НОВЫЙ АЛИЦИКЛИЧЕСКИЙ СПИРТ

Настоящее изобретение относится к новому алициклическому спиртовому соединению, представленному химической формулой (1), которое может быть использовано в качестве исходного материала для парфюмерного состава и которое обладает превосходным цветочно-травянистым ароматом с бодрящими свежими нотами. Также изобретение относится к парфюмерной композиции, содержащей заявленное алициклическое спиртовое соединение, и к способу его получения. Способ получения заключается во взаимодействии 4-изопропил-1-метилциклогексена с монооксидом углерода в присутствии фторида водорода, изомеризации получаемого фторида 4-изопропил-1-метилциклогексанкарбоновой кислоты с получением 2-метил-2-(4-метилциклогексил)пропионилфторида, с последующим его взаимодействием со спиртом и получением карбонильного соединения циклогексана, и затем восстановлением карбонильного соединения циклогексана. 3 н.п. ф-лы, 4 пр.

КОМПОЗИЦИИ ЭТАНОЛА

Настоящее изобретение относится к вариантам композиции этанола для смешения с топливом. В одном из вариантов предлагаемая композиции включает по меньшей мере, 92 масс. % этанола; от 95 частей на миллион (ч./млн) по массе до 1000 ч./млн по массе изопропанола; и н-пропанол, где массовое соотношение изопропанола к н-пропанолу составляет по меньшей мере 0,5:1. В другом из предложенных вариантов композиция включает вышеуказанные компоненты и ее получают посредством гидрирования уксусной кислоты в присутствии катализатора для образования неочищенного этанольного продукта, содержащего этанол, изопропанол, и одну или более примесей и отделения по меньшей мере части неочищенного этанольного продукта для удаления одной или более примесей и извлечения композиции этанола. 11 н. и 6 з.п. ф-лы, 3 ил., 11 табл., 4 пр.

ДВУХСТАДИЙНЫЙ СПОСОБ ГИДРИРОВАНИЯ МАЛЕИНОВОЙ КИСЛОТЫ В 1,4-БУТАНДИОЛ

Изобретение относится к усовершенствованному способу (вариантам) конверсии малеиновой кислоты в 1,4-бутандиол, гамма-бутиролактон и/или тетрагидрофуран. Способ получения по меньшей мере одного из продуктов, выбранного из группы, включающей гамма-бутиролактон, 1,4-бутандиол и тетрагидрофуран, включает в себя следующие операции: создание первой зоны гидрирования и второй зоны гидрирования, соединенных последовательно; подача в первую зону гидрирования потока сырья, который содержит малеиновую кислоту; проведение реакции в первой зоне гидрирования исходной малеиновой кислоты и водорода в контакте с катализатором для получения продукта реакции, содержащего янтарную кислоту; подача во вторую зону гидрирования продукта реакции из первой зоны гидрирования; проведение реакции во второй зоне гидрирования продукта реакции из первой зоны гидрирования и водорода в контакте с катализатором для получения потока продукта, который содержит по меньшей мере один из продуктов из группы, которая включает гамма-бутиролактон ...

СПОСОБ ПОЛУЧЕНИЯ ЭТИЛЕНГЛИКОЛЯ

... 1. Способ получения этиленгликоля при использовании сырья, содержащего оксалат, и катализатора, содержащего медь и/или оксид меди, включающий:введение сырья в контакт с катализатором в реакторе при температуре от приблизительно 170 до приблизительно 270°С, массовой часовой объемной скорости оксалата от приблизительно 0,2 до приблизительно 7 час, молярному соотношению между водородом и оксалатом от приблизительно 20:1 до приблизительно 200:1 и давлению реакции от приблизительно 1,5 до приблизительно 10 МПа в целях получения потока, содержащего этиленгликоль,причем реактор представляет собой трубчатый реактор, использующий секционированный теплообмен и применяющий внешние и внутренние трубы, сконфигурированные в виде двухтрубной конструкции для улучшения теплообмена катализатора.2. Способ получения этиленгликоля по п.1, где температура реакции в реакторе находится от приблизительно 180 до приблизительно 260°С; массовая часовая объемная скорость оксалата от приблизительно 0,3 до приблизительно ...

Способ получения амидов бифенилмасляной кислоты

Способ получения 4-(4-бифенилил)1-бутанола

СПОСОБ ПОЛУЧЕНИЯ 4-

VERFAHREN ZUM DIREKTEN HYDRIERUNG VON CARBONSÄUREESTERN

VERFAHREN ZUR HERSTELLUNG VON ZUCKERALKOHOLEN

A WATER-IN-OIL TYPE COSMETIC COMPOSITION AND AN EMULSIFIER COMPOSITION

VERFAHREN ZUR HERSTELLUNG VON FETTALKOHOLEN AUF PFLANZLICHER BASIS DURCH FRAKTIONIERUNG

Process for the direct hydrogenation of glyceride oils in the pressure range from 20 to 49.9 bar

In the direct catalytic hydrogenation of glyceride oils, glyceride oils are reacted continuously together with hydrogen at pressures from 20 to 49.9 bar and at temperatures from 180 to 270@C at molar ratios of hydrogen : fatty acid radicals in the glyceride oil starting material of 10 : 1 to 500 : 1 on catalysts which contain 30 to 40% by weight of copper, 23 to 30% by weight of chromium, 1 to 10% by weight of manganese, 1 to 10% by weight of silicon and 1 to 7% by weight of barium - the % by weight in each case being based on oxidic catalyst mass - and, if desired, further transition metals in the form of their oxides, and have been converted after the calcination of the components forming the catalyst mass with 1 to 10% by weight - based on oxidic catalyst - of at least one binder in addition to 1 to 10% by weight of graphite to give lumpy and/or granular moulded articles and activated with hydrogen or a hydrogen-containing gas mixture.

HYDROGENOLYSE VON C-5-ZUCKERN UND C-5-ZUCKERALKOHOLEN

Verfahren zur Herstellung von Methanol

Process for the preparation of chiral 2-methyl-1,4-butanediol

There is described a simple preparation process for chiral 2-methyl-1,4-butanediol, which is characterised in that chiral 2-methylsuccinic acid diester is hydrogenated in the presence of a heterogeneous catalyst at temperatures of not more than 220@C and under such conditions that the hydrogenation rate of the chiral 2-methylsuccinic acid diester is at most 97%, in that the said monohydric alcohol, residual chiral 2-methylsuccinic acid diester and chiral 2-methyl-1,4-butanediol formed are separated off from a part or the entire reaction mixture and collected and in that the said chiral 2-methylsuccinic acid diester collected is subjected again to the said heterogeneous catalytic hydrogenation reaction.

Process for the direct hydrogenation of triglycerides

In the direct catalytic hydrogenation of triglycerides, triglycerides are reacted continuously with hydrogen at pressures of from 50 to 300 bar and at temperatures of from 160 to 250 DEG C at molar ratios of hydrogen : fatty acid radicals in the triglyceride starting material of from 10 : 1 to 500 : 1 over catalysts which contain from 30 to 40 % by weight of copper, from 23 to 30 % by weight of chromium and from 1 to 7 % by weight of barium - % by weight in each case relative to oxidic catalyst composition - and if desired further transition metals in the form of their oxides and, after the calcination of the components forming the catalyst composition, have been converted with 1 to 10 % by weight - relative to oxidic catalyst - of at least one binder to give lumpy and/or granular moulded articles and activated with hydrogen or a hydrogen-containing gas mixture.

Verfahren zur Herstellung von Diolen durch Hydrierung eines Carbonsäure enthaltenden Gemisches mittels Kobalt enthaltenden Katalysatoren

Die vorliegende Erfindung betrifft ein Verfahren zur Herstellung von Diolen durch Hydrierung eines Carbonsäure, Carbonsäureanhydride und/oder Carbonsäureester/Lactone enthaltenden Gemischs mit Hilfe eines Kobalt enthaltenden Katalysators, wobei dem Hydrierzulauf Alkali- und/oder Erdalkaliionen hinzugefügt werden und Alkali- und/oder Erdalkaliionen von Mineralsäuren ausgeschlossen sind.

Production of an ester compound of low sulfur content comprises reaction of a fatty acid, derived from natural fats or oils, with an alcohol followed by the adsorption of the resulting ester compound using clay and/or activated carbon

A process for the production of an ester compound (I) comprises reaction of a fatty acid, derived from natural fats or oils, with a 1-4C alcohol followed by the adsorption of the resulting ester compound using at least one adsorbent, comprising clay and/or activated carbon. An Independent claim is included for a process for producing an alcohol by hydrogenation of the ester compound (I).

Verfahren zur Herstellung von Hydroxymethyl-cyclopropan

CYCLOALIPHATIC ALCOHOLS

VERFAHREN ZUR ENTFERNUNG VON SULFAT AUS GLYKOLSAEURE

Verfahren zur Herstellung von Alkoholen

VERFAHREN ZUR HERSTELLUNG VON BUTAN-1,4-DIOL, GAMMA-BUTYROLACTONE UND TETRAHYDROFURAN

VERFAHREN ZUR VERBESSERUNG DER WAERMEABFUEHRUNG BEI KATALYTISCHEN HYDRIERUNGEN

PROCESS

Process for reducing fatty acids and esters thereof

... Fatty oils or wax esters (including sperm and like oils) or the corresponding fatty acids or other esters thereof are reduced to the corresponding alcohols by treatment with hydrogen and a hydrogenation catalyst such as nickel, cobalt, copper, iron, platinum, palladium or oxides thereof or zinc oxide with or without an acidic oxide such as silica, alumina, or an oxide of tungsten, chromium, molybdenum or vanadium, the reaction mixture being vigorously agitated and the hydrogen passed through rapidly to carry over the alcohols, Pressure may be employed for instance not more than 50 atmospheres. In the apparatus described hydrogen, admitted at 2 is circulated by a pump 1 through a preheater 3, reaction vessel 4 (containing an agitator) and pipe 5 to condenser 6 connected with a receiver 7 and thence to a second cooler 8 to remove water, and back to the pump. The condensates are removed continuously or intermittently by valved pipes 9, 10. In an example spermaceti is reduced ...

PRODUCING ALCOHOLS

Process for the production of higher aliphatic alcohols

Higher aliphatic alcohols containing more than five carbon atoms in the chain are prepared by treating the corresponding free carboxylic acids, completely free from ageing products, with hydrogen at elevated pressures and temperatures in the presence of hydrogenating catalysts. The ageing products are those which are formed on storing and impair the activity of the catalysts. The desired initial material may be obtained by splitting off the acid from the glyceride shortly before carrying out the reduction. In an example, cocoanut oil acids freshly prepared by hydrolysing cocoanut oil are mixed with a catalyst prepared by precipitating copper carbonate on kieselguhr from copper acetate and reducing or not, and heating the mixture under pressure. The alcohols obtained may be used directly for sulphonation.

CHEMICAL PROCESS

PROCESS FOR CONTINUOUSLY PREPARING ETHYLENE GLYCOL

Process

A process for carrying out a reaction in a reaction column 1 by providing a first reactant , such as carboxylic acid, 2 in the liquid phase to the reaction column and contacting the first reactant with an excess of a second reactant, such as methanol 3. At least a portion of the second reactant is provided to the reaction column in the vapour phase. Reaction takes place within the reaction column to form a relative low boiling and high boiling product. An overhead stream 6 comprising unreacted second reactant and the low boiling product, for example water, is recovered from the reaction column and the high boiling product, for example ester, is recovered as a bottoms stream of the reaction column. At least a portion of the heat required to vaporise the second reactant provided to the reaction column in the vapour phase is provided in a heat exchanger by heat exchange with a hot stream generated within the process other than a hot stream generated within the reaction column. The process ...

Process

RECOVERING AND CLEANING CATALYSTS

PROCESS FOR HYDROGENATION OF ESTERS INTO ALCOHOLS

Improved production of alcohols and/or esters

Saturated alcohols and esters are obtained by hydrogenating without a catalyst a saturated carboxylate of lead, cadmium or copper, or an unsaturated carboxylate of copper. When a hydroxy-carboxylate is used, the product is a dihydric alcohol or its ester. Carboxylates of several metals, at least one of which is lead cadmium or copper, may be used and result in different yields and different relative proportions of alcohols and esters. The other metals mentioned are chromium, cobalt, nickel, zinc, manganese and iron. Examples describe the reduction with hydrogen of the lead salts of coconut oil acids, copper oleate and lead acetate. Reference has been directed by the Comptroller to Specification 484,995.

Process for the production of fatty alcohols

A fatty alcohol is produced by the catalytic hydrogenation of a fatty acid, or a derivative thereof, at 200-350 DEG C. and 200-700 atm. in the presence of a known catalyst for the hydrogenation of carboxylic acid esters to alcohols, the material to be hydrogenated being continuously introduced into a reaction medium which consists almost entirely of the desired alcohol which has been saturated with hydrogen, so that the material is distributed uniformly almost instantaneously throughout a large excess of the alcohol. Fatty acid derivatives which may be used as starting materials are esters, anhydrides and lactones of fatty acids, oxyfatty acids with or without esterified hydroxy groups and free or esterified ketofatty acids. The preferred starting material is a symmetrical ester of the fatty acid, e.g. n-heptyl-n-heptoate or lauryl laurate. The preferred catalysts are copper/chromium oxide catalysts which may be modified by additional components, e.g. barium. Examples are given of the hydrogenation ...

PROCESS

Manufacture of wool wax alchohols

An emulsifier for oil-in-water emulsions consisting essentially of a substantially steroid-free wool-wax alcohol free of alpha , omega -diols prepared by subjecting (a) wool-wax esters of mono- or multi-valent alcohols of 1 to 6 carbon atoms or (b) wool-wax alcohols optionally containing monovalent aliphatic alcohols of 1 to 6 carbon atoms to catalytic hydrogenation at a pressure of 170 to 300 bars and a temperature of 200 DEG to 300 DEG C. in the presence of a high pressure hydrogenation catalyst to obtain substantially steroid-free wool wax alcohols and removing therefrom alpha , omega -diols useful as emulsifiers.

Separation process for the production of C5 or C6 alkanediol

Anti-inflammatory agents

The invention comprises compounds of general formula wherein R1 represents cycloalkyloxy (C3-C5), cycloalkylthio (C3-C5), alkylthio (C2-C3), when R2 is hydrogen; or R1 represents ethyl, n-propyl, isopropyl, n-butyl, n-pentyl, branched alkyl (C6-C7), cycloalkyl (C3-C5), alkoxy (C3-C4), alkenyloxy (C3-C4), alkylthio (C1-C5), alkenylthio (C3-C5), cycloalkyloxy (C3-C7), cycloalkylthio (C3-C7), phenoxy, phenylthio, alkenyl (C2-C4), when R2 is methyl; X represents CH2OH, COOR3 where R3 is hydrogen or alkyl (C1-C4) or, when R2 is methyl, dialkylamino substituted alkyl (C1-C4), CONH2, CH2NH2; and the non-toxic organic and inorganic salts of the acids, basic esters and amines; provided that X is not CH2OH when R1 is ethyl; and their preparation by methods described, these being analogous to known methods. Processes and intermediate and final compounds in examples are as follows:- 4-Substituted phenyl acetic acids are esterified to form ethyl esters which on treatment with ethyl ...

Processing and transforming biomass

Processing biomass and energy

Processing materials

Controlling process gases

Processing biomass

Processing materials

Upgrading process streams

Processing biomass materials

Reconfigurable processing enclosures

Array for processing materials

Upgrading process streams

Processing biomass

Processing biomass and energy

Filtration

Processing materials

Processing materials

Processing and transforming biomass

Controlling process gases

Processing biomass materials

Enclosures for treating materials

Procees.

Process for production of fatty alcohols.

Process of production of alcohols.

Processing materials

Processing biomass

Processing biomass materials

Processing biomass and energy

Reconfigurable processing enclosures

Processing materials

Upgrading process streams

Filtration

Enclosures for treating materials

Controlling process gases

Array for processing materials

Processing and transforming biomass

Enclosures for treating materials

Array for processing materials

Reconfigurable processing enclosures

Filtration

PROCEDURE FOR THE PRODUCTION OF HEXANDIOL - 1,6

TWO-STAGE PROCEDURE FOR the HYDROGENATION FROM MALEIC ACID TO 1,4-BUTANDIOL

IMPROVED CATALYST AND PROCEDURE FOR THE PRODUCTION OF ALCOHOLS BY HYDROGENATION AT THIS CATALYST

PROCEDURE FOR the PRODUCTION OF 1,4-BUTANDIOL AT RHENIUMHALTIGEN ACTIVATED CHARCOAL CARRIER CATALYSTS

VERFAHREN ZUR HERSTELLUNG NEUER (4-BIPHENYLYL) -ALKOHOLE

PROCEDURE FOR the PRODUCTION of NEW (4-BIPHENYLYL) - 1-BUTANOLE

PROCEDURES FOR THE PRODUCTION OF BENZYLE ALCOHOL AND SUBSTITUTED BENZYLE ALCOHOLS

PROCEDURE FOR the PRODUCTION of NEW (4-BIPHENYLYL) - ALCOHOLS

PROCEDURE FOR the PRODUCTION of NEW (4-BIPHENYLYL) -3-BUTEN-1-OLE

HYDROGENATION PROCEDURE

PROCEDURE FOR REGULATING THE QUANTITY OF THE USED CATALYST, WHICH IS LED BACK IN A HYDROGENATION MECHANISM FOR PRODUCING FETTALKOHOLEN FROM FATTY ACIDS AND/OR FATTY ACID DERIVATIVES

2.3-DIALKOXYPROPYLGLYCERYLAETHER, PROCEDURE FOR THEIR PRODUCTION AND THIS CONTAINING COSMETIC COMPOSITION.

SAEURERESISTENTER CATALYST FOR THE FATTY ACID DIRECT HYDROGENATION TO FETTALKOHOLEN.

PROCEDURE FOR the PRODUCTION OF 1,4-BUTANDIOL AND TETRAHYDROFURANE.

PROCEDURE FOR the PRODUCTION OF 1,1-DIHYDROPERFLUORALKANOLEN.

CYCLO-ALIPHATIC ALCOHOLS.

COSMETIC MEANS OF THE TYPE WATER IN OEL AND A EMULSIFYING COMPOSITION.

PROCEDURE FOR the PRODUCTION of NEW (4-BIPHENYLYL) - 1-BUTANOLE

HYDROGENATION CATALYST.

ALCOHOL PRODUCTION THROUGH HYDROGENIERUNG OF CARBONIC ACIDS.

Separation of Vapor Crude Alcohol Product

Recovery of alcohol, in particular ethanol, by separating a vapor crude alcohol product obtained from the hydrogenation of acetic acid using a low energy process. The vapor crude ethanol product is separated in a column to produce a distillate stream comprising ethanol and at least one non-condensable gas. The vapor crude ethanol product may pass through a membrane before the first distillation column to separate the at least one non-condensable gas from the ethanol. The ethanol product is subsequently recovered from the distillate stream.

Liquid Esterification For The Production Of Alcohols

Purifying and/or recovery of ethanol from a crude ethanol product obtained from the hydrogenation of acetic acid. Separation and purification processes of crude ethanol mixture are employed to allow recovery of ethanol and remove impurities. In addition, the process involves returning acetaldehyde separated from the crude ethanol product to the reactor.

Alcohol Production Process with Impurity Removal

A method of removing impurities, such as halogens, sulfurs, and corrosion metal impurities, in an ethanol production process. Ion exchange resins may be used to remove these impurities from acetic acid feed streams and recycle streams that comprise unreacted acetic acid.

Integrated process for producing alcohols from a mixed acid feed

Processes for producing alcohols such as ethanol and propanol from a mixed acid feedstock in an integrated process. In one embodiment, the process comprises the step of carbonylating methanol in the presence of a carbonylation catalyst to form a mixed acid feedstock comprising acetic acid and one or more higher acids, preferably comprising propionic acid. The mixed acid feed is hydrogenated in the presence of a hydrogenation catalyst to form a crude alcohol product comprising ethanol and one or more higher alcohols, preferably including propanol.

Integrated Process for the Production of Vinyl Acetate from Acetic Acid Via Ethylene

This invention provides an integrated two stage economical process for the production of vinyl acetate monomer (VAM) from acetic acid in the vapor phase. First, acetic acid is selectively hydrogenated over a hydrogenating catalyst composition to form ethylene either in a single reactor zone or in a dual rector zone wherein the intermediate hydrogenated products are either dehydrated and/or cracked to form ethylene. In a subsequent second stage so formed ethylene is reacted with molecular oxygen and acetic acid over a suitable catalyst to form VAM. In an embodiment of this invention reaction of acetic acid and hydrogen over a hydrogenation catalyst and subsequent reaction over a dehydration catalyst selectively produces ethylene, which is further mixed with acetic acid and molecular oxygen and reacted over a supported palladium/gold/potassium catalyst.

Plasticiser Alcohol And Production Improvement

Embodiments of the invention disclosed herein relate to a process for the production of a C 6 -C 15 alcohol mixture comprising the steps of: hydroformylating an olefin mixture comprising a branched C 5 -C 14 olefin to form a hydroformylation product comprising aldehydes and formate esters, whereby the hydroformylation product has a net cold sap number from 15 to 38 mg KOH/g, and converting the aldehydes and formate esters to alcohols in a hydrogenation step comprising at least one first hydrogenation reactor comprising a fixed bed of a heterogeneous sulphided bimetallic catalyst.

Processes for the production of hydrogenated products

A process for making a hydrogenated product includes providing a clarified DAS-containing fermentation broth, distilling the broth to form an overhead that includes water and ammonia, and a liquid bottoms that includes MAS, at least some DAS, and at least about 20 wt % water, cooling and/or evaporating the bottoms, and optionally adding an antisolvent to the bottoms, to attain a temperature and composition sufficient to cause the bottoms to separate into a DAS-containing liquid portion and a MAS-containing solid portion that is substantially free of DAS, separating the solid portion from the liquid portion, recovering the solid portion, hydrogenating the second solid portion in the presence of at least one hydrogenation catalyst to produce the hydrogenated product comprising at least one of THF, GBL or BDO, and recovering the hydrogenated product.

Vent scrubbers for use in production of ethanol

A process for producing ethanol comprising the steps of hydrogenating an acetic acid feed stream to form a crude ethanol product and separating at least a portion of the crude ethanol product to form an ethanol stream and at least one vent stream. The vent stream comprises non-condensable gases at least one volatile organic. The process further comprises the step of scrubbing the vent stream with at least two different solvents to recover the volatile organics. The vent stream may also comprise entrained ethanol, which may also be recovered.

Extractive Distillation of Crude Alcohol Product

Recovery of ethanol from a crude ethanol product obtained from the hydrogenation of acetic acid using an extractive distillation column. The column yields a first residue that comprises ethanol, ethyl acetate, acetic acid, and water. The first residue is separated in a second column to yield a second distillate comprising ethanol and ethyl acetate. The second distillate is then separated in a third column to yield a third distillate comprising ethyl acetate and a third residue comprising ethanol.

Recovering Ethanol with Sidestreams to Regulate C3+ Alcohols Concentrations

This invention relates to a process for producing ethanol and recovering methyl iodide, the process comprising the steps of carbonylating methanol in a carbonylation system in the presence of a carbonylation catalyst under conditions effective to form acetic acid; hydrogenating the acetic acid in a hydrogenation system in the presence of a hydrogenation catalyst to form a crude ethanol product comprising ethanol and water; and separating the crude ethanol product to form an ethanol stream and a water stream.

Process to Recover Alcohol with Secondary Reactors for Hydrolysis of Acetal

A process for recovering ethanol obtained from the hydrogenation of acetic acid. The crude ethanol product is separated in a column to produce a distillate stream comprising acetaldehyde and ethyl acetate and a residue stream comprising ethanol, acetic acid and water. Acetal byproduct can be reduced or removed through configurations of hydrolysis secondary reactors. The ethanol product is recovered from the residue stream.

Process to Recover Alcohol with Reduced Water From Overhead of Acid Column

A process for recovering ethanol obtained from the hydrogenation of acetic acid. The crude ethanol product is separated in a column to produce a distillate stream comprising acetaldehyde and ethyl acetate and a residue stream comprising ethanol, acetic acid, ethyl acetate and water. The ethanol product is recovered from the residue stream.

Production of alcohols

A process is described for producing an alcohol product, in which (a) a first feed composition comprising acetic acid is converted to a product comprising acetone; and (b) a second feed composition comprising at least part of the acetone produced in (a) is hydrogenated in the presence of a catalyst to produce a hydrogenation effluent comprising isopropanol.

Process for Separating Ethanol Having Low Acid

A process for operating a distillation column to separate an ethanol mixture comprising ethanol and acetic acid where the recovered ethanol comprises less than 700 wppm acetic acid. The operating conditions for the column may vary depending on the fed composition. In particular the process provides energy efficient recovery of ethanol with low concentration acetic acid.

Process for Vapor Phase Hydrogenation

A process for selective formation of ethanol from acetic acid includes contacting a feed stream containing acetic acid and hydrogen at an elevated temperature with catalyst comprising platinum and tin on a high surface area silica promoted with calcium metasilicate. Selectivities to ethanol of over 85% are achieved at 280° C. with catalyst life in the hundreds of hours. 1108-. (canceled)109. A process for the production of ethanol by reduction of acetic acid comprising passing a gaseous stream comprising hydrogen and acetic acid in the vapor phase in a molar ratio of hydrogen to acetic acid of at least about 4:1 at a temperature of between about 225° C. and 300° C. over a particulate hydrogenation catalyst comprising a silicaceous support having dispersed thereon a platinum group metal selected from the group consisting of platinum , palladium and mixtures thereof , with a promoter metal comprising cobalt , the silicaceous support having a surface area of at least 175 m/g and being chosen from the group consisting of silica , calcium metasilicate and calcium metasilicate promoted silica having calcium metasilicate disposed on the surface thereof , the surface of the silicaceous support being essentially free of Bronsted acid sites due to alumina unbalanced by calcium.110. The process of claim 109 , wherein the catalyst consists of silicaceous support having dispersed thereon a platinum group metal and cobalt.111. The process of claim 109 , wherein the silicaceous support is silica.112. The process of claim 109 , wherein the silicaceous support is calcium metasilicate.113. The process of claim 109 , wherein the silicaceous support has a surface area of at least 200 m/g.114. The process of claim 109 , wherein the platinum group metal is present from 0.5 to 5 wt. % claim 109 , based on the total weight of the catalyst.115. The process of claim 109 , wherein a weight ratio of cobalt to platinum group metal is from 20:1 to 3:1.116. A process for the production of ethanol ...

Synthesis of High Caloric Fuels and Chemicals

In one embodiment, the present application discloses methods to selectively synthesize higher alcohols and hydrocarbons useful as fuels and industrial chemicals from syngas and biomass. Ketene and ketonization chemistry along with hydrogenation reactions are used to synthesize fuels and chemicals. In another embodiment, ketene used to form fuels and chemicals may be manufactured from acetic acid which in turn can be synthesized from synthesis gas which is produced from coal, biomass, natural gas, etc.

Electrochemical Co-Production of Chemicals with Sulfur-Based Reactant Feeds to Anode

The present disclosure includes a system and method for producing a first product from a first region of an electrochemical cell having a cathode and a second product from a second region of the electrochemical cell having an anode. The method may include a step of contacting the first region with a catholyte comprising carbon dioxide. The method may include another step of contacting the second region with an anolyte comprising a sulfur-based reactant. Further, the method may include a step of applying an electrical potential between the anode and the cathode sufficient to produce a first product recoverable from the first region and a second product recoverable from the second region. An additional step of the method may include removing the second product and an unreacted sulfur-based reactant from the second region and recycling the unreacted sulfur-based reactant to the second region.

System and Method for Oxidizing Organic Compounds While Reducing Carbon Dioxide

Methods and systems for electrochemically generating an oxidation product and a reduction product may include one or more operations including, but not limited to: receiving a feed of at least one organic compound into an anolyte region of an electrochemical cell including an anode; at least partially oxidizing the at least one organic compound at the anode to generate at least carbon dioxide; receiving a feed including carbon dioxide into a catholyte region of the electrochemical cell including a cathode; and at least partially reducing carbon dioxide to generate a reduction product at the cathode.

Copper hydrogenation catalyst, especially for converting oxalate to ethylene glycol, method of preparing the catalyst and applications thereof

A copper catalyst for producing ethylene glycol by hydrogenation of an oxalate. The catalyst includes a carrier, an additive, and an active component. The carrier is ceramic or metallic honeycomb. The additive is Al, Si, Ba, Ca, Ti, Zr, Fe, Zn, Mn, V, La, Ce, an oxide thereof, or a mixture thereof. The active component is copper, and the active component and the additive are coated on the carrier to form a coating layer. The additive accounts for 5-90 wt. % of the carrier, the active component accounts for 1-40 wt. % of the carrier, and the copper accounts for 5-50 wt. % of the coating layer.

Hydrogenating Acetic Acid to Produce Ethyl Acetate and Reducing Ethyl Acetate to Ethanol

Disclosed herein are processes for alcohol production by reducing an ethyl acetate produced by hydrogenating acetic acid in the presence of a suitable catalyst. The ethyl acetate is reduced with hydrogen in the presence of a catalyst to obtain a crude reaction mixture comprising the alcohol, in particular ethanol, which may be separated from the crude reaction mixture. Thus, ethanol may be produced from acetic acid through an ethyl acetate intermediate without an esterification step. This may reduce the recycle of ethanol in the hydrogenolysis process and improve ethanol productivity. 1. A method of producing ethanol comprising:hydrogenating acetic acid in a first reactor in the presence of a first catalyst to form a hydrogenation product comprising ethyl acetate, water, and acetic acid;recovering an ester feed stream from the hydrogenation product; andreducing the ester feed stream in a second reactor in the presence of a second catalyst to form ethanol.2. The method of claim 1 , wherein the ester feed stream is recovered in the absence of an esterification process.3. The method of claim 1 , wherein none of the ethanol formed by reducing the ester feed stream is recycled to the first reactor.4. The method of claim 1 , wherein the hydrogenation product comprises from 20 to 95 wt. % ethyl acetate claim 1 , from 5 to 40 wt. % water and from 0.01 to 90 wt. % acetic acid.5. The method of claim 1 , wherein the hydrogenation product further comprises from 0.1 to 30 wt. % ethanol.6. The method of claim 1 , wherein the hydrogenation product is fed to a distillation column to yield a distillate comprising ethyl acetate claim 1 , ethanol claim 1 , and water claim 1 , wherein the ester feed stream comprises the distillate; and a residue comprising acetic acid claim 1 , and wherein the residue is returned to the first reactor.7. The method of claim 6 , wherein the distillate is further condensed and biphasically separated into an organic phase and an aqueous phase claim 6 , and ...

Electrochemical Co-Production of Chemicals Utilizing a Halide Salt

The present disclosure includes a system and method for co-producing a first product and a second product. The system may include a first electrochemical cell, at least one second reactor, and an acidification chamber. The method and system for co-producing a first product and a second product may include co-producing a carboxylic acid and at least one of an alkene, alkyne, aldehyde, ketone, or an alcohol while employing a recycled halide salt. 1. A method for co-producing a first product and a second product , the method comprising the steps of:contacting a first region of an electrochemical cell having a cathode with a catholyte comprising carbon dioxide;contacting a second region of the electrochemical cell having an anode with an anolyte comprising an MX where M is at least one cation and X is selected from a group consisting of F, Cl, Br, I and mixtures thereof;applying an electrical potential between the anode and the cathode sufficient to produce M-carboxylate recoverable from the first region of the electrochemical cell and a halogen recoverable from the second region of the electrochemical cell;reacting the halogen from the second region of the electrochemical cell with at least one of an alkane, an alkene, an aromatic, or other organic compound to produce a halogenated compound and HX, the HX being recycled back to an acidification chamber;reacting the M-carboxylate with the HX via the acidification chamber to produce a carboxylic acid and MX, the MX being recycled to an input of the second region of the electrochemical cell.2. The method according to claim 1 , further comprising:reacting the halogenated compound via a third reactor to produce the second product and HX, the HX being recycled to the acidification chamber.3. The method according to claim 1 , wherein the halogen includes at least one of F claim 1 , Cl claim 1 , Bror I.4. The method according to claim 1 , wherein the halogenated compound includes at least one of a brominated compound claim 1 , ...

Integrated process for producing polyvinyl alcohol or a copolymer thereof and ethanol

Ethanol is produced from acetic acid or acetic anhydride or a mixture of acetic acid and acetic anhydride by a hydrogenation reaction. The acetic acid or acetic anhydride or a mixture of acetic acid and acetic anhydride is produced from methyl acetate by a carbonylation reaction. The methyl acetate is produced as a byproduct during the conversion of a vinyl acetate polymer or copolymer to a polymer or copolymer of vinyl alcohol. By integrating processes as described herein, a valuable product, i.e. ethanol, is produced from a methyl acetate byproduct.

CO-GASIFICATION OF AQUATIC BIOMASS AND COAL

The invention also relates to co-gasification processes for forming syngas from aquatic biomass and a fossil fuel. In one aspect, the invention is to a process for producing syngas, comprising: introducing aquatic biomass, a fossil fuel, water and oxygen to a gasifier and forming syngas comprising hydrogen, carbon monoxide and carbon dioxide; and feeding aquatic biomass with carbon dioxide derived from the syngas. In other aspects, the invention relates to integrated processes for producing industrial chemicals, such as alcohols, carboxylic acids, esters, aldehydes, olefins and polymers from such syngas. 1. A process for producing syngas , comprising:(a) introducing aquatic biomass, a fossil fuel, water and oxygen to a gasifier and forming syngas comprising hydrogen, carbon monoxide and carbon dioxide; and(b) feeding aquatic biomass with carbon dioxide derived from the syngas.2. The process of claim 1 , wherein the aquatic biomass that is introduced into the gasifier comprises the aquatic biomass that is fed in step (b).3. The process of claim 1 , wherein the aquatic biomass is selected from the group consisting of microalgae claim 1 , macroalgae claim 1 , microplants claim 1 , duckweed claim 1 , water hyacinth claim 1 , cattails claim 1 , banana tree stem claim 1 , kelp claim 1 , and green algae.4. The process of claim 1 , wherein the gasifier is an entrained flow slagging gasifier.5. The process of claim 4 , wherein the gasifier is operated at a pressure greater than 30 bar.6. The process of claim 4 , wherein runoff from the gasifier provides nutrients for the aquatic biomass that is fed with carbon dioxide.7. The process of claim 4 , wherein the aquatic biomass and fossil fuel are introduced to the gasifier at a weight ratio from 1:99 to 40:60.8. The process of claim 4 , wherein the aquatic biomass is formed from microalgae having an average size less than 15 μm.9. The process of claim 4 , wherein the aquatic biomass is formed from macroalgae having an average ...

PROCESSES FOR THE PRODUCTION OF HYDROGENATED PRODUCTS AND DERIVATIVES THEREOF

Processes for making hydrogenated products including caprolactame (CL) caprolactone (CLO) or 1,6-hexanediol (HDO) and derivative thereof from monoammonium adipate (MAA) and/or adipic acid (AA) obtained from a clarified diammonium adipate-containing (DAA-containing) fermentation broth or monoammonium adipate-containing (MAA-containing) fermentation broth. 1. A process for making a hydrogenated product from a clarified DAA-containing fermentation broth comprising;(a) distilling the broth to form an overhead that comprises water and ammonia, and a liquid bottoms that comprises MAA, at least some DAA, and at least about 20 wt % water;(b) cooling and/or evaporating the bottoms, and optionally adding an antisolvent to the bottoms, to attain a temperature and composition sufficient to cause the bottoms to separate into a DAA-containing liquid portion and a MAA-containing solid portion that is substantially free of DAA;(c) separating the solid portion from the liquid portion;(d) recovering the solid portion;(e) hydrogenating the solid portion in the presence of at least one hydrogenation catalyst to produce the hydrogenated product comprising at least one of CL, CLO or HDO; and(f) recovering the hydrogenated product.2. A process for making a hydrogenated product from a DAA-containing fermentation broth comprising:(a) distilling the broth to form a first overhead that includes water and ammonia, and a first liquid bottoms that includes MAA, at least some DAA, and at least about 20 wt % water;(b) cooling and/or evaporating the bottoms, and optionally adding an antisolvent to the bottoms, to attain a temperature and composition sufficient to cause the bottoms to separate into a DAA-containing liquid portion and a MAA-containing solid portion that is substantially free of DAA;(c) separating the solid portion from the liquid portion;(d) recovering the solid portion;(e) dissolving the solid portion in water to produce an aqueous MAA solution;(f) distilling the aqueous MAA ...

Processes for the production of hydrogenated products and derivatives thereof

A process for making a hydrogenated product comprising caprolactone (CLO) and 1,6-hexanediol (HDO) and derivatives thereof from adipic acid (AA) obtained from fermentation broths containing diammonium adipate (DAA) or monoammonium adipate (MAA).

Esterifying an ethanol and acetic acid mixture to produce an ester feed for hydrogenolysis

Disclosed herein are processes for alcohol production by hydrogenating acetic acid to obtain a mixture of ethanol and acetic acid, esterifying the mixture to produce an esterification product and reducing the esterification product. The mixture may provide a sufficient amount of ethanol and acetic acid for esterification and reduces the need for additional acetic acid and/or ethanol. This may reduce the recycle of ethanol in the hydrogenolysis process and improve ethanol productivity.

Method for producing alcohol and/or amine from amide compound

Disclosed herein is a method for producing an alcohol and an amine from an amide under an atmosphere of hydrogen with the use of, as a catalyst, a ruthenium complex that is easily prepared, easy to handle, and relatively cheaply obtained. Specifically, the method is a method for producing an alcohol and/or an amine from an amide compound under an atmosphere of hydrogen with the use of as a catalyst, a ruthenium carbonyl complex represented by the following general formula (1): RuXY(CO)(L) (1) wherein X and Y may be the same or different from each other and each represents an anionic ligand and L represents a tridentate aminodiphosphine ligand containing two phosphino groups and a —NH— group.

Process for Monitoring Separation of Ethanol Mixture

A process is disclosed for monitoring separation streams of an ethanol purification process, including measuring the concentrations of impurities, monitoring one or more binary streams, or monitoring conductivity in an ethanol containing stream to determine acetic acid concentrations. The ethanol is produced by hydrogenating acetic acid. One or more on-line analyzers may be used to monitor the separation streams. 1. A process for producing ethanol , comprising:hydrogenating an acetic acid feed stream in the presence of a catalyst to form a crude ethanol product;separating the crude ethanol product in one or more distillation columns, wherein acetic acid is present in a residue and ethanol is present in a distillate, and wherein at least one of the distillate or residue comprises an organic impurity;measuring temperature, pressure, density, concentration, or conductivity of at least one of the distillate or the residue from the one or more distillation columns;setting a baseline value for the at least one of the distillate or the residue;adjusting at least one column parameter based on the measured data and the baseline value; andrecovering the ethanol product.2. The process of claim 1 , wherein the measuring is conducted using one or more on-line analyzers.3. The process of claim 2 , wherein the on-line analyzer is selected from the group consisting of gas chromatograph claim 2 , Raman spectrometer claim 2 , high-performance liquid chromatograph claim 2 , mass spectrometer claim 2 , infrared spectrometer claim 2 , and near-infrared spectrometer.4. The process of claim 1 , wherein the at least one column parameter is selected from the group consisting of reflux ratio claim 1 , residue to feed ratio claim 1 , distillate to feed ratio claim 1 , column temperature claim 1 , column pressure claim 1 , reboiler energy input claim 1 , and combinations thereof.5. The process of claim 1 , wherein the organic impurity is selected from the group consisting of ethyl acetate ...

Hydrogenation Catalysts with Cobalt-Modified Supports

The present invention relates to catalysts, to processes for making catalysts and to chemical processes employing such catalysts. The catalysts are preferably used for converting acetic acid to ethanol. The catalyst comprises a precious metal and one or more active metals on a modified support that comprises cobalt.

HYDROGENATION CATALYSTS WITH BULK MULTIPLE OXIDATED SUPPORTS

The present invention relates to catalysts, to processes for making catalysts and to chemical processes employing such catalysts. The catalysts are preferably used for converting acetic acid and ethyl acetate to ethanol. The catalyst comprises an extruded modified support, and a precious metal. The processes for making the catalysts comprises modifying the catalyst, extruding the catalyst, and impregnating the precious metal onto the catalyst. 1. A process for forming a catalyst for hydrogenating acetic acid and/or an ester thereof to form ethanol , the process comprising the steps of:(a) mixing a support with at least one support modifier precursor having a metal selected from the group consisting of tungsten, molybdenum, vanadium, niobium, cobalt, tin, tantalum, and mixtures thereof to form a modified support;(b) extruding the modified support to form a pellet; and(c) impregnating the pellet with a precious metal.2. The process of claim 1 , wherein the support is selected from the group consisting of silica claim 1 , alumina claim 1 , titania claim 1 , silica/alumina claim 1 , pyrogenic silica claim 1 , high purity silica claim 1 , zirconia claim 1 , carbon claim 1 , zeolites and mixtures thereof.3. The process of claim 1 , wherein the metal is selected from the group consisting of tungsten claim 1 , cobalt claim 1 , tin claim 1 , and mixtures or oxides thereof.4. The process of claim 1 , wherein the metal comprises tungsten and cobalt.5. The process of claim 1 , wherein the precious metal is selected from the group consisting of rhodium claim 1 , rhenium claim 1 , ruthenium claim 1 , platinum claim 1 , palladium claim 1 , osmium claim 1 , iridium claim 1 , gold and mixtures thereof.6. The process of claim 1 , further comprising impregnating the pellet with at least one active metal that is selected from the group consisting of copper claim 1 , iron claim 1 , vanadium claim 1 , tin claim 1 , cobalt claim 1 , nickel claim 1 , titanium claim 1 , zinc claim 1 , ...

Process for Acetal Removal In the Purification of a Crude Ethanol Product

Recovery of ethanol from a crude ethanol product obtained from the hydrogenation of acetic acid. Separation and purification processes of the crude ethanol products are employed to allow recovery of ethanol and hydrolyze acetal impurities by the addition of an acid stream. 1. A process for purifying a crude ethanol product , the process comprising the steps of:hydrogenating acetic acid in the presence of a catalyst in a reactor to form a crude ethanol product comprising ethanol, water, ethyl acetate and acetal;separating at least a portion of the crude ethanol product in a first column into a first distillate comprising ethanol, water, and ethyl acetate, and a first residue comprising acetic acid; andfeeding an acid stream to the first column to hydrolyze the acetal.2. The process of claim 1 , wherein the crude ethanol product comprises more than 0.005 wt. % diethyl acetal claim 1 , based on the total weight of the crude ethanol product.3. The process of claim 1 , wherein the first distillate comprises less than 0.01 wt. % diethyl acetal.4. The process of claim 1 , wherein the first residue comprises less than 0.01 wt. % diethyl acetal.5. The process of claim 1 , further comprising the steps of:separating at least a portion of the first distillate in a second column into a second distillate comprising ethyl acetate and a second residue comprising ethanol and water; andseparating at least a portion of the second residue in a third column into a third distillate comprising ethanol and a third residue comprising water.6. The process of claim 5 , further comprising the step of adding acetic acid to a part of the third column that contains acetal.7. The process of claim 5 , wherein at least a portion of the first distillate is hydrolyzed in the second column.8. The process of claim 5 , wherein the third distillate contains no detectable amount of acetal.9. The process of claim 5 , further comprising separating at least a portion of the second distillate in a fourth ...

HYDROGENATION CATALYSTS WITH ACIDIC SITES

The present invention relates to catalysts and to chemical processes employing such catalysts. The catalysts are preferably used for converting acetic acid to ethanol. The catalyst comprises acidic sites and two or more metals. The catalyst has acidic sites on the surface and the balance favors Lewis acid sites. 1. A hydrogenation catalyst comprising a precious metal and at least one active metal on a modified silica support , wherein the catalyst has at least 70% Lewis acid sites based on the total number of acid sites as measured by Fourier transform infrared spectroscopy of chemisorbed pyridine , and wherein the modified silica support comprises: (i) a support material; and (ii) a support modifier comprising a metal selected from the group consisting of tungsten , molybdenum , vanadium , niobium , and tantalum.2. The catalyst of claim 1 , wherein the catalyst has at least 80% Lewis acid sites claim 1 , based on the total number of acid sites claim 1 , as measured by Fourier transform infrared spectroscopy of chemisorbed pyridine.3. The catalyst of claim 1 , wherein the modified silica support comprises cobalt tungstate.4. The catalyst of claim 1 , wherein the precious metal is selected from the group consisting of rhodium claim 1 , rhenium claim 1 , ruthenium claim 1 , platinum claim 1 , palladium claim 1 , osmium claim 1 , iridium and gold.5. The catalyst of claim 1 , wherein the at least one active metal is selected from the group consisting of copper claim 1 , iron claim 1 , vanadium claim 1 , nickel claim 1 , titanium claim 1 , zinc claim 1 , chromium claim 1 , molybdenum claim 1 , tungsten claim 1 , tin claim 1 , lanthanum claim 1 , cerium claim 1 , cobalt claim 1 , manganese and combinations thereof.6. The catalyst of claim 1 , wherein the catalyst is prepared by:(a) impregnating a support material with a first solution to form a first impregnated support, wherein the first solution comprises a precursor to the support modifier metal selected from the group ...

Process for Producing Ethanol Using a Molar Excess of Hydrogen

The present invention relates to a process for the production of ethanol using a molar excess of hydrogen. A mixed feed of acetic acid and ethyl acetate is fed to a reactor to be converted to ethanol. Hydrogen flow is increased to avoid a negative conversion of ethyl acetate.

METHOD FOR PRODUCING HIGHER ALCOHOL

Provided is a method of producing a higher alcohol, comprising a step of hydrogenating a lipid obtained by culturing in the presence of a hydrogenation catalyst. 115-. (canceled)16Euglena. A method for producing a higher alcohol , comprising a step of performing pretreatment of a lipid obtained by culturing and a step of hydrogenating the pretreated lipid in the presence of a hydrogenation catalyst.17. The method for producing a higher alcohol according to claim 16 , wherein the pretreatment of the lipid comprises a step of washing the lipid with water.18. The method for producing a higher alcohol according to claim 17 , wherein the lipid is washed with water in an amount of 0.01 to 50 times by mass with respect to the lipid.19. The method for producing a higher alcohol according to claim 17 , wherein the lipid is washed with water at 5 to 100° C.20. The method for producing a higher alcohol according to claim 17 , wherein an acidic aqueous solution is used as the water.21. The method for producing a higher alcohol according to claim 20 , wherein the acidic aqueous solution has a pH of 1 to 6.22. The method for producing a higher alcohol according to claim 20 , wherein the acidic aqueous solution is an aqueous solution of citric acid.23. The method for producing a higher alcohol according to claim 16 , wherein the pretreatment of the lipid comprises adsorption treatment with an adsorbent.24. The method for producing a higher alcohol according to claim 23 , wherein a mixture of the lipid and the adsorbent in the adsorption treatment has a temperature of 5° C. to 200° C.25. The method for producing a higher alcohol according to claim 23 , wherein the adsorbent is white clay.26. The method for producing a higher alcohol according to claim 23 , wherein the adsorbent is activated carbon.27. The method for producing a higher alcohol according to claim 23 , wherein the adsorbent is a combination of white clay and activated carbon.28. The method for producing a higher ...

Electrochemical Co-Production of a Glycol and an Alkene Employing Recycled Halide

The present disclosure is a method and system for electrochemically co-producing a first product and a second product. The system may include a first electrochemical cell, a first reactor, a second electrochemical cell, at least one second reactor, and at least one third reactor. The method and system for for co-producing a first product and a second product may include co-producing a glycol and an alkene employing a recycled halide.

Processes for Making Ethanol From Acetic Acid

A process for selective formation of ethanol from acetic acid by hydrogenating acetic acid in the presence of first metal, a silicaceous support, and at least one support modifier. Preferably, the first metal is selected from the group consisting of copper, iron, cobalt, nickel, ruthenium, rhodium, palladium, osmium, iridium, platinum, titanium, zinc, chromium, rhenium, molybdenum, and tungsten. In addition the catalyst may comprise a second metal preferably selected from the group consisting of copper, molybdenum, tin, chromium, iron, cobalt, vanadium, tungsten, palladium, platinum, lanthanum, cerium, manganese, ruthenium, rhenium, gold, and nickel. 145-. (canceled)46. A process for producing ethanol , comprising hydrogenating acetic acid in the presence of a catalyst comprising a first metal , a second metal , a silicaceous support , and at least one support modifier; wherein the first metal is selected from the group consisting of copper , iron , cobalt , nickel , ruthenium , rhodium , palladium , osmium , iridium , platinum , titanium , zinc , chromium , rhenium , molybdenum , and tungsten and wherein the second metal is selected from the group consisting of copper , molybdenum , tin , chromium , iron , cobalt , vanadium , tungsten , palladium , platinum , lanthanum , cerium , manganese , ruthenium , rhenium , gold , and nickel , provided that the second metal is different than the first metal.47. The process of claim 46 , wherein the first metal is present in an amount of from 0.1 to 25 wt. % claim 46 , based on the total weight of the catalyst.48. The process of claim 46 , wherein the second metal is present in an amount of from 0.1 to 10 wt. % claim 46 , based on the total weight of the catalyst.49. The process of claim 46 , wherein the at least one support modifier is selected from the group consisting of (i) alkaline earth metal oxides claim 46 , (ii) alkali metal oxides claim 46 , (iii) alkaline earth metal metasilicates claim 46 , (iv) alkali metal ...

Hydrogenation of Mixed Oxygenate Stream to Produce Alcohol

The present invention relates to processes for the recovery of ethanol from a crude ethanol product obtained from the hydrogenation of a mixed oxygenate stream comprising ethyl acetate and acetaldehyde. The crude ethanol product is separated in at least one distillation column to product ethanol. The mixed oxygenate stream may be obtained from syngas.

Separation Process Having An Alcohol Sidestream

Recovery of ethanol from a crude ethanol product obtained from the hydrogenation of acetic acid. The crude ethanol product is fed to a distillation column to yield an ethanol sidestream. 118-. (canceled)19. A process for producing ethanol , comprising the steps of:hydrogenating acetic acid from an acetic acid feed stream in a reactor to form a crude ethanol product comprising from 0 to 50 wt. % acetic acid;separating at least a portion of the crude ethanol product in a distillation column into a distillate comprising acetaldehyde and ethyl acetate, a sidestream comprising ethanol, and a residue comprising less than 0.01 wt. % ethyl acetate; andrecovering ethanol from the sidestream.20. The process of claim 19 , wherein the crude ethanol product comprises less than 5 wt. % acetic acid.21. The process of claim 19 , wherein the residue comprises less than 2 wt. % ethanol.22. The process of claim 19 , wherein the distillate comprises from 45 wt. % to 90 wt. % ethanol.23. The process of claim 19 , wherein a mass flow ratio for the distillate to the sidestream to the residue is about 1:25:7.24. The process of claim 19 , further comprising neutralizing the residue.25. The process of claim 19 , wherein at least 90% of the ethanol in the crude ethanol product is removed in the sidestream.26. The process of claim 19 , wherein the sidestream comprises 50 to 90 wt. % ethanol claim 19 , and 10 to 45 wt. % water.27. The process of claim 19 , wherein the sidestream further comprises water and the process further comprises reducing the water content of the sidestream to yield an ethanol product stream with reduced water content.28. The process of claim 27 , wherein the ethanol product stream comprises less than 3 wt. % water.29. The process of claim 27 , wherein the reducing step uses an adsorption unit.30. The process of claim 27 , wherein the reducing step comprises separating at least a portion of the sidestream with a membrane into a permeate stream comprising water and a ...

METHODS FOR RECOVERY AND RECYCLE OF RUTHENIUM HOMOGENOUS CATALYSTS

Disclosed is a process for the extractive recovery of a homogeneous ruthenium catalyst from the reaction product of the hydrogenation of glycolic acid, glycolate esters, and/or glycolic acid oligomers with an extractant comprising a hydrophobic solvent and an optional hydrophilic solvent. The ruthenium catalyst, which can include 1,1,1-tris(diaryl- or dialkylphosphinomethyl)alkane ligands, can be recovered from the hydrophobic extract phase by back extraction with a hydrophilic solvent and recycled to a process for the preparation of ethylene glycol by the hydrogenation of glycolic acid and glycolic acid derivatives. 1. A process for recovering a homogeneous catalyst , comprising(A) contacting an aqueous mixture comprising glycolic acid, glycolate esters, methyl glycolate, oligomers of glycolic acid, or mixtures thereof, with hydrogen in the presence of a catalyst composition comprising ruthenium and tris-1,1,1-(diphenylphosphinomethyl)ethane to form a glycolic acid hydrogenation product comprising about 50 to about 90 weight percent, based on the total weight of said glycolic acid hydrogenation product, ethylene glycol, about 0.5 to about 25 weight percent water, and about 0.5 to about 30 weight percent of one or more reaction by-products selected from glycolic acid, oligomers of glycolic acid, and glycolate esters of ethylene glycol, and said catalyst composition;(B) extracting said glycolic acid hydrogenation product with a first extractant, comprising about 60 to 100 weight percent, based on the total weight of said first extractant, 2-ethylhexanol and about 0 to about 40 weight percent of a hydrocarbon having 5 to 20 carbon atoms to form a first raffinate phase comprising a major amount of said ethylene glycol contained in said glycolic acid hydrogenation product and a first extract phase comprising a major amount of said catalyst composition contained in said glycolic acid hydrogenation product;(C) separating said first raffinate and extract phases;(D) ...

CATALYST FOR HYDROGENATION OF OXALIC ESTER TO ETHANOL, METHOD OF PREPARING THE CATALYST, AND METHOD OF USING THE SAME

A catalyst including: a support, the support including a mixture of SiOand ZrO; an active ingredient including copper; a first additive including a metal, an oxide thereof, or a combination thereof; and a second additive including Li, Na, K, or a combination thereof. The metal is Mg, Ca, Ba, Mn, Fe, Co, Zn, Mo, La, or Ce. Based on the total weight of the catalyst, the weight percentages of the different components are as follows: SiO=50-90 wt. %; ZrO=0.1-10 wt. %; copper=10-50 wt. %; the first additive=0.1-10 wt. %; and the second additive=0.1-5 wt. %. 2. The catalyst of claim 1 , wherein the weight of SiOis 50-80% of that of the catalyst.3. The catalyst of claim 1 , wherein the weight of ZrOis 0.4-5% of that of the catalyst.4. The catalyst of claim 1 , wherein the weight of active ingredient copper is 20-40% of that of the catalyst.5. The catalyst of claim 1 , wherein the weight of first additive is 0.5-5% of that of the catalyst.6. The catalyst of claim 1 , wherein the weight of second additive is 0.3-1% of that of the catalyst.7. A method for preparing the catalyst of claim 1 , the method comprising:1) providing an aqueous solution comprising a soluble copper precursor;2) providing a first soluble precursor comprising the first additive, and uniformly mixing the first soluble precursor with the soluble copper precursor;3) adding a precipitator of aqueous ammonia or urea to the aqueous solution and stirring;4) dissolving a precursor of Zr with diluted nitric acid and adding aqueous ammonia to the precursor until a pH value therein is 1.5-2.0 to form a semitransparent Zr sol;5) adding the Zr sol to gel sol and stirring for 2-10 h under heating;6) adding a mixed sol obtained in step 5) to the aqueous solution obtained in step 3), stirring for 2-12 h, heating the mixture to 50-100° C. to allow for precipitation of copper and the first additive, terminating heating when the pH value is lower than 7, filtering a resulting precipitant, washing, and drying; and7) ...

Novel ruthenium complexes and their uses in processes for formation and/or hydrogenation of esters, amides and derivatives thereof

The present invention relates to novel Ruthenium catalysts and related borohydride complexes, and the use of such catalysts, inter alia, for (1) hydrogenation of amides (including polyamides) to alcohols and amines; (2) preparing amides from alcohols with amines (including the preparation of polyamides (e.g., polypeptides) by reacting dialcohols and diamines and/or by polymerization of amino alcohols); (3) hydrogenation of esters to alcohols (including hydrogenation of cyclic esters (lactones) or cyclic di-esters (di-lactones) or polyesters); (4) hydrogenation of organic carbonates (including polycarbonates) to alcohols and hydrogenation of carbamates (including polycarbamates) or urea derivatives to alcohols and amines; (5) dehydrogenative coupling of alcohols to esters; (6) hydrogenation of secondary alcohols to ketones; (7) amidation of esters (i.e., synthesis of amides from esters and amines); (8) acylation of alcohols using esters; (9) coupling of alcohols with water to form carboxylic acids; and (10) dehydrogenation of beta-amino alcohols to form pyrazines. The present invention further relates to the novel uses of certain pyridine Ruthenium catalysts.

Method For Producing Beta-Fluoroalcohol

A production method of a β-fluoroalcohol includes performing a reaction of an α-fluoroester with hydrogen gas (H 2 ) in the presence of a specific ruthenium complex (i.e. a ruthenium complex of the general formula [2], preferably a ruthenium complex of the general formula [4]). This production method can employ a suitable hydrogen pressure of 1 MPa or less by the use of such a specific ruthenium complex and does not require a high-pressure gas production facility when put in industrial practice. In addition, this production method can remarkably reduce the amount of catalyst used therein (to e.g. a substrate/catalyst ratio of 20,000) in comparison to the substrate/catalyst ratio conventional reduction of α-fluoroalcohol. It is possible by these reduction in hydrogen pressure and catalyst amount to largely reduce the production cost of the β-fluoroalcohol.

METHOD FOR PRODUCING ETHYLENE GLYCOL FROM OXALATE THROUGH THE FLUIDIZED BED CATALYTIC REACTION

A process for producing ethylene glycol includes contacting an oxalate with a fluidized bed catalyst under the following conditions: a reaction temperature of from about 170 to about 270° C., a weight space velocity of oxalate of from about 0.2 to about 7 hours, a hydrogen/ester molar ratio of about 20˜200:1, a reaction pressure of from about 1.5 to about 10 MPa, and a reaction temperature difference T of from about 1 to about 15° C. The fluidized bed catalyst includes: a) from about 5 to about 80 parts by weight of copper and the oxide thereof, b) from about 10 to about 90 parts by weight of at least one carrier selected from silica, molecular sieve or alumina, c) from about 0.01 to about 30 parts by weight of bismuth and tungsten metallic elements or the oxides thereof, or cerium and niobium metallic elements or the oxides thereof. 1. A process for producing ethylene glycol , the process comprising contacting an oxalate as a raw material with a fluidized bed catalyst under the following conditions: a reaction temperature of from about 170° C. to about 270° C. , a weight space velocity of the oxalate of from about 0.2 hto about 7 h , a hydrogen/ester molar ratio of from about 20:1 to about 200:1 , a reaction pressure of from about 1.5 MPa to about 10 MPa , and a reaction temperature difference T of from about 1° C. to about 15° C. , to produce an effluent containing ethylene glycol;wherein said fluidized bed catalyst is a catalyst comprising copper and the an oxide thereof.2. The process for producing ethylene glycol according to claim 1 , wherein the fluidized bed reaction temperature ranges from about 180° C. to about 260° C. claim 1 , the weight space velocity of the oxalates ranges from about 0.3 hto about 3 h claim 1 , the hydrogen/ester molar ratio ranges from about 50:1 to about 150:1 and the reaction pressure ranges from about 2.0 MPa to about 6.0 MPa.3. The process for producing ethylene glycol according to claim 1 , wherein said fluidized bed catalyst ...

Method for improving the quality of ethylene glycol products

A method for improving the quality of ethylene glycol products, which mainly solves the technical problem of low UV-light transmittance of the ethylene glycol products present in the prior art. The method successfully solves the problem by use of the technical solution wherein the ethylene glycol raw material and hydrogen are passed through a rotating packed bed reactor loaded with solid oxide catalyst at a temperature of about 20 to about 280 ° C., a pressure of about 0.1 to about 4.0 MPa, a space velocity of about 0.2 to about 100.0 hr −1 and a molar ratio of hydrogen to ethylene glycol of from about 0.01 to 40:1, and ethylene glycol is obtained after the reaction. The solid oxide catalyst is at least one of copper-based, nickel-based and palladium-based catalysts, and the rotation rate of the rotating packed bed reactor is about 300 to about 5000 rpm.

NOVEL ALICYCLIC ALCOHOL

Provided is an alicyclic alcohol compound which can be used as a raw material for a compound perfume, and which has excellent floral-green-like aromas which are crisp and fresh; also provided are a manufacturing method for the same, and a perfume composition which contains the alicyclic alcohol compound. An alicyclic alcohol compound having a specified structure represented by chemical formula (1) has excellent floral-green-like aromas which are crisp and fresh; and a method for manufacturing the alicyclic alcohol compound represented by chemical formula (1) by reacting, in the presence of hydrogen fluoride, 1-isopropyl-4-methylcyclohexene and carbon monoxide, reacting the resulting 4-isopropyl-1-methylcyclohexane carboxylic acid fluoride with alcohol, and, after having acquired a cyclohexane carbonyl compound, reducing the cyclohexane carbonyl compound. The present invention relates to an alicyclic alcohol compound which can be used as a raw material for compounded perfumes, a method for manufacturing the same, and a perfume composition containing said alicyclic alcohol compound.It is known that some of alicyclic alcohol compounds are useful for a raw material for compounded perfumes. For example, Non-patent Document 1 discloses that Mayol having green and muguet-like fragrance, Mugetanol having muguet-like light floral fragrance, Patchone having patchouli-like woody fragrance and the like are useful as a raw material for compounded perfumes.The object of the present invention is to provide a novel alicyclic alcohol compound having floral-green-like fragrance useful for a raw material for compounded perfumes, a method for manufacturing the same and a perfume composition containing said alicyclic alcohol compound.As a result of synthesizing various compounds and studying fragrances thereof, the present inventors have found that the alicyclic alcohol compound represented by the following chemical formula (1) which is a novel compound has excellent floral-green-like ...

METHOD FOR THE PRODUCTION OF ETHYLENE GLYCOL

The present invention relates to a method for the production of ethylene glycol using a feedstock comprising an oxalate and a catalyst containing copper and/or a copper oxide, comprising contacting the feedstock with the catalyst in a reactor under the conditions of a temperature in the range from about 170 to about 270° C., a weight hourly space velocity of the oxalate in the range from about 0.2 to about 5 h, a molar ratio of hydrogen to the oxalate in the range from about 40:1 to about 200:1 and a reaction pressure in the range from about 1.5 to about 10 MPa, to produce an effluent containing ethylene glycol, in which the reactor is a tube-array reactor using partitioned heat exchange and adopting outer and inner tubes configured in a double-tube structure to facilitate the heat exchange of the catalyst. 1. A method for production of ethylene glycol using a feedstock comprising an oxalate and a catalyst containing copper and/or a copper oxide , comprising:{'sup': '−1', 'contacting the feedstock with the catalyst in a reactor under conditions of a temperature in a range from about 170 to about 270° C., a weight hourly space velocity of the oxalate in a range from about 0.2 to about 7 h, a molar ratio of hydrogen to the oxalate in a range from about 20:1 to about 200:1 and a reaction pressure in a range from about 1.5 to about 10 MPa, to produce an effluent containing ethylene glycol, wherein the reactor is a tube-array reactor using partitioned heat exchange and adopting outer and inner tubes configured in a double-tube structure to facilitate heat exchange of the catalyst.'}2. The method for production of ethylene glycol according to claim 1 , wherein the reaction temperature in the reactor is about 180 to about 260° C.; the weight hourly space velocity of the oxalate is about 0.3 to about 3 h; the molar ratio of hydrogen to the oxalate is about 50:1 to about 150:1; and the reaction pressure is about 2.0 to about 6.0 MPa.3. The method for production of ethylene ...

Process for Making Ethanol from Acetic Acid Using Acidic Catalysts

A process for selective formation of ethanol from acetic acid by hydrogenating acetic acid in the presence of a catalyst comprises a first metal on an acidic support. The acidic support may comprise an acidic support material or may comprise an support having an acidic support modifier. The catalyst may be used alone to produced ethanol via hydrogenation or in combination with another catalyst. In addition, the crude ethanol product is separated to obtain ethanol. 1. A process for producing ethanol , comprising hydrogenating acetic acid in the presence of a catalyst to form ethanol , wherein the hydrogenation has a selectivity to ethanol of at least 65% wherein the catalyst comprises a first metal on an acidic support selected from the group consisting ofan acidic support material selected from the group consisting of iron oxide, alumina, silica/aluminas, titania, zirconia, and mixtures thereof, anda support material modified with an acidic modifier.2. The process of claim 1 , wherein the support material is selected from the group consisting of silica claim 1 , silica/alumina claim 1 , calcium metasilicate claim 1 , pyrogenic silica claim 1 , high purity silica claim 1 , carbon claim 1 , iron oxide claim 1 , alumina claim 1 , silica/aluminas claim 1 , titania claim 1 , zirconia claim 1 , and mixtures thereof.3. The process of claim 1 , wherein the acidic modifier is selected from the group consisting of oxides of Group IVB metals claim 1 , oxides of Group VB metals claim 1 , oxides of Group VIB metals claim 1 , oxides of Group VIIB metals claim 1 , oxides of Group VIIIB metals claim 1 , aluminum oxides claim 1 , and mixtures thereof.4. The process of claim 1 , wherein the acidic modifier is selected from the group consisting of TiO claim 1 , ZrO claim 1 , NbO claim 1 , TaO claim 1 , AlO claim 1 , BO claim 1 , PO claim 1 , and SbO.5. The process of claim 1 , wherein the acidic modifier is selected from the group consisting of WO claim 1 , MoO claim 1 , FeO claim 1 , ...

Production of Adipic Acid and Derivatives from Carbohydrate-Containing Materials

The present invention generally relates to processes for the chemocatalytic conversion of a carbohydrate source to an adipic acid product. The present invention includes processes for the conversion of a carbohydrate source to an adipic acid product via a furanic substrate, such as 2,5-furandicarboxylic acid or derivatives thereof. The present invention also includes processes for producing an adipic acid product comprising the catalytic hydrogenation of a furanic substrate to produce a tetrahydrofuranic substrate and the catalytic hydrodeoxygenation of at least a portion of the tetrahydrofuranic substrate to an adipic acid product. The present invention also includes products produced from adipic acid product and processes for the production thereof from such adipic acid product.

Process for Heat Integration for Ethanol Production and Purification Process

Ethanol production from the hydrogenation of acetic acid requires energy to drive the hydrogenation reaction and the purification of the crude ethanol product. Heat integration process to recover heat from one part of the production process to be used within the process improves efficiencies and reduces costs. 130-. (canceled)31. A process for producing ethanol , the process comprising the steps of:introducing an acetic acid vapor feed stream comprising acetic acid into a reactor;hydrogenating the acetic acid in the reactor in the presence of a catalyst to form a reactor product stream;flashing the reactor product stream to form a vapor stream and a liquid stream comprising ethanol, ethyl acetate, water, and acetic acid;transferring at least part of the heat from the reactor product stream in a first heat exchange stage to the acetic acid vapor feed stream;transferring at least part of the heat from the reactor product stream in a second heat exchange stage to the vapor feed stream; andrecovering ethanol from the liquid stream.32. The process of claim 31 , further comprising separating at least a part of the liquid stream in one or more distillation columns to recover ethanol.33. The process of claim 32 , further comprising transferring at least part of the heat from the reactor product stream in a third heat exchange stage to the liquid stream prior to being introduced to the one or more distillation columns.34. The process of claim 32 , further comprising transferring at least part of the heat from the reactor product stream in a fourth heat exchange stage to a reboiler stream of at least one of the one or more distillation columns.35. The process of claim 31 , further comprising introducing an acetic acid feed stream claim 31 , a hydrogen feed stream claim 31 , and the vapor stream to a vaporizer to produce the acetic acid vapor feed stream.36. The process of claim 35 , further comprising transferring at least part of the heat from the reactor product stream in a ...

CATALYST FOR HYDROGENATION OF CARBONYL COMPOUND AND ALCOHOL PRODUCTION METHOD

Provided is a catalyst including a metal component including a first component that is rhenium and one or more second components selected from the group consisting of silicon, gallium, germanium, and indium and a carrier on which the metal component is supported, the carrier including an oxide of a metal belonging to Group 4 of the periodic table. Also provided is an alcohol production method in which a carbonyl compound is treated using the above catalyst. It is possible to produce an alcohol by a hydrogenation reaction of a carbonyl compound with high selectivity and high efficiency while reducing side reactions. 1. An alcohol production method in which an alcohol is produced from a carbonyl compound , the method comprising producing an alcohol by contacting a carbonyl compound with a catalyst , the catalyst comprising a metal component comprising a first component that is rhenium and one or more second components selected from the group consisting of silicon , gallium , germanium , and indium and a carrier on which the metal component is supported , the carrier comprising an oxide of a metal belonging to Group 4 of the periodic table.2. The alcohol production method according to claim 1 , wherein a mass ratio of elements that are the second components included in the catalyst to the rhenium element included in the catalyst is in a range of 0.1 to 10.3. The alcohol production method according to claim 1 , wherein the oxide of a metal belonging to Group 4 of the periodic table claim 1 , the oxide being included in the catalyst claim 1 , comprises titanium oxide and/or zirconium oxide.4. The alcohol production method according to claim 1 , wherein the catalyst is a catalyst prepared by a method comprising attaching the metal component to a carrier comprising a sulfate ion.5. The alcohol production method according to claim 4 , wherein the sulfate ion content in the carrier is 0.01% by mass to 10% by mass of the mass of the carrier.6. The alcohol production method ...

Method for producing tetrahydrofurane, 1,4-butanediol or gamma-butyrolactone

Processes for preparing tetrahydrofuran and/or butane-1,4-diol and/or gamma-butyrolactone are provided, including a process for preparing tetrahydrofuran (THF) from succinic acid that has been obtained by conversion of biomass, by conversion of the succinic acid to succinic anhydride, and hydrogenation of the succinic anhydride, with removal of certain secondary components.

Fluorine-containing nano composite particles and method for producing the same

Fluorine-containing nano composite particles comprising a condensate of a fluorine-containing alcohol represented by the general formula: R F -A-OH   [I] wherein R F is a perfluoroalkyl group or a polyfluoroalkyl group in which some of the fluorine atoms of the perfluoroalkyl group are replaced by hydrogen atoms, and A is an alkylene group having 1 to 6 carbon atoms; and an alkoxysilane, or fluorine-containing nano composite particles comprising a condensate of a fluorine-containing alcohol represented by the general formula: R F ′-A-OH   [Ia] or the general formula: HO-A-R F ″-A-OH   [Ib] wherein R F ′ is a linear or branched perfluoroalkyl group containing an O, S, or N atom, R F ″ is a linear or branched perfluoroalkylene group containing an O, S, or N atom, and A is an alkylene group having 1 to 6 carbon atoms; and an alkoxysilane.

ARRAY FOR PROCESSING MATERIALS

Materials (e.g., plant biomass, animal biomass, and municipal waste biomass) are processed to produce useful intermediates and products, such as energy, fuels, foods or materials. For example, systems equipment, and methods are described that can be used to treat feedstock materials, such as cellulosic and/or lignocellulosic materials, using an array of vaults. 1. A treatment operating unit , comprising:a plurality of enclosure systems, each enclosure system including one or more vaults, andwithin each vault, an irradiation device and a treatment conveyor.2. The operating unit of claim 1 , wherein the enclosure systems are arranged in rows.3. The operating unit of claim 2 , wherein the rows extend in a first direction claim 2 , and wherein each enclosure system comprises two or more vaults extending in a direction generally perpendicular to the first direction.4. The operating unit of claim 3 , wherein the first and second vaults of each enclosure share a common wall.5. The operating unit of claim 4 , wherein each first vault is configured to accept untreated biomass from a storage facility claim 4 , and wherein the biomass material is treated in each vault utilizing the irradiation device and the treatment conveyor.6. The operating unit of claim 5 , wherein the first vault of each enclosure system further encloses equipment configured to transfer treated biomass from the first vault to the second vault of the enclosure system.7. The operating unit of claim 1 , wherein the irradiation device comprises an electron accelerator.8. The operating unit of claim 1 , wherein the treatment conveyor comprises a vibratory conveyor.9. A method for producing treated materials claim 1 , the method comprising;partitioning a material into a plurality of material portions,conveying the material portions into a plurality of first vaults, each first vault accepting one of the material portions,treating the material portions in the vaults,conveying the material portions out of the ...

Fluorine-containing nano-silica composite particles and method for producing the same

Fluorine-containing nano-silica composite particles comprising a condensate of a fluorine-containing alcohol represented by the general formula: R F -A-OH  [I] wherein R F is a perfluoroalkyl group or a polyfluoroalkyl group in which some of the fluorine atoms of the perfluoroalkyl group are replaced by hydrogen atoms, and A is an alkylene group having 1 to 6 carbon atoms; and an alkoxysilane with nano-silica particles, or fluorine-containing nano-silica composite particles comprising a condensate of a fluorine-containing alcohol represented by the general formula: R F ′-A-OH  [Ia] or the general formula: HO-A-R F ″-A-OH  [Ib] wherein R F ′ is a linear or branched perfluoroalkyl group containing an O, S, or N atom, R F ″ is a linear or branched perfluoroalkylene group containing an O, S, or N atom, and A is an alkylene group having 1 to 6 carbon atoms; and an alkoxysilane with nano-silica particles.

RECONFIGURABLE PROCESSING ENCLOSURES

Biomass (e.g., plant biomass, animal biomass, and municipal waste biomass) or other materials are processed to produce useful intermediates and products, such as energy, fuels, foods or materials. For example, systems and methods are described that can be used to treat feedstock materials, such as cellulosic and/or lignocellulosic materials, in a vault in which the walls and optionally the ceiling include discrete units. Such vaults are re-configurable. 1. A treatment facility comprising:a vault, having walls, ceiling, and a foundation; andwithin the vault, a material conveying system configured to convey biomass under an electron beam, wherein each of the walls comprises a plurality of discrete reconfigurable units and at least one unit of the plurality of units comprises a high Z material.2. The facility as in claim 1 , wherein the ceiling comprises a plurality of discrete units.3. The facility as in claim 1 , wherein the high Z material is a metal with a Z value above 25.4. The facility as in claim 1 , further comprising an electron irradiation device supported by the ceiling of the vault and disposed to irradiate biomass conveyed by the conveying system.5. The facility as in claim 4 , wherein the irradiation device weighs at least 5 Tons.6. The facility as in claim 4 , wherein the irradiation device weighs at least 10 tons.7. The facility as in claim 4 , wherein the irradiation device weighs between about 5 and about 20 tons.8. The facility as in claim 1 , wherein the foundation comprises a concrete slab.9. The facility as in claim 1 , wherein the walls comprise interlocking blocks.10. The facility as in claim 1 , wherein the walls support a network of I-beams and the network of I-beams supports ceiling panels.11. The facility as in claim 1 , wherein the walls claim 1 , ceiling and foundation are at least about 4 feet thick.12. The facility as in claim 1 , wherein the walls claim 1 , ceiling and foundation include concrete and the concrete is selected from the ...

Process for producing 2-butanol from gammavalerolactone

A process is disclosed for selectively producing 2-butanol from GVL by using at least one transition metal catalyst selected from the group consisting of iron, ruthenium, cobalt, rhodium and iridium.

Ethanol Production via Dimethylether Recycle

This invention relates to a process for producing ethanol comprises supplying a feed comprising carbon monoxide, hydrogen and dimethyl ether to a reaction zone operated under conditions such that (i) part of the carbon monoxide in the feed reacts with part of the hydrogen in the feed to produce methanol; (ii) part of the carbon monoxide in the feed reacts with at least part of the dimethyl ether in the feed to produce methyl acetate; and (iii) part of the hydrogen in the feed reacts with at least part of the methyl acetate produced in (ii) to produce an effluent comprising methanol and ethanol. At least part of the ethanol is recovered from the effluent and at least part of the methanol is dehydrated to produce dimethyl ether, which is recycled to the reaction zone.

CHEMISORPTION OF ETHYL ACETATE DURING HYDROGENATION OF ACETIC ACID TO ETHANOL

A hydrogenation catalyst and process using the catalyst for converting a mixture comprising acetic acid and ethyl acetate to ethanol at a first temperature, and the catalyst desorbs ethyl acetate, in the absence of hydrogen, at a second temperature that is greater than the first temperature. The catalyst has a suitable chemisorption of ethyl acetate at the first temperature in the absence of hydrogen. In one embodiment, the first temperature ranges from 125° C. to 350° C. and the second temperature ranges from 300° C. to 600° C. The catalyst comprises one or more active metals or oxide thereof on a support that comprises tungsten or an oxide thereof. The one or more active metals are selected from the group consisting of cobalt, copper, gold, iron, nickel, palladium, platinum, iridium, osmium, rhenium, rhodium, ruthenium, tin, zinc, lanthanum, cerium, manganese, chromium, vanadium, and molybdenum. 1. A hydrogenation catalyst for converting a mixture comprising acetic acid and ethyl acetate to ethanol at a first temperature , the catalyst comprising one or more active metals or oxide thereof on a support that comprises tungsten or an oxide thereof , wherein the one or more active metals are selected from the group consisting of cobalt , copper , gold , iron , nickel , palladium , platinum , iridium , osmium , rhenium , rhodium , ruthenium , tin , zinc , lanthanum , cerium , manganese , chromium , vanadium , and molybdenum; and wherein the catalyst desorbs ethyl acetate , in the absence of hydrogen , at a second temperature that is greater than the first temperature.2. The catalyst of claim 1 , wherein the catalyst has a chemisorption of ethyl acetate at the first temperature in the absence of hydrogen.3. The catalyst of claim 1 , wherein the first temperature ranges from 125° C. to 350° C.4. The catalyst of claim 1 , wherein the second temperature ranges from 300° C. to 600° C.5. The catalyst of claim 1 , wherein the support is selected from the group consisting of ...

Process for Producing Ethanol Using Hydrogenation Catalysts

The present invention relates to catalysts, to processes for making catalysts and to chemical processes employing such catalysts. The catalysts are preferably used for converting acetic acid to ethanol. The catalyst comprises a precious metal and one or more active metals on a modified support. The modified support may comprise cobalt tungstate. 123-. (canceled)24. A process for producing for producing ethanol , comprising contacting a feed stream comprising acetic acid , and/or ethyl acetate , and hydrogen in a reactor at an elevated temperature in the presence of a catalyst under conditions effective to form ethanol , wherein the catalyst comprises a precious metal and one or more active metals on a modified support , wherein the modified support comprises: (i) support material; (ii) a support modifier comprising an oxide of tungsten , molybdenum or vanadium in an amount from 0.1 to 50 wt. % , and (iii) at least one of the one or more active metals.25. The process of claim 24 , wherein the precious metal is selected from the group consisting of rhodium claim 24 , rhenium claim 24 , ruthenium claim 24 , platinum claim 24 , palladium claim 24 , osmium claim 24 , iridium and gold.26. The process of claim 24 , wherein the precious metal is selected from the group consisting of palladium claim 24 , platinum claim 24 , and rhodium.27. The process of claim 24 , wherein the precious metal is present in an amount from 0.05 to 10 wt. %.28. The process of claim 24 , wherein the support modifier is present in an amount from 0.1 wt. % to 40 wt. %.29. The process of claim 24 , wherein the one or more active metals are selected from the group consisting of copper claim 24 , iron claim 24 , cobalt claim 24 , vanadium claim 24 , nickel claim 24 , titanium claim 24 , zinc claim 24 , chromium claim 24 , molybdenum claim 24 , tungsten claim 24 , tin claim 24 , lanthanum claim 24 , cerium claim 24 , and manganese.30. The process of claim 24 , wherein the one or more active metals are ...

Process for producing 1,3-butanediol and for optionally further producing (r)-3-hydroxybutyl (r)-3-hydroxybutyrate

A process is described for producing 1,3-butanediol, wherein an ester of poly-(R)-3-hydroxybutyrate such as formed by transesterification with an alcohol is reduced by hydrogenation in the presence of a skeletal copper-based catalyst to provide 1,3-butanediol. The 1,3-butanediol may be transesterified by reaction with additional poly-(R)-3-hydroxybutyrate ester to produce (R)-3-hydroxybutyl (R)-3-hydroxybutyrate.

Process for Producing Oxalic Acid

A process for producing oxalic acid containing or having the following steps: i) Utilizing a chemical reaction to produce an alkali metal formate and/or alkaline earth metal formate; ii) Converting the alkali metal formate and/or alkaline earth metal formate to an alkali metal oxalate and/or alkaline earth metal oxalate in a thermal reaction, preferably utilizing hydrogen in the process; iii) Converting the alkali metal oxalate and/or alkaline earth metal oxalate to oxalic acid and an alkali metal base and/or alkaline earth metal base utilizing an electrochemical process; and iv) Recycling the alkali metal base and/or alkaline earth metal base from step (iii) to step (i). 1. A method for producing oxalic acid , comprising the following steps:i) Utilizing a chemical reaction to produce an alkali metal formate and/or alkaline earth metal formate;ii) Converting the alkali metal formate and/or alkaline earth metal formate to an alkali metal oxalate and/or alkaline earth metal oxalate in a thermal reaction, preferably utilizing hydrogen in the process;iii) Converting the alkali metal oxalate and/or alkaline earth metal oxalate to oxalic acid and an alkali metal base and/or alkaline earth metal base utilizing an electrochemical process; andiv) Recycling the alkali metal base and/or alkaline earth metal base from step (iii) to step (i).2. The method according to claim 1 , wherein step (i) comprises utilizing a chemical reaction to convert carbon claim 1 , carbon monoxide claim 1 , carbon dioxide claim 1 , methane claim 1 , hydrogen or a combination of any of these to thereby produce an alkali metal formate and/or alkaline earth metal formate.3. The method according to claim 1 , wherein the alkali metal base and/or alkaline earth metal base in step (iv) is recycled from step (iii) into step (i) in addition to hydrogen claim 1 , oxygen claim 1 , or chlorine.4. The method according to claim 1 , wherein step (i) further includes the use of an electrochemical cell for the ...

Shaped porous carbon products

Shaped porous carbon products and processes for preparing these products are provided. The shaped porous carbon products can be used, for example, as catalyst supports and adsorbents. Catalyst compositions including these shaped porous carbon products, processes of preparing the catalyst compositions, and various processes of using the shaped porous carbon products and catalyst compositions are also provided.

FLEXIBLE CHEMICAL PRODUCTION PLATFORM

Disclosed are integrated systems and methods for the conversion of epoxides to beta lactones and to multiple Cproducts and/or Cproducts. 1. A system for the production of Cand Cproducts , comprising:an epoxide source;a carbon monoxide (CO) source; an inlet configured to receive epoxide from the epoxide source and CO from the CO source,', 'a central reaction zone configured to convert at least some of the epoxide to a beta lactone, and', 'an outlet configured to provide an outlet stream comprising the beta lactone,, 'a central reactor, comprising [{'sub': '3', 'claim-text': an inlet configured to receive the outlet stream comprising beta lactone of the central reactor,', {'sub': 3', '3, 'a first Creaction zone configured to convert at least some of the beta lactone to a first Cproduct, and'}, {'sub': '3', 'an outlet configured to provide an outlet stream comprising the first Cproduct,'}], '(i) a first Creactor, comprising, {'sub': '3', 'claim-text': an inlet configured to receive the outlet stream comprising beta lactone of the central reactor,', {'sub': 3', '3, 'a second Creaction zone configured to convert at least some of the beta lactone to a second Cproduct, and'}, {'sub': '3', 'an outlet configured to provide an outlet stream comprising the second Cproduct, and'}], '(ii) a second Creactor, comprising, {'sub': '4', 'claim-text': an inlet configured to receive the outlet stream comprising beta lactone of the central reactor,', {'sub': 4', '4, 'a first Creaction zone configured to convert at least some of the beta lactone to a first Cproduct, and'}, {'sub': '4', 'an outlet configured to provide an outlet stream comprising the first Cproduct, and'}], '(iii) a first Creactor, comprising], 'two or more of (i)-(iii)a controller to independently modulate production of the beta lactone and each of the products,{'sub': 3', '3, 'provided that the first Cproduct differs from the second Cproduct.'}2. The system of claim 1 , wherein the epoxide is ethylene oxide (EO) and the ...

Preparation of Butanol from Ethanol Derived from Fermentation

In one embodiment, the present application discloses methods to selectively synthesize higher alcohols and hydrocarbons useful as fuels and industrial chemicals from syngas and biomass. Ketene and ketonization chemistry along with hydrogenation reactions are used to synthesize fuels and chemicals. In another embodiment, ketene used to form fuels and chemicals may be manufactured from acetic acid which in turn can be synthesized from synthesis gas which is produced from coal, biomass, natural gas, etc. 137-. (canceled)39. The method of claim 38 , wherein Rand Rare hydrogen and the formula I is ketene claim 38 , and the ketene is prepared from acetic acid.40. The method of where the acetic acid which is made from ethanol.41. The method of where the ethanol is prepared by fermentation.38. The method of where butanol is a product.43. The method of where the transition metal catalyst comprises more than one transition metal.44. The method of wherein the transition metal catalyst is a copper zinc oxide based catalyst.45. The method of wherein the transition metal catalyst is combined with a main group metal.46. The method of wherein the butanol is blended with an automotive fuel.48. The method of wherein the Calcohol is methanol.49. The method of where the Calcohol is butanol.50. The method of claim 41 , wherein Rand Rare hydrogen and the formula I is ketene claim 41 , and the ketene is prepared from acetic acid.51. The method of where the acetic acid which is prepared from ethanol.52. The method of where the ethanol is prepared by fermentation.53. The method of where the metal catalyst is a transition metal.54. The method of where the metal catalyst is a transition metal.55. The method of where the transition metal catalyst comprises a main group metal.56. The method of where the transition metal catalyst is a copper-zinc based catalyst. This application claims the benefit of U.S. Provisional Application No. 61/558,321 filed Nov. 10, 2011 entitled “Synthesis of Higher ...

METHOD OF MANUFACTURE OF OCTANEDIOIC ACID, PRECURSORS, AND DERIVATIVES

A method for the manufacture of 1,8-octanedioic acid comprises: reacting gamma-valerolactone with an alcohol in the presence of an acid or a base catalyst to provide an alkyl pentenoate, converting the alkyl pentenoate in the presence of a metathesis initiator to provide the dialkyl octenedioate, reacting the dialkyl octenedioate with hydrogen in the presence of a hydrogenation catalyst to provide a dialkyl 1,8-octanedioate and hydrolyzing the dialkyl 1,8-octanedioate to provide the 1,8-octanedioic acid. 2. The method of claim 1 , wherein the metathesis initiator is a transition metal carbene metathesis initiator claim 1 , a transition metal salt in combination with an alkylating agent claim 1 , and a transition metal complex capable of forming an active metal carbene by reaction with an olefin.3. The method of claim 1 , wherein converting the alkyl pentenoate having the formula (4) to the dialkyl octenedioate having the formula (1) comprises conducting the metathesis at a temperature of about −20° C. to about 600° C. and a pressure of about 0 to about 2000 psig.2132.-. (canceled) This application claims the priority to U.S. Provisional Patent Application Ser. No. 61/790,826, filed on Mar. 15, 2013, the contents of which are incorporated herein by reference in their entirety.This disclosure relates to a method for the manufacture of octanedioic acid, its precursors, and the derivatives of octanedioic acid and its precursors. These compounds can be used directly, or as intermediates to produce other derivatives.A method for the manufacture of a dialkyl octenedioate having the formula (1)wherein R is a Calkyl, preferably a Calkyl, comprises: reacting gamma-valerolactone having the formula (2)with an alcohol having the formula (3) R—OH (3) in the presence of an acid or a base catalyst to provide an alkyl pentenoate having the formula (4)and converting the alkyl pentenoate having the formula (4) in the presence of a metathesis initiator to provide the dialkyl ...

Recovering Ethanol with Sidestreams to Regulate C3+ Alcohols Concentrations

This invention relates to purification and/or recovery of ethanol from a crude ethanol product obtained from the hydrogenation of acetic acid. Separation and purification processes of a crude ethanol mixture are employed to allow recovery of ethanol and remove impurities. In particular, the process involves one or more sidestreams to regulate C 3 + alcohols concentration in the recovered ethanol.

Processing materials

Biomass feedstocks (e.g., plant biomass, animal biomass, and municipal waste biomass) are processed to produce useful products, such as fuels. For example, novel systems, methods and equipment for conveying and/or cooling treated biomass are described.

Process for the separation and purification of a mixed diol stream

Disclosed is a process for the purification of a mixed diol stream. The mixed diol stream comprising two-, three-, and four-carbon diols is separated into component diols by extraction with a hydrophobic solvent mixture. The diols recovered in the extractant may be removed from the extractant stream by back extraction with water or by distillation with an azeotrope-forming agent present, preferably an azeotroping agent already present in the extractant mixture.

PROCESS FOR TREATING HOMOSERINE-BASED COMPOUND

The present disclosure relates to the preparation of a useful compound, which can be used as an intermediate for preparing an important compound in the industrial field from a homoserine-based compound, and provides a process for treating a homoserine-based compound, capable of mass-producing a useful compound from a homoserine-based compound in a simple manner with excellent efficiency. 1. A process for preparing gamma-butyrolactone , a gamma-butyrolactone derivative , furanone , dialkyl succinate , a by-product , or a mixture thereof , comprising:{'sub': 'x', 'reacting a solution of a homoserine-based compound with NO(step 1); and'}recovering gamma-butyrolactone, a gamma-butyrolactone derivative, furanone, dialkyl succinate, a by-product, or a mixture thereof from the products obtained in step 1 (step 2),wherein, in step 1, x is any of 1, 1.5, 2, and 3.2. The process according to claim 1 , wherein NO claim 1 , directly as a gas or in the form of an acid or salt claim 1 , reacts with the homoserine-based compound in step 1.3. The process according to claim 2 , wherein the acid or salt is HNO claim 2 , NHNO claim 2 , NaNO claim 2 , Fe(NO) claim 2 , Al(NO) claim 2 , Cu(NO) claim 2 , Bi(NO) claim 2 , Zn(NO) claim 2 , or Pb(NO).4. The process according to claim 2 , wherein the reaction with the NOin step 1 is performed by injecting NO gas; or NO gas in combination with Ogas claim 2 , an inert gas claim 2 , or a mixture thereof.5. The process according to claim 1 , wherein the solvent for the solution of a homoserine-based compound is water claim 1 , chloroform claim 1 , dichloroform claim 1 , methanol claim 1 , halo-gamma-butyrolactone claim 1 , or a mixture thereof.6. The process according to claim 1 , wherein the homoserine-based compound is homoserine claim 1 , homoserine lactone claim 1 , O-acetylhomoserine claim 1 , O-succinyl homoserine claim 1 , homoserine lactone hydrochloride claim 1 , homoserine lactone hydrobromide claim 1 , or a mixture thereof.7. The ...

PROCESSING MATERIALS

Biomass feedstocks (e.g., plant biomass, animal biomass, and municipal waste biomass) are processed to produce useful products, such as fuels. For example, novel systems, methods and equipment for conveying and/or cooling treated biomass are described. 1. An apparatus for processing a biomass material , the apparatus comprising:a first treatment cell equipped with a first electron beam device for irradiating a biomass material therein with electron beams;a screw conveyor for cooling and conveying the biomass material from the first treatment cell.2. The apparatus of claim 1 , further including a second treatment cell equipped with a second electron beam device for further irradiating the biomass material.3. The apparatus of claim 1 , wherein the screw conveyor includes interior portions that are cooled.4. The apparatus of claim 3 , wherein the interior portions are cooled using a chilled liquid.5. The apparatus of claim 3 , wherein the interior portions include a hollow shaft and hollow flight.6. The apparatus of further including a geothermal ground loop for cooling the chilled liquid.7. The apparatus of claim 1 , wherein the cooling reduces the temperature of the biomass material by between about 1° C. and 110° C.8. The apparatus of claim 1 , wherein the cooling reduces the temperature of the biomass material by between about 10° C. and about 75° C.9. The apparatus of claim 1 , wherein the cooling reduces the temperature of the biomass material by between about 10° C. and about 50° C.10. The apparatus of claim 1 , wherein a total dose delivered is between about 1 and 200 Mrad.11. The apparatus of claim 1 , wherein a total dose delivered is between about 10 Mrad and about 50 Mrad.12. The apparatus of claim 1 , wherein a total dose delivered is between about 20 Mrad and about 40 Mrad.13. The apparatus of claim 1 , wherein the temperature of the biomass material during the irradiation does not exceed about 160° C.14. The apparatus of claim 1 , wherein the temperature ...

Processing materials

Materials, such as biomass feedstocks (e.g., plant biomass, animal biomass, and municipal waste biomass) are processed to produce useful products, such as fuels. Conveying systems, such as flowing gas conveying systems and such as closed-loop flowing gas conveying systems are described.

ENCLOSURES FOR TREATING MATERIALS

Biomass (e.g., plant biomass, animal biomass, and municipal waste biomass) is processed to produce useful intermediates and products, such as energy, fuels, foods or materials. For example, systems and methods are described that can be used to treat feedstock materials, such as cellulosic and/or lignocellulosic materials, in two or more vaults that can share a common wall. 115-. (canceled)16. A biomass treatment facility , comprising:a first conveying system configured to convey a biomass material through a first enclosure while exposing the biomass material to a first dose of ionizing radiation from a first electron accelerator to produce a first treated biomass material; anda second conveying system configured to convey the first treated biomass material through a second enclosure while exposing the first treated biomass material to a second dose of ionizing radiation from a second electron accelerator to produce a second treated biomass material.17. The facility of claim 16 , wherein the first and second enclosure share a common wall.18. The facility of claim 16 , wherein each accelerator operates at a power of between about 100 kW and about 300 kW.19. The facility of claim 16 , wherein walls of both the first and second enclosures are fabricated from discrete interconnecting blocks configured to provide a photo-tight structure. This application is a continuation of PCT/US14/21604 filed Mar. 7, 2014 which claims priority to the following provisional applications: U.S. Ser. No. 61/774,684, filed Mar. 8, 2013; U.S. Ser. No. 61/774,773, filed Mar. 8, 2013; U.S. Ser. No. 61/774,731, filed Mar. 8, 2013; U.S. Ser. No. 61/774,735, filed Mar. 8, 2013; U.S. Ser. No. 61/774,740, filed Mar. 8, 2013; U.S. Ser. No. 61/774,744, filed Mar. 8, 2013; U.S. Ser. No. 61/774,746, filed Mar. 8, 2013; U.S. Ser. No. 61/774,750, filed Mar. 8, 2013; U.S. Ser. No. 61/774,752, filed Mar. 8, 2013; U.S. Ser. No. 61/774,754, filed Mar. 8, 2013; U.S. Ser. No. 61/774,775, filed Mar. 8, 2013; U.S ...

PROCESSES TO CREATE MULTIPLE VALUE STREAMS FROM BIOMASS SOURCES

Use of diverse biomass feedstock in a process for the recovery of target C5 and C6 alditols and target glycols via staged hydrogenation and hydrogenolysis processes is disclosed. Particular alditols of interest include, but are not limited to, xylitol and sorbitol. Various embodiments of the present invention synergistically improve overall recovery of target alditols and/or glycols from a mixed C5/C6 sugar stream without needlessly driving total recovery of the individual target alditols and/or glycols. The result is a highly efficient, low complexity process having enhanced production flexibility, reduced waste and greater overall yield than conventional processes directed to alditol or glycol production. 1. A process , comprising:selecting a target alditol or a target blend of alditols,hydrogenating continuously a mixed C5/C6 monomer sugar stream to form a mixed C5/C6 alditol stream;isolating the target alditol or target blend of alditols from the mixed C5/C6 alditol stream to leave a residual mixed C5/C6 alditol stream;continuous hydrogenolysis of the residual mixed C5/C6 alditol stream to form a mixed C2-C4 glycol stream; andisolating a target glycol or target blend of glycols from the mixed C2-C4 glycol stream;wherein at least 10% of the overall target product yield is either target alditol/target blend of alditols or target glycol/target blend of glycols.23.-. (canceled)4. The process of claim 1 , wherein the monomer sugar stream or the mixed C5/C6 monomer sugar stream comprises greater than or equal to 60% C5 monomer sugar based on the combined total of C5 and C6 monomer sugars claim 1 , specifically greater than or equal to 65% C5 monomer sugar claim 1 , and more specifically greater than or equal to 70% C5 monomer sugar; orwherein the monomer sugar stream or the mixed C5/C6 monomer sugar stream comprises greater than or equal to 60% C6 monomer sugar based on the combined total of C5 and C6 monomer sugars, specifically greater than or equal to 65% C6 ...

Hydrogenation Reaction Conditions To Produce Ethanol and Reduce Ethyl Acetate Formation

The present invention is directed to processes for selective formation of ethanol from acetic acid by hydrogenating acetic acid in the presence of a hydrogenation catalyst, wherein the temperature and liquid hourly space velocity (LHSV) are controlled to maximize acetic acid conversion and to minimize selectivity to ethyl acetate. The hydrogenation catalyst comprises a metal selected from the group consisting of platinum, palladium, gold, iridium, osmium, and rhodium on a support modified by at least one support modifier selected from the group consisting of (i) alkaline earth metal oxides, (ii) alkali metal oxides, (iii) alkaline earth metal metasilicates, (iv) alkali metal metasilicates, (v) Group IIB metal oxides, (vi) Group IIB metal metasilicates, (vii) Group IIIB metal oxides, (viii) Group IIIB metal metasilicates, and mixtures thereof. 1. A process for producing ethanol , comprising contacting acetic acid and hydrogen in a reactor at a temperature of greater than 225° C. in the presence of a catalyst , under conditions effective to form ethanol , wherein the liquid hourly space velocity of the acetic acid fed to the reactor is from 0.3 to 1.6 hr , wherein the catalyst comprises at least one metal selected from the group consisting of platinum , palladium , gold , iridium , osmium , and rhodium , on a support modified by a support modifier selected from the group consisting of (i) alkaline earth metal oxides , (ii) alkali metal oxides , (iii) alkaline earth metal metasilicates , (iv) alkali metal metasilicates , (v) Group IIB metal oxides , (vi) Group IIB metal metasilicates , (vii) Group IIIB metal oxides , (viii) Group IIIB metal metasilicates , and mixtures thereof.2. The process of claim 1 , wherein the temperature is from 225° C. to 300° C.3. The process of claim 1 , wherein the temperature is from 250° C. to 300° C.4. The process of claim 1 , wherein the liquid hourly space velocity of the acetic acid fed to the reactor is from 1 to 1.3 hr.5. The process ...

Ruthenium complex, method for producing same, and use of same

The present invention provides a novel ruthenium complex that is easy to produce and handle and that can be supplied relatively inexpensively, a method for producing this ruthenium complex, a method for producing alcohols and the like using this ruthenium complex as a catalyst, a method for producing carbonyl compounds using this ruthenium complex as a catalyst, and a method for producing N-alkylamine compounds using this ruthenium complex as a catalyst. The present invention pertains to a ruthenium complex represented by general formula (1) RuX 1 X 2 (PNP) (NHC) m (Solv) n (1) (in general formula (1), X 1 and X 2 each independently represent a monovalent anionic monodentate ligand; PNP represents a tridentate aminodiphosphine ligand, NHC represents an N-heterocyclic carbene derived from a nitrogen-containing heterocyclic ring, and Solv represents a coordinating solvent; and m represents an integer from 1 to 3, n represents an integer from 0 to 2, and 1≦m+n≦3.), a method for producing the same, a catalyst including the same, and methods for producing various organic compounds using this catalyst.

CARBON-BASED, PRECIOUS METAL-TRANSITION METAL COMPOSITE CATALYST AND PREPARATION METHOD THEREFOR

The present invention relates to a carbon-based precious metal-transition metal composite catalyst and a preparation method therefor, and more particularly, to a catalyst synthesis method in which, when preparing a high-content precious metal-transition metal composite catalyst, a catalyst having uniform particles and composition can be prepared, and cyclohexane dimethanol (CHDM) is efficiently produced by the hydrogenation reaction of cyclohexane dicarboxylic acid (CHDA) in an aqueous solution. Provided is a method for preparing a carbon-based precious metal-transition metal composite catalyst, wherein, in the carbon-based precious metal-transition metal composite catalyst, the precious metal is included in an amount of 10-20 parts by weight, and the transition metal is included in an amount of 10-20 parts by weight based on 100 parts by weight of the composite catalyst, and thus a total amount of the precious metal-transition metal is 20-40 parts by weight based on 100 parts by weight of the composite catalyst.

Process for Recovering Ethanol

Recovery of ethanol from a crude ethanol product obtained from the hydrogenation of acetic acid. Separation and purification processes of the crude ethanol products are employed to allow recovery of ethanol and remove impurities. 122-. (canceled)23. A process for recovering ethanol , comprising:hydrogenating an acetic acid feed stream in the presence of a catalyst to form a crude ethanol product;separating at least a portion of the crude ethanol product in a first column into a first distillate comprising ethanol and water, and a first residue comprising less than 30 wt. % water, based on the total weight of the first residue;introducing at least a portion of the first distillate in a second column and recovering a second residue comprising ethanol and water;separating at least a portion of the second residue in a third column into a third distillate comprising ethanol and a third residue comprising water; anddirectly or indirectly returning at least a portion of the first residue to a reactor for the hydrogenation of acetic acid.24. The process of claim 23 , wherein the crude ethanol product and first distillate further comprise a light end compound selected from the group consisting of acetaldehyde claim 23 , ethyl acetate claim 23 , and mixtures thereof.25. The process of claim 24 , further comprising recovering a second distillate from the second column claim 24 , wherein the second distillate comprises at least light end compound.26. The process of claim 24 , wherein the second distillate comprises from 1 to 25 wt. % acetaldehyde and from 10 to 90 wt. % ethyl acetate.27. The process of claim 23 , wherein the crude ethanol product comprises from 0 to 90 wt. % acetic acid and further comprises from 0 to 20 wt. % ethyl acetate.28. The process of claim 27 , wherein the second residue comprises less than 3 wt. % ethyl acetate.29. The process of claim 23 , wherein the crude ethanol product comprises from 5 to 35 wt. % water and from 5 to 70 wt. % ethanol.30. The ...

Process for Vapor Phase Hydrogenation

A process for selective formation of ethanol from acetic acid includes contacting a feed stream containing acetic acid and hydrogen at an elevated temperature with catalyst comprising platinum and tin on a high surface area silica promoted with calcium metasilicate. Selectivities to ethanol of over 85% are achieved at 280° C. with catalyst life in the hundreds of hours. 1108-. (canceled)109. A process for the production of ethanol by reduction of acetic acid comprising passing a gaseous stream comprising hydrogen and acetic acid in the vapor phase in a molar ratio of hydrogen to acetic acid of at least about 4:1 at a temperature of between about 225° C. and 300° C. over a particulate hydrogenation catalyst comprising a silicaceous support having dispersed thereon a platinum group metal selected from the group consisting of platinum , palladium and mixtures thereof , with a promoter metal comprising cobalt , the silicaceous support having a surface area of at least 175 m/g and being chosen from the group consisting of silica , calcium metasilicate and calcium metasilicate promoted silica having calcium metasilicate disposed on the surface thereof , the surface of the silicaceous support being essentially free of Bronsted acid sites due to alumina unbalanced by calcium.110. The process of claim 109 , wherein the catalyst consists of silicaceous support having dispersed thereon a platinum group metal and cobalt.111. The process of claim 109 , wherein the silicaceous support is silica.112. The process of claim 109 , wherein the silicaceous support is calcium metasilicate.113. The process of claim 109 , wherein the silicaceous support has a surface area of at least 200 m/g.114. The process of claim 109 , wherein the platinum group metal is present from 0.5 to 5 wt. % claim 109 , based on the total weight of the catalyst.115. The process of claim 109 , wherein a weight ratio of cobalt to platinum group metal is from 20:1 to 3:1.116. A process for the production of ethanol ...

METHOD FOR REGENERATING HYDROGENATION CATALYST

The present invention relates to a method for regenerating a dicarboxylic acid or carboxylic acid hydrogenation catalyst, and more particularly, to a method for regenerating a hydrogenation catalyst to be used in a reaction of converting a dicarboxylic acid group into a diol group. The present invention provides an effect of regenerating a catalyst deactivated by the deposition of esters to be produced in a reaction of converting a dicarboxylic acid group into a diol group. 1. A method for regenerating a catalyst used in a hydrogenation reaction of carboxylic acid or carboxylic acid ester , the method comprising the steps of:(a) adding a used catalyst to an organic solvent and washing the catalyst while stirring the catalyst;(b) separating and recovering the catalyst by filtering after the washing; and(c) drying and reactivating the separated and recovered catalyst.2. A method for regenerating a catalyst used in a hydrogenation reaction of carboxylic acid or carboxylic acid ester , the method comprising the steps of:(i) adding a used catalyst and a solvent to a reactor;(ii) replacing a composition of gas inside the reactor with hydrogen; and(iii) reactivating the catalyst by performing a hydrothermal hydrogenation reaction while stirring under a condition in which a reactor internal temperature is 100-400° C. and a hydrogen gas pressure is 1-20 Mpa.3. The method of claim 1 , wherein the organic solvent includes at least one selected from the group consisting of acetone claim 1 , pyridine claim 1 , hexafluoroisopropanol claim 1 , methanol claim 1 , ethanol claim 1 , propanol claim 1 , butanol claim 1 , cyclohexane claim 1 , toluene claim 1 , and dichloromethane.4. The method of claim 1 , wherein the step (a) of washing the catalyst while stirring the catalyst is performed at 0-150° C. for 0.15-12 hours.5. The method of claim 1 , wherein the drying in the step (c) is performed at a temperature of 40-200° C.6. The method of claim 2 , wherein the solvent in the step (i) ...

Carbon-based noble metal-transition metal catalyst enabling high selective conversion and production method therefor

Provided are a carbon-based noble metal-transition metal composite catalyst enabling high selective conversion of a carboxylic acid functional group into an alcohol functional group by pre-treating a carbon carrier including a predetermined ratio or more of mesopores, and a production method therefor.

Transition metal isonitrile catalysts

The present disclosure relates to new transition metal isonitrile compounds, processes for the production of the compounds and the use of the compounds as catalysts. The disclosure also relates to the use of the metal isonitrile compounds as catalysts for hydrogenation and transfer hydrogenation of compounds containing one or more carbon-oxygen, and/or carbon-nitrogen and/or carbon-carbon double bonds.

Combined Column for Separating Products of Different Hydrogenation Reactors

Recovery of ethanol from a crude product comprising ethyl acetate obtained from the hydrogenation of acetic acid. The crude product is separated to form an organic stream that may be subjected to hydrogenolysis to form ethanol. The organic phase may comprise ethyl acetate is reacted via hydrogenolysis form ethanol that may be directly or indirectly fed to the separation zone or the hydrogenation reactor.

System and method for producing 1,4-cyclohexanedimethanol and 1,4-cyclohexanedicarboxylic acid from terephthalic acid

This invention relates to the continuous production of 1,4-cyclohexane dimethanol (CHDM) and optionally and additionally of 1,4-cyclohexane dicarboxylic acid (CHDA) directly using terephthalic acid (TPA) as the raw material. More specifically, this invention relates to a method and system for continuous production of CHDM and CHDA that features direct use of TPA as feedstock, promotes efficient use of solvent and energy, and provides products with the desired high trans isomer content, by exploiting unexpected features of the thermodynamic phase behavior and the reaction mechanisms.

BIOMASS-DERIVED POLYMERS AND COPOLYMERS INCORPORATING MONOLIGNOLS AND THEIR DERIVATIVES

The invention includes methods and materials for forming and manipulating aromatic-based polymers and copolymers using biomass compounds as starting materials. Embodiments of the invention can be used in processes designed to replace those used in the petro-chemical industry. Typical embodiments of the invention include methods and materials for forming and/or modifying compounds including dicarboxylic acid ester dimers, benzoxazines and dicarboxylic acid ether dimers. Embodiments of the invention further provide methods and materials for utilizing these compounds to form commercially desirable polymers having structures and physical properties akin to those found in polymers formed from petroleum products. 1. A method of forming a dicarboxylic acid ester dimer comprising the steps of:(a) reacting an aromatic aldehyde with a malonic ester in a Doebner modification of a Knoevenagel condensation reaction so as to generate an ester compound;(b) reacting the ester compound of (a) with a deprotonating agent in situ so as to generate a salt of the ester compound;(c) reacting the salt of the ester compound of (b) with a diacid chloride or bromide in a salt metathesis reaction so as to generate an ester of a monolignol dimer; and(d) converting the ester of a monolignol dimer of (c) into a carboxylic acid via a reaction with trifluoroacetic acid (TFA);so that a dicarboxylic acid ester dimer is formed.2. The method of further comprising:converting the dicarboxylic acid ester dimer to a diacid chloride via a reaction with a thionyl chloride;removing excess thionyl chloride under vacuum;dissolving the diacid chloride ester dimer in a halogenated organic solvent; andcombining the halogenated organic solvent solution with an aqueous basic solution comprising a diamine in a condensation polymerization reaction so as to form a poly(ester-amide).3. The method of claim 2 , wherein the diamine is an aliphatic or aromatic diamine.5. The method of claim 2 , wherein the polyester-airside ...

ORGANIC COMPOUNDS

A process for the hydrogenation of a substrate comprising a carbon heteroatom double bond in the presence of a transition metal complex comprising a tridentate or bisdentate-ligand containing a nitrogen, sulphur and phosphorus atom, of which at least the N- and P- and optionally also the S-atom coordinates with the transition metal. 2. A process according to claim 1 , wherein the nitrogen atom on the tridentate or bisdentate ligand forms part of an amine group or an imine group; the sulphur atom forms part of an aliphatic group or forms part of an aromatic ring; and the phosphorus atom forms part of a phosphine group.3. A process according to or wherein the nitrogen atom-containing group is flanked on one side by the phosphorus atom-containing group claim 1 , and on the other side by the sulphur atom-containing group.6. A process according to any of the preceding claims wherein the metal M is ruthenium or osmium.7. A process according to any of the preceding claims wherein the functional group that is hydrogenated is selected from the group consisting of an ester claim 1 , lactone claim 1 , ketone claim 1 , aldehyde claim 1 , amide claim 1 , lactam and imine.8. A process according to any of the preceding claims wherein the substrate bearing a functional group containing a carbon heteroatom double bond is sclareolide and the hydrogenated product is sclareodiol.11. A complex according to wherein the nitrogen atom on the tridentate or bisdentate ligand forms part of an amine group or an imine group; the sulphur atom forms part of an aliphatic group or forms part of an aromatic ring; and the phosphorus atom forms part of a phosphine group.12. A complex according to or claim 10 , wherein the nitrogen atom-containing group is flanked on one side by the phosphorus atom-containing group claim 10 , and on the other side by the sulphur atom-containing group.15. A complex according to any of the through wherein the metal M is ruthenium or osmium. The present invention relates ...

PREPARATION METHOD FOR CYCLOHEXANE DIMETHANOL HAVING HIGH TRANS CONTENT AND CYCLOHEXANE DIMETHANOL PREPARED THEREBY

Provided is a preparation method for a cyclohexane dimethanol (CHDM), which can have a high trans content through particular conditions, additive addition, or reactant addition, which is controlled in a cyclohexane dicarboxylic acid (CHDA) hydrogenation reaction, and a cyclohexane dimethanol prepared thereby. 1. A method for preparing a cyclohexane dimethanol (CHDM) by performing a hydrogenation reaction of a catalyst and a cyclohexane dicarboxylic acid (CHDA) , wherein a weight ratio of the catalyst to the cyclohexane dicarboxylic acid (CHDA) is 1:1 to 1:5.2. The method of claim 1 , wherein at least one selected from a homogeneous additive and a heterogeneous additive is further included in the hydrogenation reaction.3. The method of claim 2 , wherein the homogeneous additive includes at least one selected from the group consisting of ammonium bicarbonate (NHHCO) claim 2 , sodium hydroxide (NaOH) claim 2 , potassium carbonate (KCO) claim 2 , and sodium borohydride (NaBH) claim 2 , and the heterogeneous additive includes at least one selected from the group consisting of zirconia claim 2 , titania claim 2 , ceria claim 2 , silica claim 2 , and magnesia.4. The method of claim 2 , wherein a weight ratio of the homogeneous additive to the catalyst is 1:0.05 to 1:1.5. The method of claim 2 , wherein a weight ratio of the heterogeneous additive to the catalyst is 1:0.5 to 1:3.6. The method of claim 1 , wherein the hydrogenation reaction of the cyclohexane dicarboxylic acid (CHDA) is performed in a temperature range of 200° C. to 280° C.7. The method of claim 1 , wherein the hydrogenation reaction of the cyclohexane dicarboxylic acid (CHDA) is performed in a pressure range of 50 bar to 150 bar.8. The method of claim 1 , wherein the hydrogenation reaction of the cyclohexane dicarboxylic acid (CHDA) is performed for 1 hour to 8 hours.9. The method of claim 1 , wherein the cyclohexane dicarboxylic acid (CHDA) uses a reactant selected from a cis form claim 1 , a trans form ...

HYDROFORMYLATION METHOD FOR THE LARGE-SCALE PRODUCTION OF ALDEHYDES AND/OR ALCOHOLS

A process for preparing Cto Cmonohydroxy compounds from a bottom fraction arising in the distillation of a crude mixture of Cto Coxo-process aldehydes from cobalt-catalyzed or rhodium-catalyzed hydroformylation, or in the distillation of a crude mixture of Cto Coxo-process alcohols, which comprises contacting the bottom fraction in the presence of hydrogen with a catalyst comprising copper oxide and aluminum oxide, at a temperature of 150° C. to 300° C. and a pressure of 20 bar to 300 bar and subjecting the resulting crude hydrogenation product to distillation, and the amount of Cto Cmonohydroxy compounds present in the crude hydrogenation product after the hydrogenation being greater than the amount of Cto Cmonohydroxy compounds given stoichiometrically from the hydrogenation of the ester and aldehyde compounds present in the bottom fraction, including the Cto Cmonohydroxy compounds still present in the bottom fraction before the hydrogenation. 19.-. (canceled)10. A process for preparing Cto Cmonohydroxy compounds from a bottom fraction arising in the distillation of a crude mixture of Cto Coxo-process aldehydes from cobalt-catalyzed or rhodium-catalyzed hydroformylation , or in the distillation of a crude mixture of Cto Coxo-process alcohols , which comprises contacting the bottom fraction in the presence of hydrogen with a catalyst comprising copper oxide (CuO) and aluminum oxide , at a temperature of 180° C. to 260° C. and a pressure of 150 bar to 280 bar and subjecting the resulting crude hydrogenation product to distillation , and the amount of Cto Cmonohydroxy compounds present in the crude hydrogenation product after the hydrogenation being greater than the amount of Cto Cmonohydroxy compounds given stoichiometrically from the hydrogenation of the ester and aldehyde compounds present in the bottom fraction , including the Cto Cmonohydroxy compounds still present in the bottom fraction before the hydrogenation.11. The process according to claim 10 , wherein ...

METHODS OF PRODUCING COMPOUNDS FROM 5-(HALOMETHYL)FURFURAL

Provided herein are methods of producing compounds, such as cyclohexanone, hexanediamine, hexanediol, hexamethylenediamine, caprolactam and nylon, from 5-(halomethyl)furfural. 2. A method of producing cyclohexanone , comprising:converting 5-(halomethyl)furfural to hexane-1,5-diol;oxidizing the hexane-1,5-diol to produce 6-hydroxyhexan-2-one; andcyclizing the 6-hydroxyhexan-2-one to produce cyclohexanone.4. A method of producing hexane-1 ,6-diol , comprising:contacting 5-(halomethyl)furfural with an alkanolate or acetate salt to produce 5-(alkoxymethyl)furan-2-carbaldehyde; andreducing the 5-(alkoxymethyl)furan-2-carbaldehyde to produce hexane-1,6-diol.7. The method of claim 6 , wherein the compound of formula (A) and the ammonia are further combined with a copper catalyst to produce the compound of formula (G) and/or a salt thereof.10. A method of producing hexamethylenediamine claim 6 , comprising:converting 5-(halomethyl)furfural to (tetrahydrofuran-2,5-diyl)dimethanamine; andconverting the (tetrahydrofuran-2,5-diyl)dimethanamine to hexamethylenediamine.11. The method of claim 10 , wherein the converting of 5-(halomethyl)furfural to (tetrahydrofuran-2 claim 10 ,5-diyl)dimethanamine comprises:converting the 5-(halomethyl)furfural to (5-(iminomethyl)furan-2-yl)methanamine; andconverting the (5-(iminomethyl)furan-2-yl)methanamine to the (tetrahydrofuran-2,5-diyl)dimethanamine.12. The method of claim 10 , wherein the converting of 5-(halomethyl)furfural to (tetrahydrofuran-2 claim 10 ,5-diyl)dimethanamine comprises:combining the 5-(halomethyl)furfural with ammonia to produce (5-(iminomethyl)furan-2-yl)methanamine; andreducing the (5-(iminomethyl)furan-2-yl)methanamine to produce the (tetrahydrofuran-2,5-diyl)dimethanamine.13. The method of claim 10 , wherein the converting of 5-(halomethyl)furfural to (tetrahydrofuran-2 claim 10 ,5-diyl)dimethanamine comprises:converting the 5-(halomethyl)furfural to (5-(azidomethyl)furan-2-yl)methanimine; andconverting the (5-( ...

METHODS FOR PREPARATION OF AMMONIUM SALTS OF C4 DIACIDS BY FERMENTAION AND INTEGRATED METHODS FOR MAKING C4 DERIVATIVES

Methods for forming ammonium salts of C4 diacids in a fermentation process with removal of divalent metal carbonate salts are disclosed. The pH of fermentation broths for production of C4 diacids is controlled by adding alkaline oxygen containing calcium or magnesium compounds, which forms divalent metal salts of the diacids. The divalent metal salts of the diacids are substituted with ammonium by introduction of ammonium salts at elevated temperature and pressure forming soluble ammonium salts thereof. C02 or bicarbonate is simultaneously added to the fennentation media at the elevated temperature and pressure. Reducing the temperature and pressure forms insoluble divalent metal carbonate salts that are separated from the solubilized ammonium diacid salts. 1. A method of making C4 acid derivative compound , comprising ,obtaining a clarified fermentation broth from growth of a microorganism to produce at least one diammonium salt of a C4 diacid selected from the group consisting of succinic, malic, maleic and fumaric acid; and{'sub': '2', 'contacting the clarified fermentation broth containing the diammonium salt of the C4 diacid with a hydrogenation catalyst and Hin a reaction mixture under conditions of temperature, pressure and time sufficient to hydrogenate the diammonium salt of the C4 diacid to form a derivative compound selected from the group consisting of -methyl-2-pyrrolidone (NMP), gamma-butyrolactone (GBL) and 1,4-butane-diol (BDO).'}2. The method of wherein the derivative compound is NMP claim 1 , and methanol is included in the clarified fermentation broth during the contacting with the hydrogenation catalyst.3. The method of wherein the derivative compound is GBL; C4 diacids in the fermentation broth comprise primarily succinate or are reduced to succinic acid during the hydrogenation; a dioxane solvent is included in the hydrogenation reaction mixture; and the hydrogenation catalyst for formation of the GBL comprises palladium and AlO.4. The method ...

Catalysts and processes for the hydrogenation of amides

There is provided a process for the reduction of one or more amide moieties in a compound comprising contacting the compound with hydrogen gas and a transition metal catalyst in the presence or absence of a base under conditions for the reduction an amide bond. The presently described processes can be performed at low catalyst loading using relatively mild temperature and pressures, and optionally, in the presence or absence of a base or high catalyst loadings using low temperatures and pressures and high loadings of base to effect dynamic kinetic resolution of achiral amides.

Hydroconversion of renewable feedstocks

A hydroconversion process comprises contacting a feedstock comprising renewable materials under hydroprocessing conditions with a promoted catalyst selected from a self-supported catalyst, a supported catalyst and combinations thereof, wherein the reaction conditions can be tailored to directly convert the renewable feedstock to the desired product(s) including fatty alcohols, esters, normal paraffins, or combinations thereof. The catalyst comprising at least a Group VIB metal selected from molybdenum and tungsten, a Group VIII metal selected from cobalt and nickel to convert the feedstock into any of fatty alcohols, esters, and normal paraffins. In some embodiments, the process further comprising additional steps to generate various desirable products, including α-olefins (or PAO, by dehydrating the fatty alcohol products), lubricants and bright stocks (from the oligomerizing of the PAO), and Group 3 lubricants (from co-oligomerizing of the PAO with some short chain olefins).

Group VIII Metal Hydrogenolysis Catalysts Having Low Selectivity to Ethers

Group VIII metal containing catalysts used in processes for producing ethanol from ethyl acetate by reacting the ethyl acetate with hydrogenation. The Group VIII metal containing catalyst has a selectivity to ether, especially diethyl ether, that is very low. The process may be integrated with an ethyl acetate production process, such as esterification, hydrogenation, or dehydrogenation. 1. A process for producing ethanol comprisingcontacting a feed stream comprising ethyl acetate with hydrogen in a reactor in the presence of a catalyst to produce a crude ethanol product that comprises less than 0.5 wt. % ether compounds, wherein the catalyst comprises tin, a Group VIII metal selected from the group consisting of palladium, platinum, and combinations thereof, and a support that comprises calcium, magnesium, tungsten, or molybdenum, provided that when the support comprises tungsten and/or molybdenum, the catalyst further comprises cobalt and/or the support further comprises cobalt and/or tin.2. The process of claim 1 , wherein the crude ethanol product comprises from 0.0001 to 0.5 wt. % diethyl ether.3. The process of claim 1 , wherein the support comprises a support material selected from the group consisting of silica claim 1 , pyrogenic silica claim 1 , and high purity silica.4. The process of claim 3 , wherein the support material is substantially free of alumina.5. The process of claim 1 , wherein the selectivity to ether compounds is less than 1%.6. The process of claim 1 , wherein the support comprises calcium oxide claim 1 , calcium silicate claim 1 , calcium metasilicate claim 1 , magnesium oxide claim 1 , magnesium silicate claim 1 , or magnesium metasilicate.7. The process of claim 1 , wherein the support comprises from 1 to 25 wt. % calcium or magnesium claim 1 , based on the total weight of the catalyst.8. The process of claim 1 , wherein the support comprises tungsten oxide claim 1 , cobalt tungstate claim 1 , molybdenum oxide claim 1 , cobalt molybdate ...

Catalytic conversion of carbon dioxide to methanol

The present disclosure relates to a new catalytic process for the production of methanol from carbon dioxide, comprising: (1) the conversion of carbon dioxide and hydrogen to formic acid or formate salts; (2) converting the formic acid or formate salts to diformate esters of diols; (3) hydrogenating the diformate esters to methanol and diols. The diols produced from the hydrogenation reaction can be recovered and re-used to prepare the diformate esters.

PROCESSING MATERIALS

Biomass feedstocks (e.g., plant biomass, animal biomass, and municipal waste biomass) are processed to produce useful products, such as fuels. For example, novel systems, methods and equipment for conveying and/or cooling treated biomass are described. 1. A system for processing a biomass material comprising:a first treatment cell equipped with a first electron beam device for irradiating the biomass material with electron beams, anda screw conveyor comprising a housing and interior portions, wherein the interior portions convey the irradiated biomass material from the first treatment cell and the housing is cooled.2. The system of claim 1 , further comprising a second treatment cell equipped with an second electron beam device claim 1 , wherein the screw conveyor conveys the biomass material from the first treatment cell to the second treatment cell.3. The system of claim 1 , wherein the housing is cooled using a chilled liquid.4. The system of claim 3 , wherein the housing is cooled using water or glycol water mixtures.5. The system of claim 1 , wherein the screw conveyor comprises two or more screws.6. The system of claim 1 , wherein the screw conveyor has a material inlet and a material discharge.7. The system of claim 1 , wherein the first and second treatment cells are capable of delivering a total dose of between about 1 and 200 Mrad.8. The system of claim 7 , wherein the first and second treatment cells are capable of delivering a total dose of between about 10 Mrad and about 50 Mrad.9. The system of claim 8 , wherein the first and second treatment cells are capable of delivering a total dose of between about 20 Mrad and about 40 Mrad.10. The system of claim 1 , wherein the screw conveyor further comprises a notched flight for comminuting the biomass material while it is conveyed.11. The system of claim 1 , wherein the biomass comprises a lignocellulosic material.12. The system of claim 2 , wherein at least one of the first and second electron beam devices ...

Process To Recover Alcohol From An Ethyl Acetate Residue Stream

Recovery of ethanol from a crude ethanol product obtained from the hydrogenation of acetic acid using a low energy process. The crude ethanol product is separated in a column to produce a distillate stream comprising acetaldehyde and a residue stream comprising ethanol, acetic acid, ethyl acetate and water. The ethanol product is recovered from the residue stream. 118-. (canceled)19. A process for producing ethanol comprising:providing a crude ethanol product stream comprising ethanol, ethyl acetate, acetaldehyde, and water;separating at least a portion of the crude ethanol product stream in a first distillation column to form a first distillate comprising acetaldehyde and a first residue comprising ethanol, ethyl acetate and water;separating at least a portion of the first residue to form an organic stream comprising ethyl acetate and ethanol and an aqueous stream comprising water; andseparating the organic stream in a second distillation column to form a second distillate comprising ethyl acetate and a second residue comprising ethanol.2021-. (canceled)22. A process for producing ethanol comprising:hydrogenating acetic acid and/or an ester thereof in a reactor in the presence of a catalyst to form a crude ethanol product;separating a portion of the crude ethanol product in a first distillation column to yield a first distillate comprising acetaldehyde and a first residue comprising ethanol, acetic acid and/or ethyl acetate;separating a portion of the first residue in a second distillation column to yield a second residue comprising high boiling point components and a second distillate comprising ethanol and ethyl acetate; andseparating at least a portion of the second distillate to yield a third distillate comprising ethyl acetate and a third residue comprising ethanol.23. The process of claim 22 , wherein the high boiling point components are selected from the group consisting of acetic acid claim 22 , water claim 22 , alcohols having more than 2 carbon atoms ...

Process to Recover Alcohol with Reduced Water From Overhead of Acid Column

A process for recovering ethanol obtained from the hydrogenation of acetic acid. The crude ethanol product is separated in a column to produce a distillate stream comprising acetaldehyde and ethyl acetate and a residue stream comprising ethanol, acetic acid, ethyl acetate and water. The ethanol product is recovered from the residue stream.

Polyhydroxyalkanoate derivatives, preparation and uses thereof

Provided herein are methods that utilize polyhydroxyalkanoates (PHAs) as a substrate for further conversion to C4 and C5 compounds. Polyhydroxyalkanoates can undergo esterification to yield alkyl hydroxyalkanoates and alkyl alkenoates, which may serve as useful precursors in the production of alkadienes and alkenedioic acids, including for example butadiene and butenedioic acid.

Ethanol Refining Process Using Intermediate Reboiler

The present invention relates to processes for producing and recovering ethanol using an intermediate reboiler. An intermediate stream may be withdrawn from a removal zone of a distillation column and recirculated through the intermediate reboiler to the distillation column. The distillation column may also comprise a bottoms reboiler.

LIGAND, METAL COMPLEX CONTAINING LIGAND, AND REACTION USING METAL COMPLEX CONTAINING LIGAND

A hydrogen transfer reaction may be more efficiently promoted by using a metal complex represented by Formula (2): 37-. (canceled)911-. (canceled)13. A method for producing a hydrogen transfer reaction product , comprising the step of:{'claim-ref': {'@idref': 'CLM-00008', 'claim 8'}, 'subjecting an organic compound to a dehydrogenation reaction (oxidation reaction) in the presence of the compound according to .'}14. (canceled)16. A method for producing a hydrogen transfer reaction product , comprising the step of:{'claim-ref': {'@idref': 'CLM-00015', 'claim 15'}, 'subjecting an organic compound to a hydrogenation reaction in the presence of the catalyst for hydrogenation reaction according to .'}19. The compound according to claim 18 , wherein claim 18 , in Formula (2a) claim 18 , Rare the same or different claim 18 , and each represents a methyl group claim 18 , ethyl group claim 18 , n-propyl group claim 18 , isopropyl group claim 18 , n-butyl group claim 18 , isobutyl group claim 18 , sec-butyl group claim 18 , pentyl group claim 18 , hexyl group claim 18 , or Ccycloalkyl group.21. A method for producing a dehydrogenation reaction product claim 18 , comprising the step of:{'claim-ref': {'@idref': 'CLM-00020', 'claim 20'}, 'subjecting an organic compound to a dehydrogenation reaction in the presence of the catalyst for dehydrogenation reaction according to .'}23. The compound according to claim 22 , wherein claim 22 , in Formula (2a) claim 22 , Rare the same or different claim 22 , and each represents a linear or branched Calkyl group claim 22 , or Ccycloalkyl group.25. A method for producing a dehydrogenation reaction product claim 22 , comprising the step of:{'claim-ref': {'@idref': 'CLM-00024', 'claim 24'}, 'subjecting an organic compound to a dehydrogenation reaction in the presence of the catalyst for dehydrogenation reaction according to .'} The present invention relates to a ligand, a metal complex comprising the ligand, and a reaction (specifically, ...

METHOD OF PRODUCING ESTOLIDE HAVING HIGH STRUCTURAL STABILITY

Disclosed is a method of producing an estolide having high structural stability, including: a) preparing a fatty acid mixture from biomass-derived oil; b) separating the fatty acid mixture into a C16 fatty acid and a C18 fatty acid; c) converting the C18 fatty acid into a C18 or C17 linear internal olefin; and d) subjecting the C18 or C17 linear internal olefin and the C16 fatty acid to an estolide reaction, thus obtaining an estolide. 1. A method of producing an estolide having high structural stability , comprising:a) preparing a fatty acid mixture from biomass-derived oil;b) separating the fatty acid mixture into a C16 fatty acid and a C18 fatty acid;c) converting the C18 fatty acid into a C18 or C17 linear internal olefin; andd) subjecting the C18 or C17 linear internal olefin and the C16 fatty acid to an estolide reaction, thus obtaining an estolide.2. A method of producing an estolide having high structural stability , comprising:A) preparing a fatty acid mixture from biomass-derived oil; andB) subjecting the fatty acid mixture to an estolide reaction and then hydrodeoxygenation, thus obtaining an estolide.3. The method of claim 1 , wherein c) comprises converting the C18 fatty acid into a C18 linear internal olefin through partial hydrogenation and dehydration.4. The method of claim 1 , wherein c) comprises converting the C18 fatty acid into a C17 linear internal olefin through decarbonylation.5. The method of claim 1 , further comprising e) performing hydrotreating to increase stearic acid content claim 1 , between steps a) and b).6. The method of claim 1 , further comprising f) hydrotreating the C18 fatty acid separated in b) to increase stearic acid content claim 1 , between steps b) and c).7. The method of claim 2 , further comprising C) performing hydrotreating to increase stearic acid content claim 2 , after A).8. The method of claim 2 , further comprising D) separating or purifying the estolide obtained in B) to obtain a desired estolide.9. The method ...