator 130 by the 4th pipeline 132.At as described in the system 100, can in separator 130, produce at least two logistics: bottoms and overhead stream as the front.Bottoms can be circulated back in the hydroformylation unit 120 by bottoms circulation line 134.But the overhead stream purifying also is separated at least two logistics: paraffinic hydrocarbons and unreacted olefins stream and thick fatty alcohol product stream.To small part paraffinic hydrocarbons and unreacted olefins stream can be recycled, with the combination of other process-stream, be transported in other processing unit and/or be transported in the storage vessel.Thick fatty alcohol product stream can further carry out purifying as described at system 100, to produce the fatty alcohol product stream.The fatty alcohol product stream can comprise the fatty alcohol (as the primary aliphatic alcohols of branching) of branching.Can carry the fatty alcohol product streams by product pipeline 136, so that storage on the spot, commercial distribution, long-range conveying and/or be used for other processing unit.

Can in second pipeline 116, be incorporated into small part paraffinic hydrocarbons and the unreacted olefins stream and second hydrocarbon stream by the 5th pipeline 138, produce combined hydrocarbon stream.This combined hydrocarbon stream can enter in the dehydrogenation zone 310 of dehydrogenation-isomerization unit 114 by second pipeline 116.The combined hydrocarbon stream that enters in the dehydrogenation zone 310 continues dehydroisomerization metallization processes and hydroformylation technology, produces fatty alcohol.By endless chain alkane and unreacted olefins stream, the productive rate of maximizing product.In one embodiment, paraffinic hydrocarbons and unreacted olefins stream can directly enter in the dehydrogenation-isomerization unit 114 by one or more entrances.

In some embodiments, can be according to the source that enters the unitary olefin stream of hydroformylation, be adjusted in the alkene in the hydroformylation unit 120 and the concentration of paraffinic hydrocarbons.As the front at as described in the system 100, can be in the unitary upstream of hydroformylation, near small part the 4th hydrocarbon stream is incorporated in the 3rd pipeline 118.Combined stream can be incorporated in the hydroformylation unit 120 by the 3rd pipeline 118.In combined stream to small part alkene can be by hydroformylation, to produce fatty alcohol.

The fatty alcohol that produces in system 100,200 and 300 can be changed into oxo alcohol, sulfuric ester or other commerical prod.In pure product stream, can be in the alkoxylate unit in the presence of alkali, produce alkoxyl alcohol to the small part fatty alcohol with epoxide (as oxyethane, propylene oxide, butylene oxide ring) reaction.Alcohol makes the functionality of alcohol expand one or more oxygen bases with the condensation of epoxide.The quantitative range of oxygen base can be 3-12.For example alcohol can produce the pure product with 3-12 oxyethyl group with reacting ethylene oxide.Alcohol and oxyethane and propylene oxide reaction can produce the ratio with oxyethyl group and oxyethyl group/propoxy-of propoxy-be about 4: 1 to about 12: 1 alcohol.In some embodiments, the alcohol moiety of larger proportion can combine with three above ethylene oxide moieties.In other embodiments, the alcohol moiety of approximate equal proportion can combine with three following ethylene oxide moieties.In typical alkoxylation products mixture, a small amount of ratio unreacting alcohol can be present in the product mixture.In one embodiment, can be by condensation C ₅-C ₃₁Fatty alcohol and epoxide are formed up to small part fatty alcohol product stream.In some embodiments, C ₅-C ₁₅Branched primary alcohol can with oxyethane and/or propylene oxide condensation.In other embodiments, C ₁₁-C ₁₇Branched primary alcohol can with oxyethane and/or propylene oxide condensation.But the commercial distribution of gained alkoxyl alcohol, long-range conveying, store on the spot and/or be used for other processing unit.In some embodiments, alkoxyl alcohol can be formed anion surfactant by sulfation.

In one embodiment, can be with joining in the alkali to small part alcohol in the fatty alcohol product stream.Alkali can be basic metal or alkaline earth metal hydroxides (as sodium hydroxide or potassium hydroxide).Alkali can serve as the catalyzer of alkoxylation.For the alkoxylate of alcohol,, can use the alkali number of about 0.1-0.6wt% based on the gross weight of alcohol.In one embodiment, based on total alcohol amount, the weight percentage scope of alkali is about 0.1-0.4wt%.Alcohol can cause forming alkoxide with the reaction of alkali.Can dry gained alkoxide, to remove any water that exists.The dry alkoxide of crossing can with epoxide reaction.In every mole of alkoxide, the amount of employed epoxide can be about 1-12mol epoxide.Gained alkoxide-epoxide mixture reaction is consumed up to epoxide.The decline of total reaction pressure can show to react to be finished.

Range of reaction temperature in the alkoxylate unit can be about 120-220 ℃.In one embodiment, range of reaction temperature can be about 140-160 ℃.Can be incorporated into by epoxide and reach reaction pressure in the reaction vessel institute's required amount.Epoxide has high vapour pressure under required temperature of reaction.Consider that from the angle of process safety the dividing potential drop of epoxide reaction thing can for example be restricted to less than about 4atm (413kPa).Other security measures can comprise with rare gas element such as nitrogen dilution reactant.For example inert gas dilution can cause the vapor phase concentration of reactant to be about and be less than or equal to 50%.In some embodiments, can be under bigger epoxide concentration, bigger total pressure and bigger epoxide branch depress, and realizes the reaction of alcohol-epoxide safely, if suitable, takes common known safe early warning to tackle explosion hazard.About oxyethane, can use the total pressure of about 3atm (304kPa)-7atm (709kPa).In some embodiments, can use the oxyethane total pressure of about 1atm (101kPa)-4atm (415kPa).In one embodiment, can use the oxyethane total pressure of about 1.5atm (150kPa)-3atm (304kPa).Pressure can be used as level of response and measures.When pressure no longer descends along with the time, think to react and finish substantially.

Can derive fatty alcohol and alkoxyl alcohol form the composition (as sulfonate, vitriol, phosphoric acid salt) that can be used for commerical prod prescription (as washing composition, tensio-active agent, oil additive, lubricant formula).For example available SO ₃Make the alcohol sulfuration, produce vitriol.Term " sulfuration " is meant that the functional group with sulphur atom or sulfur-bearing adds in carbon or the oxygen.Sulfuration process has been described: people's such as Jacobson US 6462215, be entitled as " sulfonation, sulfation and sulfanilamideization (Sulfonation, Sulfation and Sulfamation) " in following document; People's such as Jacobson US6448435, be entitled as " sulfonation, sulfation and sulfanilamideization (Sulfonation, Sulfation andSulfamation) "; People's such as Levinsky US 3462525, be entitled as " composition for tooth (Dental Compositions Comprising Long-ChainOlefin Sulfonates) that contains the long-chain olefin sulphonate "; People's such as Rubinfeld US 3428654, be entitled as " method of sulfonating of alkene and product (Alkene Sulfonation Process and Products) "; People's such as DiSalvo US 3420875, be entitled as " alkene sulfonic acid ester (Olefin Sulfonates) "; People's such as Rubinfeld US 3506580, be entitled as " thermal treatment of sulfonation olefin product (Heat-Treatment Of Sulfonated Olefin Products) "; With the US 3579537 of Rubinfeld, be entitled as " method (Process ForSeparation Of Sultones From Alkenyl Sulfonic Acids) of separating sultones and alkenyl sulfonic acid ".

The fatty alcohol vitriol that one class is general can characterize with following chemical formula: (R-O-(A) _x-SO ₃) _nM.R represents aliphatic part." A " represents alkylene oxide moiety; X representative is in each R-O mean number of A part partly, and scope can be 0-15; With n be the numeral that depends on positively charged ion M valence state.The example of positively charged ion M includes but not limited to alkalimetal ion, alkaline-earth metal ions, ammonium ion and/or its mixture.Cationic example includes but not limited to magnesium, potassium, monoethanolamine, diethanolamine or trolamine.

Can be in the sulfation unit sulfated fatty alcohol and alkoxyl alcohol.The sulfation process can comprise makes sulphur trioxide (SO ₃), chlorsulfonic acid (ClSO ₃H), thionamic acid (NH ₂SO ₃H) or sulfuric acid and alcohol reaction.In one embodiment, can use the sulphur trioxide in the vitriol oil (as oleum) to come sulfated alcohols.The concentration of the vitriol oil can be about 75-100wt% in water.In one embodiment, the concentration of the vitriol oil can be about 85-98wt% in water.In every mol of alcohol, the amount ranges of sulphur trioxide can be about 0.3-1.3mol sulphur trioxide.In some embodiments, in every mol of alcohol, the amount ranges of sulphur trioxide can be about 0.4-1.0mol sulphur trioxide.

In one embodiment, the sulfation process of sulphur trioxide can be included in liquid alcohol or alkoxyl alcohol are contacted with gaseous sulfur trioxide, produces the sulfuric ester of alcohol.Can be at about normal atmosphere with at the reaction zone of scope for operation falling film type sulfation device under about 25-70 ℃ the temperature.The sulfuric ester of alcohol can flow out falling film type sulfation device and enter neutralization reactor.The neutralization of sulfuric ester available bases metallic solution forms alkyl-sulphate or alkoxy sulfate.The example of alkali metal soln can comprise sodium hydroxide or potassium hydroxide solution.

The alcohol of derivatize can use in multiple application.The example of using comprises detergent formulation.Detergent formulation includes but not limited to granular laundry detergent formulation, liquid laundry detergent prescription, liquid dish washing detergent formulation and mixing formula.The example of mixing formula can comprise clean-out system, liquid soap, shampoo and the liquid scrubbing agent of general purpose.

Granular laundry can comprise various ingredients except derivatize alcohol (as tensio-active agent, washing assistant, washing assistant, SYNTHETIC OPTICAL WHITNER, activator of bleaching agent, Foam Control, enzyme, anti-graying agent, the agent of optics brilliant white and stablizer altogether) with detergent formulation.The example of other tensio-active agent can comprise ion, nonionic, both sexes or cats product.

The liquid laundry detergent prescription can comprise and the granular laundry identical component of detergent formulation.In some embodiments, the liquid laundry detergent prescription can comprise than granular laundry with detergent formulation inorganic builders component still less.Hydrotropic agent can be present in the liquid detergent formula.The clean-out system of general purpose can comprise other tensio-active agent, washing assistant, Foam Control, hydrotropic agent and stablizer alcohol.

Embodiment

Embodiment 1: the isomerization of alkene in the Fisher-Tropsch derived hydrocarbon stream

Under the fischer-tropsch process condition, make carbon monoxide and hydrogen reaction, obtain the hydrocarbon mixture of linear paraffins, normal olefine, a small amount of diolefine and a small amount of oxygenate.Use fractionating technology, the fischer-tropsch hydrocarbon stream is separated into different hydrocarbon streams.It is the alkene of 8-10 and the hydrocarbon stream of paraffinic hydrocarbons that acquisition contains average carbon number.By gas chromatographic analysis gained C ₈-C ₁₀The composition of hydrocarbon stream is listed in the table 1.

Table 1

The composition of fischer-tropsch hydrocarbon stream	wt％
		C 7Lighter hydrocarbon	0.12
C 8Branched olefin	0.02
		C 8Normal olefine	0.75
The 1-octene	0.69
		Octane	2.21
C 9Branched olefin	0.16
		C 9Normal olefine	8.52
The 1-nonene	8.07
		Positive nonane	20.03
C 10Branched olefin	0.28
		C 10Normal olefine	22.92
1-decene	20.87
		N-decane	41.12
C 11Heavier hydrocarbon	0.21
		C 9-C 11Alcohol	3.56

Preparation is used for the zeolite catalyst of hydrocarbon stream isomerizating straight-chain in the manner as described below.Ferrierite ammonium (645g) is loaded in the Lancaster mixing and grinding machine, and the loss on ignition of described ferrierite ammonium is 5.4% and has following performance: the mol ratio of silicon-dioxide and aluminum oxide is 62: 1, and surface-area is 369m ²/ g (P/P ₀=0.03), soda ash content is that 480ppm and normal hexane absorptive capacity are 7.3g/100g ferrierite ammonium.With loss on ignition is that 25.7% CATAPAL  D aluminum oxide (91g) joins in this shredder.In 5 minutes milling time process, add the 152ml deionized water in the mixture of aluminum oxide/ferrierite ammonium.Next, in the mixture of the aluminum oxide/ferrierite ammonium of the mixture that slowly adds 6.8g Glacial acetic acid, 7.0g citric acid and 152ml deionized water in the shredder, make the aluminum oxide peptization.The mixture of grinding gained aluminum oxide/ferrierite ammonium/acid 10 minutes.In 15 minutes time period, slowly add the mixture of 0.20g tetramine Palladous nitrate in the 153g deionized water in the mixture of the aluminum oxide/ferrierite ammonium/acid of grinding.Ratio and loss on ignition that the gained mixture demonstrates 90: 10 zeolite and aluminum oxide are 43.5%.By extruding the stainless steel template of Zeolite/alumina mixture by 2.25 inches Bonnot forcing machines (1/16 " hole), thereby make this mixture forming.

125 ℃ of following dryings should humidity Zeolite/alumina extrudate 16 hours.After drying, manually break (longsbreak) this Zeolite/alumina extrudate for a long time into pieces.In flowing air, under 200 ℃, roasting Zeolite/alumina extrudate 2 hours.The maximum temperature of elevated temperature to 500 ℃, and other 2 hours of this Zeolite/alumina extrudate of roasting obtain isomerization catalyst.This isomerization catalyst is cooled off under nitrogen atmosphere in moisture eliminator.

1 inch OD, 0.6 inch ID and 26 inches long stainless steel tubes are used as isomerization reactor.Thermocouple sheath extends 20 inches from stainless steel reactor tube top.In order to load this reactor tube, this reactor tube that reverses, and a slice glass wool is sent on the thermocouple sheath downwards along reactor tube walls, and place the reactor tube bottom, so that serve as the stopper of reactor tube.Silicon carbide (20 order) is joined about 6 inches degree of depth places of reactor tube.On silicon carbide, place the second sheet glass cotton.Divide two parts to join in the reactor tube in the mixture of 6.0g isomerization catalyst particles (6-20 order) and 45g fresh silicon carbide (60-80 order).Divide two parts of interpolations to make isomerization catalyst uniform distribution in reactor tube, and cause the isomerization catalyst bed of about 10 inchages.The 3rd sheet glass cotton is joined catalyzer top in the reactor tube.At shop, the cotton upper strata of the 3rd sheet glass silicon carbide (20 order).On silicon carbide, place the 4th sheet glass cotton, serve as the stopper of reactor tube bottom.In order to monitor the temperature of reaction at each point place in the reactor tube, the multiple spot thermopair is inserted in the thermocouple sheath of reactor tube.Monitoring in catalyst bed above, below and the temperature at three different positions places.The counter-rotating reactor tube also is installed in the stove.In 4 hours time period, under flowing nitrogen, heat the service temperature of this reactor tube to 280 ℃.In case reach 280 ℃ temperature, then under this service temperature, kept reactor tube other 2 hours, with the conditioning isomerization catalyst.

After the conditioning isomerization catalyst, hydrocarbon stream is passed through reactor tube with the flow pumping of 60g/h.The nitrogen of 6L/h and hydrocarbon stream pass through isomerization catalyst simultaneously.Before the contact isomerization catalyst, make the hydrocarbon stream evaporation.Under top hole pressure, operate this reactor tube than the high 20kPa of normal atmosphere.

In table 2, listed in the time of 0 hour in hydrocarbon stream and after isomerization in 24 and 48 hours in the effluent in reactor tube C ₈-C ₁₀Branched olefin, C ₈-C ₁₀Normal olefine and C ₈-C ₁₀The weight percentage of paraffinic hydrocarbons.In isomerization reactor, the normal olefine greater than 90% in the hydrocarbon stream changes into branched olefin.In the isomerization steps process, a small amount of boiling point is lower than C ₈Material produce by the cracking side reaction.In addition, be present in the interior portion C of raw material ₉-C ₁₁Alcohol is dehydrated, obtains the additional alkene in the product.Discovery is C in product ₈-C ₁₀The mean number of the alkyl branches on the alkene is 1.0, and this passes through ¹H NMR analyzes and measures.

Table 2

The composition of fischer-tropsch hydrocarbon stream in the isomerization reaction	0h wt％	24h wt％	48h wt％
				C 8-C 10Branched olefin	0.46	33.04	33.16
C 8-C 10Normal olefine	32.19	2.52	2.54
				C 8-C 10Paraffinic hydrocarbons	63.19	63.32	63.27
Side chain and straight chain C 8-C 10The ratio of alkene	0.1	13.1	13.1

The isomerization of embodiment 2:1-dodecylene

Obtain the 1-dodecylene from Shell Chemical Co..Listed composition in the table 3 by the 1-dodecylene of gas chromatographic analysis.

Table 3

The composition of 1-dodecylene	wt％
		The 1-dodecylene	98.0
Other C 10-C 14Alkene	1.2
		＜C 10Hydrocarbon	0.2
＞C 14Hydrocarbon	0.2
		Paraffinic hydrocarbons	0.4
Whole C 10-C 14Hydrocarbon	99.6

Use and reactor tube identical described in the embodiment 1 design and isomerization catalyst preparation, isomerization 1-dodecylene.Make the logistics of 1-dodecylene pass through reactor tube with the flow pumping of 90g/hr.Flow is that isomerization catalyst is passed through in nitrogen and the logistics of 1-dodecylene of 6L/h simultaneously.Before the contact isomerization catalyst, the logistics of evaporation 1-dodecylene.Under than the top hole pressure of the high 20kPa of normal atmosphere and under 290 ℃ temperature, the operant response organ pipe.

Table 4 has been listed in the time of 0 hour and in the effluent at reactor tube, be lower than C in the 1-dodecylene and after 168 and 849 hours ₁₀, C ₁₀-C ₁₄Be higher than C ₁₄The weight percentage of molecule.After 168 hours treatment time, straight chain C ₁₀-C ₁₄Alkene changes into branching C with 94% productive rate ₁₀-C ₁₄Alkene.In the isomerization steps process, be lower than C less than the 3wt% boiling point by cracking side reaction generation ₁₀Material.By ¹C in the H NMR assay determination product ₁₀-C ₁₄Alkyl branches mean number on the alkene is 1.3.

Table 4

The composition of 1-dodecylene logistics in the isomerization reaction	0hwt％	168hwt％	849hwt％
				＜C 10Hydrocarbon	0.2	2.5	2.4
C 10-C 14Hydrocarbon	99.6	97.2	97.4
				＞C 14Hydrocarbon	0.2	0.3	0.2
Branching C 10-C 14Alkene	0.6	93.2	93.4
				Straight chain C 10-C 14Alkene	99.0	2.8	2.9
Paraffinic hydrocarbons	1.0	2.0	1.9

Embodiment 3: the dehydrogenation of minimum isomerized dodecane

Obtain dodecane from Aldrich Chemical Company, and before handling, under nitrogen, store.Listed composition in the table 5 by the dodecane of gas chromatographic analysis.

Table 5

Dodecane is formed	wt％
		Dodecane	99.3
＜C 10Hydrocarbon	＜0.1
		C 10、C 11、C 13And C 14Hydrocarbon	＜0.6
＞C 14Hydrocarbon	＜0.1
		Other C 10-C 14Alkene	＜0.1

According to people's such as Imai US 4430517, be entitled as embodiment 1 (catalyst A) the preparation paraffin dehydrogenation catalyzer of " method of dehydrogenating (Dehydrogenation Process Using A Catalytic Composition) that uses catalytic composition ".The gained catalyzer comprises the platinum of the 0.8wt% on gamma-aluminium oxide carrier, the tin of 0.5wt%, the tin of 2.7wt%, the potassium of 2.7wt% and the chlorine of 1.3wt%.For this catalyzer, the atomic ratio of potassium and platinum is 16.8.

By the pure basically aluminium material of dissolving in hydrochloric acid soln, thus the preparation dehydrogenation catalyst.Add an amount of tin chloride in gained solution, so that the final matrix material that contains 0.5wt% tin to be provided, and stir, so as in whole mixture uniform distribution tin component.Add vulkacit H in the gained tin mixture, and, gained tin-amine mixt is splashed in the oil bath to form the mode that median size is about 1/16 inch spheroidal particle.This spheroidal particle of ageing, with the solution washing of ammonia, dry and roasting forms spherical gamma-alumina supporting material.The gained spheroidal particle contains the tin of the 0.5wt% stannic oxide form of having an appointment.At the US 2620314 of Hoesktra, be entitled as the more details that disclose in " spherical alumina (Spheroidal Alumina) " about the method for preparing alumina supporting material.

In rotatory drier, at room temperature, make tin-alumina composite material contact (weight based on aluminum oxide is 2wt%) with the deionization solution of Platinic chloride and hydrochloric acid 15 minutes.The consumption of employed Platinic chloride is that the platinum with 0.8wt% is incorporated into necessary amount in tin-alumina composite material.Heat this solution then, and use nitrogen purging, anhydrate to remove, thereby cause platinum-chloro-tin-alumina composite material.By heating platinum-chloro-tin-alumina composite material to 550 ℃, and at 300hr ^-1Gas hourly space velocity (GHSV) under, handle this matrix material with 50/50 air/80 a ℃ vapour mixture, thereby remove the chlorine of introducing.After with the air mixture process, platinum-Xi-alumina composite material contains the chlorine less than 0.1wt%.

Platinum-Xi-alumina composite material is contacted with the deionized water solution of saltpetre.The consumption of employed saltpetre is that the potassium with 2.7wt% is incorporated into necessary amount in platinum-Xi-alumina composite material.By purging (1000hr at dry air ^-1GHSV) under, heated this matrix material 0.5 hour to 100 ℃, from platinum-Xi-potassium-alumina composite material, remove and anhydrate.Elevated temperature to 525 ℃, and with the logistics (300hr of hydrochloric acid logistics (12cc/hr, 0.9M HCl) and 50/50 air/80 ℃ vapour mixture ^-1GHSV) handle platinum-Xi-potassium-alumina composite material, chlorine is incorporated in platinum-Xi-potassium-alumina composite material.Under 525 ℃, purge (1000hr at dry air ^-1GHSV) dry platinum-Xi under-potassium-chloro-alumina composite material.The median size of gained catalyst spheres is 1/16 inch, and before test, pulverizes and sieve into 6-20 purpose particle.

1 inch OD, 0.6 inch ID and 26 inches long stainless steel tubes are as isomerization reactor.Thermocouple sheath extends 20 inches from stainless steel reactor tube top.In order to load this reactor tube, this reactor tube that reverses, and a slice glass wool is sent on the thermocouple sheath downwards along the pipe reactor wall, and place the reactor tube bottom, so that serve as the stopper of reactor tube.Silicon carbide (20 order) is joined about 6 inches degree of depth places of reactor tube.On silicon carbide, place the second sheet glass cotton.With 6.0g on aluminium oxide catalyst particle (6-20 order) platinum-Xi and the mixture of 45g fresh silicon carbide (60-80 order) divide two parts to join in the reactor tube.Divide two parts of interpolations to make catalyzer uniform distribution in reactor tube, and cause the catalyst bed of about 10 inchages.The 3rd sheet glass cotton is joined catalyzer top in the reactor tube.At shop, the cotton upper strata of the 3rd sheet glass silicon carbide (20 order).On silicon carbide, place the 4th sheet glass cotton, serve as the stopper of reactor tube bottom.In order to monitor the temperature of reaction at each point place in the reactor tube, the multiple spot thermopair is inserted in the thermocouple sheath of reactor tube.Monitoring in catalyst bed above, below and the temperature at three different positions places.The counter-rotating reactor tube also is installed in the stove.Use the nitrogen purging reactor tube.In 4 hours time period, under flowing nitrogen, the service temperature of reacting by heating organ pipe to 425 ℃ (250 standard liters/hour).In case reach 425 ℃ service temperature, then under this service temperature, kept reactor tube other 2 hours.By under 425 ℃, make 1% the mixture flow of hydrogen sulfide in hydrogen through reactor tube, thus pre-sulfide catalyst.After 5 minutes, will the hydrogen sulfide in hydrogen gas stream convert the hydrogen stream of the reactor tube of flowing through to.

After pre-sulfide catalyst, kept reactor tube 8 hours down at 425 ℃.After 8 hours, make the pressure of reactor tube be increased to 25psig with hydrogen.125 standard liters/hour hydrogen flowing quantity under, dodecane passes through reactor tube with the flow pumping of 40g/h.After 4 hours, increase the dodecane logistics to 80g/h.After the flow that obtains 80g/h, the temperature of reactor tube is elevated to 460 ℃.After the service temperature of 460 ℃ of acquisitions, reactor tube is sampled every 8 hours.

After 24 hours, the weight percentage of dodecane is 11.4wt%, as described in the table 6.Under 479 ℃ temperature, to change into the conversion of olefines rate be 16wt% to dodecane after 24 hours.In the middle of formed alkene, 84wt% is a monoolefine, and 4.1wt% is that aromatic substance and 7.5wt% are diolefine.In the middle of formed alkene total amount, 6% by branching, by ¹H NMR analysis is measured.

Table 6

Test-results
		Transformation efficiency (wt%) after 24 hours puts into production under 460 ℃	11.4
The desired temperature of 16wt% transformation efficiency	479℃
		Monoolefine selectivity under the 16wt% transformation efficiency	84wt％
Arenes selectivity under the 16wt% transformation efficiency	4.1wt％
		Diolefine selectivity under the 16wt% transformation efficiency	7.5wt％
At whole C 12% branching C in the alkene 12Alkene	6

Embodiment 4: the dehydrogenation-isomerization of dodecane:

Obtain dodecane from Aldrich Chemical Company, and before handling, under nitrogen, store.Listed composition in the table 5 by the dodecane of gas chromatographic analysis.

Prepare the dehydrogenation-isomerization catalyzer in the manner as described below.Ferrierite ammonium (645g) is loaded in the Lancaster mixing and grinding machine, and the loss on ignition of described ferrierite ammonium is 5.4% and has following performance: the mol ratio of silicon-dioxide and aluminum oxide is 62: 1, and surface-area is 369m ²/ g (P/P ₀=0.03), soda ash content is that 480ppm and normal hexane absorptive capacity are 7.3g/100g ferrierite ammonium.With loss on ignition is that 25.7% CATAPAL  D aluminum oxide (91g) joins in this shredder.In 5 minutes milling time process, add the 152ml deionized water in the mixture of aluminum oxide/ferrierite ammonium.Next, in the mixture of the aluminum oxide/ferrierite ammonium of the mixture that slowly adds 6.8g Glacial acetic acid, 7.0g citric acid and 152ml deionized water in the shredder, make the aluminum oxide peptization.The mixture of grinding gained aluminum oxide/ferrierite ammonium/acid 10 minutes.In 15 minutes time period, slowly add the mixture of 0.20g tetramine Palladous nitrate in the 153g deionized water in the mixture of the aluminum oxide/ferrierite ammonium/acid of grinding.The gained mixture demonstrates 90: 10 zeolite and the ratio of aluminum oxide and 43.5% loss on ignition.By extruding the stainless steel template of Zeolite/alumina mixture by 2.25 inches Bonnot forcing machines (1/16 " hole), thereby make this mixture forming.

With the aqueous solution of the sour sodium of six hydration chlordene platinum [IV] dipping 6g gained Zeolite/alumina mixture, 0.8wt% platinum is incorporated in 1/16 inch the extrudate.Under 125 ℃, in flowing air, the extrudate of the Zeolite/alumina platinum dipping that drying should humidity 2 hours.The maximum temperature of elevated temperature to 500 ℃, and the extrudate of this Zeolite/alumina platinum dipping of roasting obtain the dehydrogenation-isomerization catalyzer.Before test, pulverize the catalyzer of roasting and sieve into 6-20 purpose particle.

Use and reactor tube identical described in the embodiment 3 design, make dodecane dehydrogenation and isomerization.At 459 ℃ after following 24 hours, observing dodecane, to change into the conversion of olefines rate be 16.1wt%.As listed in Table 7,86wt% is a monoolefine in the formed alkene, and 1.2wt% is that aromatic substance and 6.8wt% are diolefine.In the formed alkene total amount, by ¹H NMR analyzes and records 86% by branching.

Table 7

Test-results
		Transformation efficiency (wt%) after 24 hours puts into production under 460 ℃	16.1
The desired temperature of 16wt% transformation efficiency	459℃
		Monoolefine selectivity under the 16wt% transformation efficiency	86wt％
Arenes selectivity under the 16wt% transformation efficiency	1.2wt％
		Diolefine selectivity under the 16wt% transformation efficiency	6.8wt％
At whole C 12% branching C in the alkene 12Alkene	86

Embodiment 5: the dehydrogenation-isomerization catalyzer

With the embodiment 4 the same zeolite parts that prepare the dehydrogenation-isomerization catalyzer.With the aqueous solution of tetramine Palladous nitrate dipping 6g gained Zeolite/alumina mixture, the palladium of 0.8wt% is incorporated in 1/16 inch the extrudate.

Under 125 ℃, in flowing air, the extrudate of the Zeolite/alumina palladium dipping that drying should humidity 2 hours.The maximum temperature of elevated temperature to 500 ℃, and the extrudate of this Zeolite/alumina platinum dipping of roasting obtain the dehydrogenation-isomerization catalyzer.Before test, carefully pulverize the catalyzer of roasting and sieve into 6-20 purpose particle.

Embodiment 6: the dehydrogenation-isomerization catalyzer

According to people's such as Murray US 5648585, be entitled as in " method (Process For Isomerizing Linear Olefins ToIsoolefins) that isomerizating straight-chain is become isoolefine " at the described method of catalyzer D preparation dehydrogenation-isomerization catalyzer.

Use the ferrierite ammonium, this ferrierite ammonium has following performance: the mol ratio of silicon-dioxide and aluminum oxide is 62: 1, and surface-area is 369m ²/ g (P/P ₀=0.03), soda ash content is that 480ppmwt and normal hexane absorptive capacity are the 7.3g/100g zeolite.Use the Lancaster mixing and grinding machine, grind this catalyst component.Use Bonnot syringe (pin barrel) forcing machine to extrude the catalystic material of grinding.Employed tackiness agent is the CATAPAL  D aluminum oxide available from Sasol.Will be available from the Vltra tears of the METHOCEL  F4M of Dow Chemical Company as extrusion aid.

The Lancaster mixing and grinding machine is mounted with 632g ferrierite ammonium (LOI is 3.4%) and 92g CATAPAL  D aluminum oxide (LOI is 26.2%).With aluminum oxide and ferrierite blend 5 minutes, in this time period, add the 156ml deionized water.The mixture of 6.8g Glacial acetic acid and 156ml deionized water is slowly joined in the shredder, so that make the aluminum oxide peptization.This mixture of mixed grinding 10 minutes.Tetramine platinum nitrate and tetramine Palladous nitrate are joined in this mixing and grinding machine, so that produce the catalyzer that contains 0.25wt% palladium and 0.55wt% platinum.Add 10gMETHOCEL  F4M Vltra tears, and other 15 minutes of milled zeolite/aluminum oxide.Extrudate is transferred in the Bonnot syringe forcing machine, and used the stainless steel template in 1/16 inch hole to extrude.At 120 ℃ of following dry extrudates 16 hours, roasting 2 hours in air under 500 ℃ then.Before test, carefully pulverize the catalyzer of roasting and sieve into 6-20 purpose particle.

Claims (24)

1. method of producing fatty alcohol, this method comprises:

First hydrocarbon stream that will contain alkene and paraffinic hydrocarbons is incorporated in the hydrogenation unit, wherein construct this hydrogenation unit make in first hydrocarbon stream to the small part olefin hydrogenation become paraffinic hydrocarbons and wherein in first hydrocarbon stream to the small part unreacted components and at least partial hydrogenation alkene form second hydrocarbon stream;

Second hydrocarbon stream is incorporated in the dehydrogenation-isomerization unit, wherein constructing this dehydrogenation-isomerization unit makes and becomes alkene to the small part paraffin dehydrogenation in second hydrocarbon stream, wherein further constructing this dehydrogenation-isomerization unit makes to the small part isomerizating straight-chain and becomes branched olefin, wherein form the 3rd hydrocarbon stream to the small part unreacted components with to small part dehydrogenation and isomerization reaction product in second hydrocarbon stream, the 3rd hydrocarbon stream comprise alkene and paraffinic hydrocarbons and wherein in the 3rd hydrocarbon stream to small part alkene be branched olefin; With

Near small part the 3rd hydrocarbon stream is incorporated in the hydroformylation unit, wherein construct this hydroformylation unit make in the 3rd hydrocarbon stream to the formylation of small part hydrogenation of olefins, produce fatty alcohol, wherein contain branched-alkyl to the fatty alcohol that small part produced.

2. the process of claim 1 wherein that first hydrocarbon stream is by fischer-tropsch process production.

3. each method of claim 1-2, wherein first hydrocarbon stream comprises that carbon number is alkene and the paraffinic hydrocarbons of 7-18.

4. each method of claim 1-3 is wherein operated hydrogenation unit in about 175-250 ℃ temperature range.

5. each method of claim 1-4 is wherein operated hydrogenation unit under the hydrogen flowing quantity of about 250-5000NL/L/hr.

6. each method of claim 1-5 is wherein operated hydrogenation unit in the pressure range of about 10-50atm.

7. each method of claim 1-6 is wherein operated dehydrogenation-isomerization unit in about 300-500 ℃ temperature range.

8. each method of claim 1-7 is wherein constructed dehydrogenation-isomerization unit to operate in the pressure range of about 0.010-15atm.

9. each method of claim 1-8 wherein makes the paraffin conversion in the second hydrocarbon stream composition become the conversion of olefines rate less than about 40mol% to the residence time of small part second hydrocarbon stream in dehydrogenation-isomerization unit.

10. each method of claim 1-9 is wherein constructed the hydroformylation unit to produce the fatty alcohol greater than about 50%.

11. each method of claim 1-10, wherein operation hydroformylation unit in about 100-300 ℃ range of reaction temperature.

12. each method of claim 1-11 also comprises:

Form the hydroformylation reaction logistics, wherein the hydroformylation reaction logistics comprise in the 3rd hydrocarbon stream to the small part unreacted components with to fatty alcohol that small part produced;

From the hydroformylation reaction logistics, separate fatty alcohol, produce paraffinic hydrocarbons and unreacted olefins stream and fatty alcohol product stream; With

Near small part paraffinic hydrocarbons and unreacted olefins stream are incorporated in the dehydrogenation-isomerization unit.

13. the method for claim 12, wherein near small part paraffinic hydrocarbons and unreacted olefins stream are incorporated into that the upstream group that is included in dehydrogenation-isomerization unit in the dehydrogenation-isomerization unit is bonded to small part paraffinic hydrocarbons and unreacted olefins stream and to small part second hydrocarbon stream, produce combined stream, and near small part said composition stream is incorporated in the dehydrogenation-isomerization unit.

14. each method of claim 1-13 also comprises:

The fatty alcohol that near small part produced is incorporated in sulfation unit and/or the alkoxylate unit, wherein constructs this sulfation unit and makes to small part fatty alcohol sulfation generation aliphatic sulfate; Wherein comprise the branched aliphatic sulfuric ester to the aliphatic sulfate that small part produced, and wherein construct this alkoxylate unit and make to small part fatty alcohol alkoxylate and produce alkoxyl alcohol, wherein comprise branched alkoxy alcohol to the alkoxyl alcohol that small part produced.

15. each method of claim 1-14, wherein dehydrogenation-isomerization unit is included as dehydrogenation reaction in the catalytic dehydrogenation isomerization unit and isomerization reaction and the dehydrogenation-isomerization catalyzer made, and this catalyzer comprises h-type zeolite, tackiness agent, the compound of oxidation coke and the promotion compound of paraffin dehydrogenation with ferrierite isotypic framework structure.

16. each method of claim 1-15, wherein dehydrogenation-isomerization unit comprises a plurality of districts, described a plurality of district comprises first reaction zone and second reaction zone, wherein constructing first reaction zone makes to the small part paraffin dehydrogenation and becomes alkene, wherein construct second reaction zone and make to the small part isomerizating straight-chain and become branched olefin, wherein form the 3rd hydrocarbon stream to the small part unreacted components with to small part dehydrogenation and isomerization reaction product in second hydrocarbon stream.

17. the method for claim 16, wherein operation first reaction zone in about 300-600 ℃ temperature range.

18. the method for claim 16, wherein operation first reaction zone under the total reaction pressure of about 0.01-25.0atm.

19. the method for claim 16 wherein makes paraffin conversion become the conversion of olefines rate less than about 50mol% to the residence time of small part second hydrocarbon stream in first reaction zone.

20. the method for claim 16, wherein operation second reaction zone in about 250-500 ℃ temperature range.

21. the method for claim 16, wherein operation second reaction zone under the hydrocarbon partial pressure of about 0.1-10atm.

22. each method of claim 16-21 comprises that also second hydrocarbon stream that near small part flows out first reaction zone is incorporated in the interchanger, wherein constructs this interchanger, with heat extraction therefrom before entering second reaction zone at part second hydrocarbon stream.

23. each method of claim 1-22, wherein dehydrogenation-isomerization unit comprises the stackeding bed catalyst structure, and wherein this stackeding bed catalyst comprises dehydrogenation catalyst and isomerization catalyst.

24. be configured to implement each the system of production fatty alcohol of method of claim 1-23.

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