Branched alcohols

Abstract

A process for producing isomerized olefins, branched aldehydes and branched alcohols through isomerization, hydroformylation and hydrogenation.

Claims

1. A process, comprising the steps of: isomerizing an alpha olefin under a CO/H2 atmosphere at a first pressure, said isomerizing catalyzed by a first catalyst which is an organometallic complex of rhodium and one type of an organophosphorus ligand or an organometallic complex of rhodium and more than one type of an organophosphorus ligand, said isomerizing producing an isomerized olefin; hydroformylating said isomerized olefin under a CO/H2 atmosphere at a second pressure higher than said first pressure, said hydroformylating catalyzed by said first catalyst; said hydroformylating producing a branched aldehyde; and hydrogenating said branched aldehyde in the presence of a hydrogenation catalyst and H2 to produce a branched alcohol.

2. The process according to claim 1, wherein the said first pressure is in a range of 0.01 bar(g) to 10 bar(g).

3. The process according to claim 1, wherein the said second pressure is in a range of 5 bar(g) to 400 bar(g).

4. The process according to claim 1, wherein said process produces a reaction product comprising a 30 wt. % or greater branched alcohol.

5. The process according to claim 1, wherein said process produces a reaction product comprising a 50 wt. % or greater branched alcohol.

6. The process according to claim 1, wherein said process produces a reaction product comprising a 70 wt. % or greater branched alcohol.

7. The process according to claim 1, wherein the alpha olefin is a mixture of one or more C4 to C36 alpha olefins.

8. The process according to claim 1, wherein the said first pressure is in a range of 0.0 bar(g) to 20 bar(g).

9. A process, comprising the steps of: providing CO and H2; providing a first catalyst which is an organometallic complex of rhodium and one type of an organophosphorus ligand or an organometallic complex of rhodium and more than one type of an organophosphorus ligand; providing a linear alpha olefin; isomerizing said linear alpha olefin by said first catalyst in the presence of CO and H2 at a first pressure to produce an isomerized olefin; hydroformylating said isomerized olefin by said first catalyst in the presence of CO and H2 at a second pressure higher than said first pressure to produce a branched aldehyde; and hydrogenating said branched aldehyde in the presence of a hydrogenation catalyst and H2 to produce a branched alcohol.

10. The process according to 9, wherein said branched alcohol is a 2-alkyl branched alcohol.

11. The process according to 9, wherein said linear alpha olefin is a 1-Dodecene and said branched alcohol comprises a branched Tridecanol.

12. The process according to 9, wherein said linear alpha olefin is a 1-Tetradecene and said branched alcohol comprises a branched Pentadecanol.

13. The process according to 9, wherein the organophosphorous ligand can be a phosphite.

14. The process according to 9, wherein the phosphite ligand can be tris (2, 4-di-t-butylphenyl) phosphite.

15. The process according to 9, wherein a mixture of organophosphorous ligands of different types can be a mixture of triphenylphosphine and tris (2, 4-di-t-butylphenyl) phosphite.

16. The process according to 9, wherein said linear alpha olefin is a mixture of one or more C4-C36 linear alpha olefins.

Description

BRIEF DESCRIPTION OF THE DRAWINGS

(1) The present invention in its several aspects and embodiments solves the problems discussed above and significantly advances the technology of branched compounds and methods for producing and manufacturing branched compounds. The present invention can become more fully understood from the detailed description and the accompanying drawings, wherein:

(2) FIG. 1 shows an embodiment of a chemical manufacturing process having an isomerization reactor and a hydroformylation reactor;

(3) FIG. 2 shows an embodiment of a chemical manufacturing process having an isomerization reactor with an isomerization reactor bypass and a hydroformylation reactor;

(4) FIG. 3 shows an embodiment of a chemical manufacturing process having an isomerization reactor, a hydroformylation reactor and catalyst recovery;

(5) FIG. 4 shows an embodiment of a chemical manufacturing process having an isomerization reactor, a hydroformylation reactor, catalyst recovery and aldehyde distillation;

(6) FIG. 5 shows an embodiment of a chemical manufacturing process having an isomerization reactor, a hydroformylation reactor, catalyst recovery and an aldehyde hydrogenation reactor;

(7) FIG. 6 shows an embodiment of a chemical manufacturing process having an isomerization reactor, a hydroformylation reactor, catalyst recovery, aldehyde distillation and an aldehyde hydrogenation reactor;

(8) FIG. 7 shows Sales Specification 1;

(9) FIG. 8 shows Sales Specification 2;

(10) FIG. 9A shows Sales Specification 3, page 1;

(11) FIG. 9B shows. Sales Specification 3, page 2;

(12) FIG. 10 shows Sales Specification 4;

(13) FIG. 11A shows Sales Specification 5, page 1;

(14) FIG. 11B shows Sales Specification 5, page 2; and

(15) FIG. 12 shows Sales Specification 6.

(16) Herein, like reference numbers in one figure refer to like reference numbers in another figure.

DETAILED DESCRIPTION OF THE INVENTION

(17) In an embodiment, a two-step process is disclosed herein that produces branched aldehyde products, with 25% to 98+% branching, that are produced from an alpha olefin feedstock. Additionally, the two-step process disclosed herein employs an organometallic complex of rhodium and at least one organophosphorous ligand for both the first step which is an isomerization reaction step and the second step which is a hydroformylation reaction step.

(18) Numeric values and ranges herein, unless otherwise stated, also are intended to have associated with them a tolerance and to account for variances of design and manufacturing. Thus, a number can include values about that number. For example, a value X is also intended to be understood as about X. Likewise, a range of YZ, is also intended to be understood as within a range of from about Y-about Z. Unless otherwise stated, significant digits disclosed for a number are not intended to make the number an exact limiting value. Variance and tolerance is inherent in mechanical design and the numbers disclosed herein are intended to be construed to allow for such factors (in non-limiting e.g., ?10 percent of a given value). Likewise, the claims are to be broadly construed in their recitations of numbers and ranges.

(19) Every numerical range given throughout this specification will include every narrower numerical range that falls within such broader numerical range, as if such narrower numerical ranges were all expressly written herein. As regarding ranges and endpoints, every maximum numerical limitation given throughout this specification includes every lower numerical limitation, as if such lower numerical limitations were expressly written herein. Every minimum numerical limitation given throughout this specification will include every higher numerical limitation, as if such higher numerical limitations were expressly written herein.

(20) Herein the term reactor means one or more physical reactors that individually or in combination are used to achieve a reactive step in chemical processing. Herein, reaction step and reactive step are used synonymously. A reactor can be a single vessel or optionally multiple vessels. A reactor can optionally be configured such that a reactive step occurs in one or more reactor vessels. If there are a number of reactor vessels, such reactor vessels can be operated in series, in parallel, or any combination thereof. Herein, the term reactor is the unit operation of conducting a chemical reaction processing step, also referred to as a reaction step, or reactive step.

(21) For example, as shown in FIGS. 1-6 the representation of a reactor and/or the recitation of a reactor should not be construed to be limited to specifically a single physical reactor. Optionally a single physical reactor can be used to achieve a reaction step, or optionally a number of physical reactor vessels can be used to achieve the reaction step. Herein, the term reactor should be construed to mean a reactive step which in fact could be carried out in one or more reactors operating in series, parallel, or any combination thereof. Therefore, isomerization reactor should be construed to mean an isomerization step (meaning an isomerization reaction step) occurring in one or more reactors operating in series, parallel, or any combination thereof. Analogously, hydroformylation reactor should be construed to mean a hydroformylation step (meaning an hydroformylation reaction step) occurring in one or more reactors operating in series, parallel, or any combination thereof. Further, hydrogenation reactor should be construed to mean a hydrogenation step (meaning a hydrogenation reaction step) occurring in one or more reactors operating in series, parallel, or any combination thereof.

(22) Unless otherwise stated temperatures recited herein are in degrees Celsius (? C.)

(23) Unless otherwise stated pressures recited herein are in bar(g), i.e. bars gauge. Herein, 0 bar(g) is atmospheric pressure, e.g. 14.70 psia (aka 0 psig).

(24) Unless otherwise stated percentages of composition recited herein are on a weight basis and disclosed as weight percent (wt. %).

(25) Alternatively, herein, concentration can be expressed in units of parts per million, or ppm.

(26) Herein, the number of carbons in a molecule is denoted with a capital C followed by an integer representing the carbon number of the molecule. For example, a C12 molecule is a molecule having 12 carbons (i.e. 1-dodecene for example).

(27) Herein, the term olefin is used synonymously with the term alkene, meaning a molecule containing a carbon-carbon double bond.

(28) Herein branched is defined as a molecule, compound or chemical structure, having one or more alkyl groups attached along a carbon backbone. Branched molecules are isomers of linear (i.e. straight-chain) molecules having the same number of carbon atoms.

(29) Herein, the term percent branched, in additional to its ordinary and customary meaning, is defined herein to mean the wt. % branched molecules in a composition. The term percent branching is use synonymously with percent branched and has the same meaning as percent branched. As an example, for an aldehyde composition, the percent branching of the aldehyde means the wt. % of the aldehyde being branched, i.e.
=100*(wt. % branched aldehyde)?(wt. % branched aldehyde+wt. % linear aldehyde).

(30) As an example, a branched C6 aldehyde composition comprising:

(31) TABLE-US-00001 25 wt. % 1-Hexanal (linear molecule) 40 wt. % 2-Methyl-Pentanal (branched molecule) 35 wt. % 2-Ethyl-butanal (branched molecule) would have a Percent Branching = 75%

(32) Unless otherwise stated percent branching recited herein are in weight percent (wt. %) is calculated based upon reactant and product weights, excluding nonparticipating compounds.

(33) Herein, the term percent isomerized, in additional to its ordinary and customary meaning, is defined herein to mean the wt. % of olefin molecules where the olefin has been isomerized from the alpha position to an internal olefin position. Specifically, the percent isomerized means the wt. % of the olefin composition being internal olefins, i.e.:
100*(wt. % internal olefin)?(wt. % alpha olefin+wt. % internal olefin).

(34) As an example, a C12 alpha olefin isomerized to produce a composition comprising:

(35) TABLE-US-00002 25 wt. % 1-Dodecene (alpha olefin) 40 wt. % 2-Dodecene (internal olefin)) 35 wt. % 3-Dodecene (internal olefin) would have a Percent Isomerized = 75%

(36) Unless otherwise stated the term internal olefin recited herein means an olefin in which a double bond is present in a position other than the alpha position.

(37) Unless otherwise stated percent isomerized recited herein are in weight percent (wt. %) is calculated based upon reactant and product weights, excluding nonparticipating compounds.

(38) In an embodiment, branched alcohols, can be manufactured by the following process method steps: 1. providing a C4-C36 alpha olefin; 2. providing a homogeneous rhodium organophosphorous ligand catalyst; 3. isomerizing said C4-C36 olefin catalyzed by said rhodium catalyst under an atmosphere of CO/H2 at a pressure between 0.01 bar(g) and 10 bar(g); 4. producing an intermediate isomerized olefin product composition having at least 20 wt. % of internal (non-alpha) olefins; 5. hydroformylating said intermediate isomerized olefin product catalyzed by said rhodium catalyst under an atmosphere of CO/H2 at a pressure between 5 bar(g) and 400 bar(g); 6. producing a branched aldehyde product composition having at least 25 wt. % branched aldehydes; 7. separating said branched aldehyde product from the rhodium containing catalyst stream via a distillation process; 8. hydrogenating said branched aldehyde in the presence of a hydrogenation catalyst at elevated hydrogen pressure; and 9. producing a branched alcohols product composition having at least 40 wt. % branched alcohols.

(39) FIG. 1 shows an embodiment of a chemical manufacturing process having an isomerization reactor and an hydroformylation reactor.

(40) FIG. 1 describes a two-step process in which Stream 1 having alpha olefins that is fed to isomerization reactor 100 which produces Stream 2 having isomerized olefins that is fed to hydroformylation reactor 200 which produces Stream 3 having branched aldehydes.

(41) Catalyst Specifications & Compositions

(42) In an embodiment the same catalyst is used in each of the first step and second step of the two-step process. In an embodiment, the same catalyst is used in the isomerization reactor 100 and the hydroformylation reactor 200.

(43) In an embodiment, the isomerization and hydroformylation reactions can be catalyzed by a rhodium organophosphorus ligand catalyst. The organophosphorus ligand catalyst can be activated by the presence of CO.

(44) In an embodiment the catalyst can be a rhodium (PPh.sub.3) catalyst system.

(45) For Example, a rhodium triphenylphosphine (PPh.sub.3) catalyst system can exist in different states and/or configurations which allow for use in different reactions such as for the isomerization reactions and hydroformylation reactions disclosed herein. As shown in sequence one below, on the far left it is shown that without the presence of CO, the catalyst is in an inactive state because the three attached PPh.sub.3 groups block the sites for catalyst activity. However, as CO is added to the system the PPh.sub.3 groups on the rhodium are increasingly replaced with CO groups which opens up the catalyst and makes it active and able to catalyze the isomerization and hydroformylation reactions of the embodiments disclosed herein.

(46) ##STR00001##

(47) Catalyst Composition

(48) In an embodiment, the molar ratio (P:Rh) of phosphorous (P) to rhodium (Rh) in the isomerization reaction or the hydroformylation reaction can be in a range of 1:1 to 1000:1, or 3:1 to 200:1, or 5:1 to 50:1, such as for non-limiting example 1:1, 3:1, 5:1, 10:1, 20:1, 30:1, 40:1, 50:1, 100:1, 200:1, 500:1 or 1000:1.

(49) In an embodiment, the concentration of Rh in the isomerization reaction or the hydroformylation reaction can be in a range of 1 to 10000 ppm, 10 to 1,000 ppm, or 20-200 ppm, such as in non-limiting example 1 ppm, 20 ppm, 50 ppm, 100 ppm, 200 ppm, 300 ppm, 400 ppm, 500 ppm, 1000 ppm, 2000 ppm, 5000 ppm, 7500 ppm, or 10000 ppm

(50) In an embodiment, the catalyst used in the isomerization and hydroformylation reactions is an organometallic rhodium ligand complex formed from Rh(CO).sub.2ACAC ((Acetylacetonato)dicarbonylrhodium(I)) and tris (2,4,-di-t-butylphenyl) phosphite ligand.

(51) Isomerization

(52) The first step occurs in isomerization reactor 100 where the Stream 1 feed to isomerization reactor 100 can have a composition comprising: A C4-C36 alpha olefin (or mixtures thereof); Rhodium catalyst A; Carbon Monoxide (CO); and Hydrogen.

(53) Optionally, Stream 1 can have a high-boiling inert solvent, for example Polyalphaolefin.

(54) Rhodium catalyst A is an organometallic complex of Rhodium and at least one organophosphorus ligand. The isomerization reaction can proceed at a temperature of 30-300? C., e.g. 90? C. in the presence of CO and H2 at a pressure of 0.1-10 bar(g). The isomerization reaction conditions can also be described as proceeding at a temperature of 30-300? C., e.g. 90? C. under a CO and H2 atmosphere at a pressure of 0.1-10 bar(g).

(55) The isomerization process can be processed batchwise, or on a continuous basis. All reactions and unit operations disclosed herein can be processed batchwise, or on a continuous basis.

(56) In an embodiment, the catalyst used in this isomerization and hydroformylation reaction is a rhodium ligand complex as Rh(CO).sub.2ACAC ((Acetylacetonato)dicarbonylrhodium(I)) with tris (2,4,-di-t-butylphenyl) phosphite in a PAO-4 (polyalphaolefin) high boiling inert solvent.

(57) In a nonlimiting example, Stream 1 can have one or more of the feedstocks specific in the sales specification of FIGS. 7-12.

(58) In an embodiment, the feed having an alpha olefin, or having a mixture of linear olefins, can be isomerized at a temperature in a range of 30? C. to 500? C., or 40? C. to 200? C., or 50? C. to 120? C., such as in non-limiting example 30? C., 50? C., 80? C., 90? C., 100? C., 120? C., 150? C., 180? C., 200? C., 250? C., 300? C., 400? C., or 500? C.

(59) In an embodiment, the feed having an alpha olefin, or having a mixture of linear olefins, can be isomerized at a pressure in a range of 0.0 bar(g) to 20 bar(g), 0.1 bar(g) to 10 bar(g), 0.5 bar(g) to 5 bar(g), such as in non-limiting example 0.01 bar(g), 1 bar(g), 5 bar(g), 7.5 bar(g), 9 bar(g), 10 bar(g), 12 bar(g), 15 bar(g), 18 bar(g), or 20 bar(g).

(60) In an embodiment, an isomerization of a linear alpha olefin, or mixture of linear alpha olefins, can be isomerized at a pressure in a range of 0 bar(g) to 20 bar(g), such as 0 bar(g), 0.1 bar(g), 0.5 bar(g), 1 bar(g), 2 bar(g), 5 bar(g), 10 bar(g), or 20 bar(g).

(61) In an embodiment, an isomerization of a linear alpha olefin, or mixture of linear alpha olefins, can be isomerized at a pressure of 20 bar(g) or less and 100? C. or less, e.g. 1 bar(g) and 90? C.

(62) Stream 1Alpha Olefin Feed Composition

(63) In an embodiment, Stream 1 can be a C4-C36 linear alpha olefin. For example, the Stream 1 feed can be a 1-dodecene feedstock which substantially is a C12 linear alpha olefin, such as the AlphaPlus? 1-Dodecene (Chevron Phillips Chemical Company LP, P.O. Box 4910, The Woodlands, TX 77387-4910, phone (800) 231-3260) as shown in FIG. 7, Sales Specification 1.

(64) In an embodiment, the Stream 1 feed can be a 1-dodecene feedstock which substantially is a C12 linear alpha olefin, such as the NEODENE? 12 (Shell Global Solutions, One Shell Plaza, 910 Louisiana, Houston, TX 77002-4916, US, phone (832) 337-2000) as shown in Sales specification 3, as shown in FIG. 9A-9B.

(65) In another embodiment, Stream 1 feed can be a 1-dodecene feedstock which substantially is a C12 linear alpha olefin, such as INEOS Oligomers, Alpha Olefin C12 (dodecane-1) (2600 South Shore Boulevard, Suite 400, League City, TX 77573, phone (281) 535-4266) as shown in Sales specification 4, as shown in FIG. 10.

(66) In an embodiment, the Stream 1 feed can be a 1-tetradecene feedstock which substantially is a C14 linear alpha olefin, such as the AlphaPlus? 1-tetradecene (Chevron Phillips Chemical Company LP, P.O. Box 4910, The Woodlands, TX 77387-4910, US, phone (800) 231-3260) as shown in FIG. 8, Sales Specification 2.

(67) In an embodiment, the Stream 1 feed can be a 1-tetradecene feedstock which substantially is a C14 linear alpha olefin, such as the NEODENE? 14 (Shell Global Solutions, One Shell Plaza, 910 Louisiana, Houston, TX 77002-4916, US, phone (832) 337-2000) as shown in FIG. 11A-11B, Sales specification 5.

(68) In another embodiment, Stream 1 feed can be a 1-tetradecene feedstock which substantially is a C14 linear alpha olefin, such as INEOS Oligomers, Alpha Olefin C14 (tetradecane-1) (2600 South Shore Boulevard, Suite 400, League City, Texas 77573, phone (281) 535-4266) as shown in FIG. 12, Sales specification 6.

(69) In an embodiment, the Stream 1 feedstock can be a composition having one or more alpha olefins. The alpha olefins of the Stream 1 feed can be the same, or different, and have the same or different carbon chain lengths. For example, the Stream 1 alpha olefins fed as reactants for isomerization can be one or more alpha olefins from the group of C4-C36 alpha olefins, or greater.

(70) In an embodiment, a C12 linear alpha olefin fed as a reactant for isomerization can be 90.0 wt. % or greater, such as greater than 94.0 wt. % C12 linear alpha olefin, or 94.6 wt. % C12 linear alpha olefin, or 99 wt. % C12 linear alpha olefin, or greater.

(71) In an embodiment, a C14 alpha olefin fed as a reactant for isomerization can be 90.0 wt. % or greater, such as greater than 93.0 wt. % C14 linear alpha olefin, or 93.4 wt. % C14 linear alpha olefin, or 99 wt. % C14 linear alpha olefin, or greater.

(72) In an embodiment, the alpha olefin feedstock to the isomerization reactor has a concentration of vinylidene of 10 wt. % or less, e.g. 4 wt. % or less.

(73) In an embodiment, a branched aldehyde product can be produced by a process, having the steps of: isomerizing one or more C4-C36 alpha olefins by a first catalyst which is an organometallic complex of rhodium and one type of an organophosphorus ligand or an organometallic complex of rhodium and more than one type of an organophosphorus ligand in the presence of a gas phase comprising CO at a first pressure producing an isomerized olefin; and hydroformylating said isomerized olefin by said first catalyst in the presence of a gas comprising CO and H2 at second pressure different from said first pressure producing a C5-C37 branched aldehyde product. In an embodiment, a branched aldehyde product can be 40 wt. % to 100 wt. % branched.

(74) Stream 2, Isomerization Reactor Product Stream Composition

(75) The isomerization reaction of isomerization reactor 100 produces an isomerization reaction product stream which can be fed into hydroformylation reaction 200. Stream 2, can have a composition comprising internal olefin products of the isomerization reaction in which a portion of the starting alpha olefins have been isomerized to an olefin mixture comprising in non-limiting example: >20 wt. % internal olefins, i.e. olefins where the double bond has been isomerized internally to the molecule and is no longer in the alpha position; and <80 wt. % alpha olefins.

(76) Stream 2 is an isomerization reactor product stream having isomerized olefins which can have a percent isomerization in a range of 10 wt. % to 99%, or greater, e.g. 10 wt. %, 15 wt. %, 20 wt. %, 25 wt. %, 30 wt. %, 35 wt. %, 40 wt. %, 45 wt. %, 50 wt. %, 60 wt. %, 70 wt. %, 80 wt. %, 90 wt. %, or 99 wt. %. In an embodiment, stream 2 which is an isomerization reactor product stream can have internal olefins in a composition of 20 wt. %, or greater.

(77) Stream 3, Hydroformylation Product Composition

(78) In an embodiment, stream 3 which is a hydroformylation product stream can have a composition which is greater than 25 wt. % branched aldehydes.

(79) Hydroformylation

(80) The second step of the two-step process depicted in Figure A occurs in Hydroformylation Reactor 200. In this step, the feed (Stream 2) has a composition comprising: A C4-C36 olefin mixture containing; >20 wt. % linear internal olefins, <80 wt. % linear alpha olefins; Rhodium catalyst A, Carbon Monoxide (CO), Hydrogen, and C5-C37 Aldehydes (minor components).

(81) Optionally, stream 2 can comprise a high-boiling inert solvent.

(82) The reaction in Hydroformylation Reactor 200 proceeds using the same Rhodium Catalyst A and at a temperature of 30-300 C. The reaction in Hydroformylation Reactor 200 occurs under a CO/H2 atmosphere and at a pressure greater than the pressure in Isomerization Reactor (100) as the higher pressure favors the production of the desired branched aldehydes. This step produces a reaction product (Stream 3) where the olefin mixture (or a portion of the olefin mixture) has been hydroformylated to produce an aldehyde mixture comprising: >25 wt. % branched aldehydes, and <75 wt. % linear aldehydes.

(83) In an embodiment, the feed to hydroformylation having an internal olefin, or having a mixture alpha olefins and internal olefins, can be hydroformylated at a temperature in a range of 30? C. to 500? C., or 40? C. to 200? C., or 50? C. to 120? C., such as in non-limiting example 30? C., 50? C., 80? C., 90? C., 100? C., 120? C., 150? C., 180? C., 200? C., 250? C., 300? C., 400? C., or 500? C.

(84) In an embodiment, the feed to hydroformylation having an internal olefin, or having a mixture of alpha olefins and internal olefins, can be hydroformylated at a pressure in a range of 0 bar(g) to 500 bar(g), 5 bar(g) to 100 bar(g), 7 bar(g) to 30 bar(g), such as in non-limiting example 0 bar(g), 1 bar(g), 5 bar(g), 7 bar(g), 10 bar(g), 15 bar(g), 30 bar(g), 50 bar(g), 100 bar(g), 150 bar(g), 200 bar(g), 250 bar(g), 300 bar(g), 350 bar(g), 400 bar(g), 500 bar(g).

(85) In an embodiment, the feed having an alpha olefin, or having a mixture of linear olefins, can be hydroformylated at a pressure of 15 bar(g) and 90? C.

(86) Stream 2 may also contain a small portion of mixed aldehydes of carbon number C5-C37 produced from hydroformylation of the C4-C36 alpha olefins and C4-C36 internal olefins. The production of aldehydes in Isomerization Reactor (100) is not an intended purpose but is to be expected to occur at low rates. Production of aldehydes in this step should be controlled at a low level as aldehydes formed in this step tend to be disproportionately linear aldehydes rather than the desired branched aldehydes.

(87) FIG. 2 shows an embodiment of a chemical manufacturing process having an isomerization reactor 100 and which uses a Stream 4, which is optional, and which is an isomerization reactor bypass that can be used to control the feed composition to the hydroformylation reactor 200. In the embodiment of FIG. 2, isomerization reactor products Stream 2 is blended with the isomerization reactor bypass stream of Stream 4 to produce Stream 6 which is a hydroformylation reactor feed stream of the embodiment of FIG. 2.

(88) FIG. 2 describes the two-step process of FIG. 1 in an embodiment that has Stream 4, which is an optional olefin bypass stream around Isomerization Reactor (100). In this manner a portion of Stream 1 can be bypassed around the Isomerization Reactor (100) as Stream 4 and a portion of Stream 1 is fed to Isomerization Reactor (100) as Stream 5. Stream 2 is the isomerized output of Isomerization Reactor (100) and is combined with Stream 4 to provide Stream 6, which is the reactor feed to Hydroformylation Reactor 200. The bypass functionality of Stream 4 provides a convenient and effective means to control the degree of olefin isomerization in the process. By adjusting the portion of Stream 1 that is isomerized (Stream 5) and the portion of Stream 1 that is not isomerized (Stream 4) the degree of olefin isomerization can be controlled to a specified, desired value. The degree of olefin isomerization is a key variable in determining the degree of aldehyde branching achieved. Thus, by controlling the degree of olefin isomerization, one can control the degree of aldehyde branching achieved in Stream 3 to a specified, desired value.

(89) In the embodiment of FIG. 2, the compositions of Stream 1, the isomerization reactor bypass stream of Stream 4 and Stream 5 can be the same. As shown in FIG. 2, Stream 4 and Stream 5 are streams split from Stream 1.

(90) Stream 1Alpha Olefin Feed Composition

(91) Stream 2Isom. Reactor Product (>20% internal olefins) Composition

(92) Stream 3Hydroformylation Product (>25% branching) Composition

(93) Stream 4Isom. Reactor Bypass (optional) Composition

(94) Stream 5Isom. Reactor Feed Composition

(95) Stream 6Hydroformylation Reactor Feed Composition

(96) FIG. 3 shows an embodiment of a chemical manufacturing process having an isomerization reactor, a hydroformylation reactor and catalyst recovery. In this nonlimiting embodiment, the process of FIG. 2 is modified by the addition of a catalyst recovery step, Catalyst Recovery 300, which recovers the rhodium catalyst and produces Stream 7 which is a recovered rhodium catalyst stream that is recycled back to the isomerization reactor 100 and produces Stream 8 having a composition of branched aldehydes and unreacted olefins. Stream 8 is a branched aldehydes and unreacted olefins product stream.

(97) FIG. 3 the process of FIG. 2 with the addition of catalyst recovery 300. Stream 3 is the reactor product of Hydroformylation Reactor 200 and has a stream 3 composition having: A C5-C37 aldehyde mixture comprising: >25 wt. % branched aldehydes, and <75 wt. % linear aldehydes; Unreacted C4-C36 olefins; Unreacted CO/H2; and Rhodium catalyst A.

(98) In an embodiment the stream 3 composition can optionally comprise a high-boiling inert solvent.

(99) In the Catalyst Recovery 300 step, unreacted CO/H2 gases are vented off, and the aldehyde mixture and unreacted olefins are distilled overhead under reduced pressure, for example <0.1 bar (absolute) and elevated temperature, for example 100-200? C., to produce overhead liquid Stream 8. In an embodiment, the olefins fed to hydroformylation reactor 200 are completely (or nearly completely) converted to aldehydes in Hydroformylation Reactor 200 and Stream 8 will be a mixed aldehyde product stream not requiring further purification.

(100) In the embodiment of FIG. 3, the non-volatile liquid residue from Catalyst Recovery 300 is shown as Stream 7 which has the recovered rhodium Catalyst A and optionally the high-boiling inert solvent, if such solvent is used. Stream 7, the recovered rhodium catalyst stream, is then recycled back to isomerization reactor 100 for re-use in the process. While it is not required for the invention to include a high-boiling inert solvent in the system, it is often convenient to do so in order to provide a convenient liquid carrier for the recovered rhodium catalyst. Polyalphaolefins (PAO's) are an example of such a high boiling inert solvent.

(101) Stream 1Alpha Olefin Feed Composition.

(102) Stream 2Isom. Reactor Product Composition.

(103) Stream 3Hydroformylation Product Composition.

(104) Stream 4Isom. Reactor Bypass Composition.

(105) Stream 5Isom. Reactor Feed Composition.

(106) Stream 6Hydroformylation Reactor Feed Composition.

(107) Stream 7Recovered Rhodium Catalyst Stream Composition.

(108) Stream 8Branched Aldehydes/Unreacted Olefins Composition.

(109) FIG. 4 shows the process of FIG. 3 to which an aldehyde distillation unit 400 has been added. FIG. 4 shows an embodiment of a chemical manufacturing process having an isomerization reactor, a hydroformylation reactor, catalyst recovery and aldehyde distillation.

(110) FIG. 4 shows the process of FIG. 3 with the addition of an aldehyde distillation step shown an aldehyde distillation 400. In this embodiment, Stream 8 is the feed stream to Aldehyde. Distillation (400) and can in an embodiment have a composition of, e.g.: 1. A C5-C37 aldehyde mixture containing, >25 wt. % branched aldehydes, <75 wt. % linear aldehydes; and 2. Unreacted C4-C36 olefins.

(111) In the embodiment of FIG. 4, during the distillation process of aldehyde distillation 400, unreacted C4-C36 olefins which were not converted to aldehydes in the hydroformylation reactor 200 are distilled overhead as a lights product shown as Stream 9 having unreacted olefin. The unreacted olefins of Stream 9 are recycled back to the beginning of the process and in the embodiment of FIG. 4 are blended with Stream 1. As shown, the unreacted olefins of Stream 9 are combined with the alpha olefin feed Stream 1 to create a Stream 10 which is a mixed olefins feed to the Isomerization Reactor 100.

(112) In the embodiment of FIG. 4, the C5-C37 aldehyde mixture of Stream 8 produced by catalyst recovery 300 is further refined and purified by distillation in aldehyde distillation 400 to produce a distilled, high purity C5-C37 branched aldehyde product stream shown as Stream 11 which in an embodiment is free of, or nearly free of, unreacted C4-C36 olefins.

(113) Stream 1Alpha Olefin Feed Composition.

(114) Stream 2Isom. Reactor Product Composition.

(115) Stream 3Hydroformylation Product Composition.

(116) Stream 4Isom. Reactor Bypass Composition.

(117) Stream 5Isom. Reactor Feed Composition.

(118) Stream 6Hydroformylation Reactor Feed Composition.

(119) Stream 7Recovered Rhodium Catalyst Stream Composition.

(120) Stream 8Branched Aldehydes/Unreacted Olefins Composition.

(121) Stream 9Unreacted Olefins Composition.

(122) Stream 10Mixed Olefins Feed Composition.

(123) Stream 11Branched Aldehydes Product Composition.

(124) FIG. 5 shows an embodiment of a chemical manufacturing process having an isomerization reactor, a hydroformylation reactor, catalyst recovery and an aldehyde hydrogenation reactor.

(125) FIG. 5 shows a different embodiment modifying the process of FIG. 3 in which Stream 8 is fed to an aldehyde hydrogenation reactor 500 which produces branched alcohols as Stream 9 which is a branched alcohols product stream.

(126) FIG. 5 shows the process of FIG. 3 with the addition of an aldehyde hydrogenation step shown as aldehyde hydrogenation reactor 500. In an embodiment, Stream 11 is the feed stream to the Aldehyde Hydrogenation Reactor (500) and can have a composition, e.g.: 1. A C5-C37 aldehyde mixture containing, a. >25 wt. % branched aldehydes, b. <75 wt. % linear aldehydes, and 2. Unreacted C4-C36 olefins.

(127) In the embodiment of FIG. 5, the C5-C37 aldehydes are hydrogenated in the Aldehyde Hydrogenation Reactor (500) in the presence of hydrogen and a hydrogenation catalyst to produce Stream 12. Stream 12 is a branched alcohols product and in an embodiment can have a composition comprising: 1. A C5-C37 alcohol mixture containing, a. >30 wt. % branched alcohols, b. <70 wt. % linear alcohols, and 2. C4-C36 paraffins (alkanes).

(128) In the embodiment of FIG. 5, the C5-C37 alcohols are produced from the hydrogenation of the corresponding aldehydes in aldehyde hydrogenation reactor 500 and the C4-C36 paraffins also produced in aldehyde hydrogenation reactor 500 resulting from the hydrogenation of the unreacted C4-C36 olefins contained in Stream 8.

(129) Optionally, the C5-C37 alcohols content (purity) can be increased in Stream 12, with a related decrease in the C4-C36 paraffin content by using an optional distillation step after aldehyde hydrogenation reactor 500 to remove the low-boiling C4-C36 paraffins and produce a distilled, high purity C5-C37 Branched Alcohols Product which is free of, or nearly free of, C4-C36 paraffins.

(130) Stream 1Alpha Olefin Feed Composition.

(131) Stream 2Isom. Reactor Product Composition.

(132) Stream 3Hydroformylation Product Composition.

(133) Stream 4Isom. Reactor Bypass Composition.

(134) Stream 5Isom. Reactor Feed Composition.

(135) Stream 6Hydroformylation Reactor Feed Composition.

(136) Stream 7Recovered Rhodium Catalyst Stream Composition.

(137) Stream 8Branched Aldehydes/Unreacted Olefins Composition.

(138) Stream 12, Branched Alcohols Product.

(139) In an embodiment, Stream 12 can be a branched alcohols product composition having greater than 25% branching.

(140) FIG. 6 shows an embodiment of a chemical manufacturing process having an isomerization reactor, a hydroformylation reactor, catalyst recovery, aldehyde distillation and an aldehyde hydrogenation reactor. FIG. 6 shows the process of FIG. 4 with the addition of an aldehyde hydrogenation reactor 500. In the embodiment of FIG. 6, Stream 11, the branched aldehyde product stream, is the feed stream to the Aldehyde Hydrogenation Reactor (500) and can have a C5-C37 aldehyde mixture containing, e.g.: 1. >25 wt. % branched aldehydes, and 2. <75 wt. % linear aldehydes.

(141) In the embodiment of FIG. 6, in the Aldehyde Hydrogenation Reactor (500), the C5-C37 aldehydes are hydrogenated in the presence of hydrogen and a hydrogenation catalyst to produce Stream 12.

(142) Examples of suitable hydrogenation catalysts are supported base metal catalysts on high surface area supports such as ceramics, carbons, aluminas, silicas, titanias and zirconias, where the metal is affixed to and dispersed on the surface of the support such as those whose primary base metal components consist of nickel, cobalt, copper, manganese, molybdenum, zinc and/or iron or varied combinations thereof. As an example, for the base metal nickel: nickel on alumina catalysts, nickel on silica catalysts, nickel on titania catalysts, nickel on zirconia catalysts or nickel on carbon catalysts. Analogous supported metal catalysts can be found for the other base metals. Supported precious metal catalysts on high surface area supports such as ceramics, carbons, aluminas, silicas, titanias and zirconias, where the metal is affixed to and dispersed on the surface of the support, are also suitable, including those of whose metals consist of platinum, palladium, gold, silver, iridium and ruthenium or varied combinations thereof. As an example, for the precious metal platinum: platinum on carbon, platinum on silica, platinum on titania, platinum on zirconia or platinum on alumina catalysts. Analogous supported precious metal catalysts can be found for the other precious metals. Raney? nickel catalysts and Raney? cobalt catalysts from W. R. Grace & Co. (7500 Grace Drive, Columbia, MD 21044, US, phone 1-410-531-4000) are also suitable hydrogenation catalysts. Suitable hydrogenation catalysts can either be finely divided slurry-type catalysts for use in stirred batch reactors or continuously stirred tank reactors (i.e. CSTR's) or can be fixed-bed type catalysts for use in reactors such as trickle-bed reactors.

(143) Stream 12 is a branched alcohols product stream and can have a C5-C37 alcohol composition of, e.g.: 1. >30 wt. % branched alcohols, and 2. <70 wt. % linear alcohols.

(144) In the embodiment of FIG. 6, the C5-C37 alcohols are produced from the hydrogenation of the corresponding aldehydes which are the reaction products of the hydroformylation reactor 200.

(145) Optionally, the C5-C37 alcohols content (purity) in Stream 12 can be increased and the level of any undesired impurities decreased, for example low levels of C4-C36 paraffins, by adding a distillation step after aldehyde hydrogenation reactor 500 to remove such impurities and produce a purified, distilled C5-C37 Branched Alcohols Product.

(146) Stream 1Alpha Olefin Feed Composition.

(147) Stream 2Isom. Reactor Product Composition.

(148) Stream 3Hydroformylation Product Composition.

(149) Stream 4Isom. Reactor Bypass Composition.

(150) Stream 5Isom. Reactor Feed Composition.

(151) Stream 6Hydroformylation Reactor Feed Composition.

(152) Stream 7Recovered Rhodium Catalyst Stream Composition.

(153) Stream 8Branched Aldehydes/Unreacted Olefins Composition.

(154) Stream 9Unreacted Olefins Composition.

(155) Stream 10Mixed Olefins Feed Composition.

(156) Stream 11Branched Aldehydes Product Composition.

(157) Stream 12Branched Alcohols Product (>30% branching)

Example 1

Introduction

(158) In an embodiment, isomerization hydroformylation and hydrogenation reactions produce two branched alcohol products based on two starting alpha olefins. Optionally a mixture of a number of alpha olefins can be used.

(159) In an embodiment a first alpha olefin, 1-Dodecene, can be converted through the process chemistry described herewith to a mixture of branched tridecanols, while the second alpha olefin, 1-Tetradecene, is converted through analogous process chemistry to a mixture of branched pentadecanols.

(160) The process can be run batchwise, or as a continuous process.

Batch Process Embodiment

(161) In an embodiment, the first step in the process can be the batch-wise isomerization of the individual alpha olefins at moderate temperatures and pressures utilizing a homogeneous rhodium organophosphorus ligand catalyst system. The second step can be a hydroformylation with the same rhodium organophosphorus ligand catalyst system that proceeds with high yield and selectivity to the corresponding branched tridecanals and branched pentadecanals. For example, the branched tridecanals product from such an isomerization and hydroformylation process would yield a composition comprising a mixture of linear 1-tridecanal and 2-alkyl branched tridecanal isomers, i.e.:

(162) TABLE-US-00003 TABLE 1 1-Dodecene Isomerization and Hydroformylation Reaction Products No. 1 1-Tridecanal CAS No. 10486-19-8 C.sub.13H.sub.26O MW 198.34 No. 2 2-Methyl Dodecanal CAS No. 37596-36-4 C.sub.13H.sub.26O MW 198.34 No. 3 2-Ethyl Undecanal CAS No. 35518-76-4 C.sub.13H.sub.26O MW 198.34 No. 4 2-Propyl Decanal CAS No. C.sub.13H.sub.26O MW 198.34 No. 5 2-Butyl Nonanal CAS No. 65899-14-1 C.sub.13H.sub.26O MW 198.34 No. 6 2-Pentyl Octanal CAS No. C.sub.13H.sub.26O MW 198.34

(163) In an embodiment, the catalyst used in the isomerization and hydroformylation reactions is an organometallic rhodium ligand complex formed from Rh(CO)2ACAC ((Acetylacetonato)dicarbonylrhodium(I)) and tris (2,4,-di-t-butylphenyl) phosphite ligand.

(164) After completion of the hydroformylation batch chemistry, the crude aldehydes can be flashed distilled to remove the high value catalyst ligand complex for recycle. The flashed aldehydes vapor can be fed directly to distillation to provide a high purity branched aldehyde intermediate.

(165) In this embodiment, the branched tridecanals and pentadecanals can be separately batch hydrogenated at high pressures and moderate temperature in the presence of a hydrogenation catalyst such as a base metal catalyst, a supported nickel catalyst, a Raney? (W. R. Grace & Co., 7500 Grace Drive, Columbia, MD 21044, US, phone 1-410-531-4000) nickel catalyst or a precious metal catalyst. During hydrogenation, the aldehyde functionality will be converted into the equivalent alcohol, producing the desired branched tridecanols and the desired branched pentadecanols.

(166) In a batch reaction embodiment, the isomerization and hydroformylation reactions can be performed in the same or different reactors.

(167) If the same reactor is used for both the isomerization and hydroformylation reactions, the isomerization can be executed under one set of reaction conditions and the hydroformylation can be executed under a different set of reaction conditions. The reaction temperatures of the isomerization and hydroformylation reactions can be the same or different. The reaction pressures of the isomerization and hydroformylation reactions can be the same or different. In one embodiment, the hydroformylation reaction is conducted at a higher pressure than the isomerization reaction.

(168) In one embodiment, the batchwise hydroformylation reaction will be performed at moderate temperatures of 80? C. to 100? C. and at a moderate pressure of 15-20 bar(g), In this embodiment, the flash removal of the branched aldehydes can be performed in a flash unit operation, e.g. flash drum, optionally in conjunction with a distillation column. In another embodiment, the flash removal of the branched aldehydes can be performed in an evaporator unit operation, e.g. a wiped-film evaporator or a falling film evaporator, optionally in conjunction with a distillation column. The optional distillation can be performed at pressures including variable vacuums down from 1 millibar absolute to 999 millibar absolute, such as in nonlimiting example 5 millibar absolute, 10 millibar absolute, or 20 millibar absolute, or 50 millibar absolute, or 100 millibar absolute, or 500 millibar absolute, or higher.

(169) In an embodiment the hydrogenation of the branched aldehyde intermediate(s) will be performed in a batch reactor at hydrogen pressures of between 10 bar(g) and 100 bar(g) e.g. 20 bar(g), 30 bar(g), 40 bar(g), 50 bar(g), 60 bar(g), 70 bar(g), 80 bar(g), 90 bar(g), or higher. This hydrogenation can be performed at temperatures between 50? C. and 300? C., e.g. 50? C., 100? C., 150? C., 200? C., 250? C., 300? C., 350? C., 400? C., 450? C.

(170) In an embodiment, the reaction of the reactants will be considered complete once there is less than 1% of the Branched Aldehyde intermediate remaining. In an embodiment, the reaction of the reactants will be considered complete once there is less than 0.1% of the Branched Aldehyde intermediate remaining. In this embodiment, the filtered crude Branched Alcohol would be a low color, high purity (>97%), highly branched (>80%) product.

(171) In an embodiment, branched alcohols products can be manufactured from the alpha olefin feeds through a batch isomerization process, a batch hydroformylation process, followed by flash distillation to produce the Branched Aldehydes intermediates. The Branched Aldehydes intermediates will then be batch hydrogenated and the product will be filtered to remove the hydrogenation catalyst to produce the finished Branched Alcohols.

Example 2: Preparation of a Branched C13 Alcohol Product

(172) A C12 linear alpha olefin feedstock (1-Dodecene) was obtained from the Chevron Phillips Chemical Company LP, as identified by product name AlphaPlus? 1-Dodecene (Chevron Phillips Chemical Company LP, P.O. Box 4910, The Woodlands, TX 77387-4910, US, phone (800) 231-3260). The homogeneous rhodium organophosphorus catalyst used in this example is prepared in a high pressure, stainless steel stirred autoclave. To the autoclave was added 0.027 wt % Rh(CO)2ACAC ((Acetylacetonato)dicarbonylrhodium(I)), 1.36 wt. % tris (2,4,-di-t-butylphenyl) phosphite ligand and 98.62 wt. % Synfluid? PAO 4 cSt (Chevron Phillips Chemical Company LP, P.O. Box 4910, The Woodlands, TX 77387-4910, phone (800) 231-3260) inert solvent. The mixture was heated at 80? C. in the presence of a CO/H2 atmosphere and 2 bar(g) pressure for four hours to produce the active rhodium catalyst solution (109 ppm rhodium, P:Rh molar ratio=20). The 1-Dodecene linear alpha olefin was added to the rhodium catalyst solution in the autoclave producing a starting reaction mixture with a rhodium concentration of 35 ppm. The alpha olefin feed was then isomerized at 80? C. in the presence of a CO/H2 atmosphere and 1 bar(g) pressure for 10 hours. The isomerized olefin was then hydroformylated at 70? C. in the presence of a CO/H2 atmosphere and 20 bar(g) pressure for 8 hours. The molar ratio of CO to H2 in both the isomerization step and the hydroformylation step was equal to 1:1.15. The resulting hydroformylation reaction product was flash distilled at 140-150? C. and 25 millibar to recover the rhodium catalyst solution as a bottoms product and recover a branched C13 Aldehyde overheads product with a composition comprising:

(173) TABLE-US-00004 Weight % 1-Tridecanal 13.9% 2-Methyl-dodecanal 28.3% 2-Ethyl-undecanal 15.2% 2-Propyl-decanal 14.5% 2-Butyl-nonanal 13.6% 2-Pentyl-octanal 12.6% TOTAL 98.0%

(174) The weight % branching in the branched C13 aldehyde product was 86.2%.

(175) The branched C13 aldehyde product was hydrogenated in a high pressure, Inconel 625 stirred autoclave at 150 C and 20 bar(g) hydrogen pressure. The hydrogenation catalyst used was a Raney? Nickel 3111 (W. R. Grace & Co., 7500 Grace Drive, Columbia, MD 21044, US, phone 1-410-531-4000) catalyst used at a 0.25 wt. % loading. The aldehyde was hydrogenated for 10 hours and the resultant reaction mixture was filtered to produce a branched C13 alcohol product comprising:

(176) TABLE-US-00005 Weight % 1-Tridecanol 13.2% 2-Methyl-dodecanol 29.1% 2-Ethyl-undecanol 15.5% 2-Propyl-dedanol 14.4% 2-Butyl-nonanol 13.2% 2-Pentyl-octanol 12.9% TOTAL 98.4%

(177) The weight % branching in the branched C13 alcohol product was 86.6%.

Example 3: Preparation of a Branched C15 Alcohol Product

(178) The recovered rhodium catalyst stream from Example 2 was charged to a high pressure, stainless steel stirred autoclave and a C14 linear alpha olefin feedstock (1-Tetradecene) from the Chevron Phillips Chemical Company LP, (AlphaPlus? 1-Tetradecene by Chevron Phillips Chemical Company LP, P.O. Box 4910, The Woodlands, TX 77387-4910, phone (800) 231-3260) was added. The resulting mixture had a rhodium concentration of approximately 30 ppm. The 1-tetradecene linear alpha olefin was then isomerized at 80? C. in the presence of a CO/H2 atmosphere and 1 bar(g) pressure for 12 hours. The isomerized olefin was then hydroformylated at 70? C. in the presence of a CO/H2 atmosphere and 20 bar(g) pressure for 8 hours. The resulting reaction product was flash distilled at 150-160? C. and 25 millibar to recover the rhodium catalyst solution as a bottoms product and recover a branched C15 Aldehyde overheads product. The recovered rhodium catalyst solution was then used again to complete a second 1-tetradecene batch isomerization (4 hours) and hydroformylation (6 hours). The resulting C15 aldehyde products from the two batches were combined to give a branched C15 Aldehyde product comprising:

(179) TABLE-US-00006 Weight % 1-Pentadecanal 12.1% 2-Methyl-tetradecanal 34.1% 2-Ethyl-tridecanal 21.9% 2-Propyl-dodecanal 14.0% 2-Butyl-undecanal 8.6% 2-Pentyl-decanal + 2-hexyl-nonanal 9.0% TOTAL 99.6%

(180) The weight % branching in the branched C15 aldehyde product was 87.8%.

(181) The branched C15 aldehyde product was hydrogenated in a high pressure, Inconel 625 stirred autoclave at 150 C and 20 bar(g) hydrogen pressure. The hydrogenation catalyst used was a Raney? Nickel 3111 (W. R. Grace & Co., 7500 Grace Drive, Columbia, MD 21044, US, phone 1-410-531-4000) catalyst used at a 0.25 wt. % loading. The aldehyde was hydrogenated for 10 hours and the resultant reaction mixture was filtered to produce a branched C15 alcohol product comprising:

(182) TABLE-US-00007 Weight % 1-Pentadecanol 13.7% 2-Methyl-tetradecanol 33.8% 2-Ethyl-tridecanol 21.4% 2-Propyl-dodecanol 12.4% 2-Butyl-widecanol 8.0% 2-Pentyl-decanol + 2-hexyl-nonanal 9.2% TOTAL 98.4%

(183) The weight % branching in the branched C15 alcohols product was 86.1%.

Example 4: Preparation of a Branched C15 Aldehyde Product

(184) A C14 linear alpha olefin feedstock (1-Tetradecene) was obtained from the Chevron Phillips Chemical Company LP, as identified by product name AlphaPlus? 1-Tetradecene (Chevron Phillips Chemical Company LP, P.O. Box 4910, The Woodlands, TX 77387-4910, US, phone (800) 231-3260). The homogeneous rhodium organophosphorus catalyst used in this example is an organometallic complex of Rh(CO)2ACAC ((Acetylacetonato)dicarbonylrhodium(I)) and triphenylphosphine ligand. The 1-Tetradecene linear alpha olefin was added to the rhodium catalyst solution in a stainless steel autoclave producing a starting reaction mixture with a rhodium concentration of 35 ppm and a P:Rh molar ratio=20. The alpha olefin feed was then isomerized at 80? C. in the presence of a CO/H2 atmosphere and 1.5 bar(g) pressure for 3.5 hours. The isomerized olefin was then hydroformylated at 95? C. in the presence of a CO/H2 atmosphere and 14 bar(g) pressure for 9 hours. The molar ratio of CO to H2 in both the isomerization step and the hydroformylation step was equal to 1:1.15. The resulting hydroformylation reaction product was flash distilled at 140-150? C. and 5 millibar to recover a branched C15 Aldehyde overheads product with aldehyde composition comprising:

(185) TABLE-US-00008 Weight % 1-Pentadecanal 52.5% 2-Methyl-tetradecanal 33.1% 2-Ethyl-tridecanal 10.8% 2-Propyl-dodecanal 1.6% 2-Butyl-undecanal 0.6% 2-Pentyl-decanal + 2-hexyl-nonanal 0.9% TOTAL 99.4%

(186) The weight % branching in the branched C15 aldehyde product was 47.2%.

CONCLUSION

(187) This disclosure regards branched compounds and methods for producing and manufacturing branched compounds in their many aspects, features and elements. Such compounds and manufacturing processes can be dynamic in its use and operation. This disclosure is intended to encompass the equivalents, means, systems and methods of the use of the branched alcohols and methods for producing and manufacturing branched alcohols and their many aspects consistent with the description and spirit of the apparatus, means, methods, functions and operations disclosed herein. Other embodiments and modifications will be recognized by one of ordinary skill in the art as being enabled by and within the scope of this disclosure.

(188) The scope of this disclosure is to be broadly construed. The embodiments herein can be used together, separately, mixed or combined. It is intended that this disclosure disclose equivalents, means, systems and methods to achieve the devices, designs, operations, control systems, controls, activities, mechanical actions, dynamics and results disclosed herein. For each compound, process, method, manufacturing method, mechanical element or mechanism disclosed, it is intended that this disclosure also encompasses within the scope of its disclosure and teaches equivalents, means, systems and methods for practicing the many aspects, compounds, processes, mechanisms and devices disclosed herein. The claims of this application are likewise to be broadly construed.

(189) The description of the technology herein in its many and varied embodiments is merely exemplary in nature and, thus, variations that do not depart from the gist of the disclosure are intended to be within the scope of the claims and the disclosure herein. Such variations are not to be regarded as a departure from the spirit and scope of the disclosed technologies.

(190) It will be appreciated that various modifications and changes can be made to the above described embodiments of the processes and resulting branched alcohols as disclosed herein without departing from the spirit and the scope of the claims.