Abstract: The present invention describes a process for production of neopentyl glycol (NPG) from formaldehyde (FD) and isobutyraldehyde (IBD). FD and IBD first react to form hydroxypivaldehyde (HPD) in an aldol condensation step, then HPD is hydrogenated to form NPG in a hydrogenation step. The aldol condensation step is performed using a solid catalyst such as an ion exchange resin catalyst, which can be easily separated from the reaction product. The feed to the aldol condensation step is made homogeneous by adjusting the ratio of IBD, FD, and water in the feed or by adding a solvent that is miscible with both IBD and water. High purity NPG is recovered from the product of the hydrogenation step by a suitable method such as crystallization.

Abstract: 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.

Abstract: 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.

Abstract: The present invention describes a process for production of neopentyl glycol (NPG) from formaldehyde (FD) and isobutyraldehyde (IBD). FD and IBD first react to form hydroxypivaldehyde (HPD) in an aldol condensation step, then HPD is hydrogenated to form NPG in a hydrogenation step. The aldol condensation step is performed using a solid catalyst such as an ion exchange resin catalyst, which can be easily separated from the reaction product. The feed to the aldol condensation step is made homogeneous by adjusting the ratio of IBD, FD, and water in the feed or by adding a solvent that is miscible with both IBD and water. High purity NPG is recovered from the product of the hydrogenation step by a suitable method such as crystallization.

Abstract: Embodiments of the present invention describe systems and methods for production of methyl isobutyl ketone (MIBK) from acetone and hydrogen in a two-step process. In a first step, acetone is converted to a product stream containing mesityl oxide (MO) at a temperature in the range of about 0-120° C. and a pressure in the range of about 1-3 atm. The composition of the product stream from the first reaction step is adjusted so that the resulting stream can undergo a favorable liquid-liquid separation in a decanter, and an MO rich product stream can be recovered. The composition of the feed to the decanter is controlled by choosing the number of reactor stages for the first reaction step and their operating temperatures, and/or by recycling some MIBK to the decanter feed. The method does not require a substantially complete conversion of acetone in the first reaction step, nor does it require a removal of DAA from the product of the first reaction step by separation.

Abstract: Embodiments of the present invention describe systems and methods for production of methyl isobutyl ketone (MIBK) from acetone and hydrogen in a two-step process. In a first step, acetone is converted to a product stream containing mesityl oxide (MO) at a temperature in the range of about 0-120° C. and a pressure in the range of about 1-3 atm. The composition of the product stream from the first reaction step is adjusted so that the resulting stream can undergo a favorable liquid-liquid separation in a decanter, and an MO rich product stream can be recovered. The composition of the feed to the decanter is controlled by choosing the number of reactor stages for the first reaction step and their operating temperatures, and/or by recycling some MIBK to the decanter feed. The method does not require a substantially complete conversion of acetone in the first reaction step, nor does it require a removal of DAA from the product of the first reaction step by separation.

Abstract: The present invention relates generally to processes and systems for the production of liquefied petroleum gas (LPG). More specifically, embodiments of the present invention relate to improved methods and systems for the direct reaction of synthesis gas (syngas) to liquefied petroleum gas.

Abstract: A system and method are provided for producing Bisphenol-A (BPA) using direct crystallization of BPA in a single crystallization stage. In one embodiment the method comprises reacting Phenol and Acetone in the presence of a catalyst to form a product solution including Bisphenol-A and Phenol; removing a part of the Phenol from the product solution if required, and providing a selective amount of solvent, so as to obtain a product solution with the desired phase equilibrium behavior; and feeding the product solution with a selective composition to a crystallization stage operated at a selected temperature, so as to recover substantially pure Bisphenol-A in crystal form.

Abstract: A system and method for producing bisphenol-A (BPA) is provided. In particular, the present invention provides a system and method of producing bisphenol-A wherein the phase equilibrium behavior of a feed solution to a crystallizer is selectively controlled and adjusted to provide desired results. This provides a powerful tool, whereby certain operating conditions or variables of the bisphenol-A process can be selectively adjusted to generate desired phase equilibrium behavior. In general, bisphenol-A is produced from a reaction of phenol and acetone, forming a product solution including phenol, bisphenol-A, isomers of bisphenol-A, unreacted reactants and by-products. A solvent is provided in the product solution and the amount and composition of solvent in the product solution are selectively controlled to adjust the composition of the product solution fed to a crystallizer such that either crystalline bisphenol-A, or an adduct of bisphenol-A and phenol is crystallized from the product solution.

Abstract: A system and method are provided for producing Bisphenol-A (BPA) using direct crystallization of BPA in a single crystallization stage. In one embodiment the method comprises reacting Phenol and Acetone in the presence of a catalyst to form a product solution including Bisphenol-A and Phenol; removing a part of the Phenol from the product solution if required, and providing a selective amount of solvent, so as to obtain a product solution with the desired phase equilibrium behavior; and feeding the product solution with a selective composition to a crystallization stage operated at a selected temperature, so as to recover substantially pure Bisphenol-A in crystal form.

Abstract: A method of separating one or more solid compound from an adduct is provided. More specifically, the present invention provides a method of separating one or more solid compounds from an adduct by crystallization wherein certain phase equilibrium conditions are selectively controlled.

Abstract: A system and method for producing bisphenol-A (BPA) is provided. In particular, the present invention provides a system and method of producing bisphenol-A wherein the phase equilibrium behavior of a feed solution to a crystallizer is selectively controlled and adjusted to provide desired results. This provides a powerful tool, whereby certain operating conditions or variables of the bisphenol-A process can be selectively adjusted to generate desired phase equilibrium behavior. In general, bisphenol-A is produced from a reaction of phenol and acetone, forming a product solution including phenol, bisphenol-A, isomers of bisphenol-A, unreacted reactants and by-products. A solvent is provided in the product solution and the amount and composition of solvent in the product solution are selectively controlled to adjust the composition of the product solution fed to a crystallizer such that either crystalline bisphenol-A, or an adduct of bisphenol-A and phenol is crystallized from the product solution.

Abstract: A method of producing aldehydes in a hydroformylation system wherein an olefinic compound is reacted with hydrogen and carbon monoxide in a hydroformylation reaction in the presence of a catalyst is provided. The hydroformylation system includes a reactor and a downstream catalyst process path. The temperature in the reactor and downstream catalyst process path is less than approximately 100° C., and preferably less than approximately 85° C., and most preferably less than approximately 80° C., such that formation of high boiler components from the reaction are substantially minimized. Further, the method of the present invention reduces degradation or decomposition of the catalyst, and in particular the ligand compound.

Abstract: A method and system for producing 1,4-butanediol (1,4-BG), and optionally additionally tetrahydrofuran (THF), that promotes more efficient usage of water (H2O) is provided. In one aspect, the method is comprised of supplying at least one feed stream including 1,4-diacetoxybutane (1,4-DAB), 1,4-hydroxyacetoxybutane (1,4-HAB) and H2O to at least one reactor. 1,4-DAB, 1,4-HAB and H2O are reacted in the reactor to produce at least one effluent stream that includes 1,4-BG, 1,4-HAB, H2O, unreacted 1,4-DAB and acetic acid. The effluent stream is supplied to a separation system having one or more separators where at least a portion of the 1,4-HAB is removed from the effluent stream and recycled back to the reaction. Alternatively, 1,4-HAB may be supplied directly to the reactor as a feed stream, or a combination of feed stream and recycled 1,4-HAB may be used.