Abstract: Contact of a crude feed with one or more catalysts containing a transition metal sulfide produces a total product that includes a crude product. The crude feed has a residue content of at least 0.2 grams of residue per gram of crude feed. The crude product is a liquid mixture at 25° C. and 0.101 MPa. One or more properties of the crude product may be changed by at least 10% relative to the respective properties of the crude feed. In some embodiments, gas is produced during contact with one or more catalysts and the crude feed.

Abstract: Contact of a crude feed with one or more catalysts containing a transition metal sulfide produces a total product that includes a crude product. The crude feed has a residue content of at least 0.2 grams of residue per gram of crude feed. The crude product is a liquid mixture at 25° C. and 0.101 MPa. One or more properties of the crude product may be changed by at least 10% relative to the respective properties of the crude feed. In some embodiments, gas is produced during contact with one or more catalysts and the crude feed.

Abstract: Contact of a crude feed with a hydrogen source in the presence of an inorganic salt catalyst produces a total product that includes a crude product. The crude feed has a residue content of at least 0.2 grams of residue per gram of crude feed. The inorganic salt catalyst may includes one or more alkali metal salts and/or one or more alkaline-earth metal salts. The crude product is a liquid mixture at 25° C. and 0.101 MPa. One or more properties of the crude product may be changed by at least 10% relative to the respective properties of the crude feed.

Abstract: Method of producing a total product are described. A method includes providing a feed and a supported inorganic salt catalyst to a contacting zone. Contact of the supported inorganic salt catalyst with the feed in the presence of a hydrogen source and steam in the contacting zone at a temperature of at most 1000° C. and a total operating pressure of at most 4 MPa produces the total product.

Abstract: Contact of a crude feed with a hydrogen source in the presence of an inorganic salt catalyst produces a total product that includes a crude product. The crude feed has a residue content of at least 0.2 grams of residue per gram of crude feed. The inorganic salt catalyst comprises alkali metals, alkaline earth metals, or mixtures thereof. The crude product is a liquid mixture at 25° C. and 0.101 MPa. One or more properties of the crude product may be changed by at least 10% relative to the respective properties of the crude feed.

Abstract: Contact of a crude feed with one or more catalysts containing a transition metal sulfide produces a total product that includes a crude product. The crude feed has a residue content of at least 0.2 grams of residue per gram of crude feed. The crude product is a liquid mixture at 25° C. and 0.101 MPa. One or more properties of the crude product may be changed by at least 10% relative to the respective properties of the crude feed. In some embodiments, gas is produced during contact with one or more catalysts and the crude feed.

Abstract: Contact of a crude feed with a hydrogen source in the presence of an inorganic salt catalyst produces a total product that includes a crude product. The crude feed has a residue content of at least 0.2 grams of residue per gram of crude feed. The inorganic salt catalyst comprises alkali metals, alkaline earth metals, or mixtures thereof. The crude product is a liquid mixture at 25° C. and 0.101 MPa. One or more properties of the crude product may be changed by at least 10% relative to the respective properties of the crude feed.

Abstract: Contact of a crude feed with a hydrogen source in the presence of an inorganic salt catalyst produces a total product that includes a crude product. The crude feed has a residue content of at least 0.2 grams of residue per gram of crude feed. The inorganic salt catalyst includes one or more alkali metals. The crude product is a liquid mixture at 25° C. and 0.101 MPa. One or more properties of the crude product may be changed by at least 10% relative to the respective properties of the crude feed.

Abstract: Contact of a crude feed with a hydrogen source in the presence of an inorganic salt catalyst produces a total product that includes a crude product. The crude feed has a residue content of at least 0.2 grams of residue per gram of crude feed. The inorganic salt catalyst may include one or more alkali metals. The crude product is a liquid mixture at 25° C. and 0.101 MPa. One or more properties of the crude product may be changed by at least 10% relative to the respective properties of the crude feed.

Abstract: Contact of a crude feed with one or more catalysts produces a total product that includes a crude product. The crude feed has a residue content of at least 0.2 grams of residue per gram of crude feed. The crude product is a liquid mixture at 25° C. and 0.101 MPa. One or more properties of the crude product may be changed by at least 10% relative to the respective properties of the crude feed. In some embodiments, gas is produced during contact with one or more catalysts and the crude feed.

Abstract: Contact of a crude feed with a hydrogen source in the presence of an inorganic salt catalyst produces a total product that includes a crude product. The crude feed has a residue content of at least 0.2 grams of residue per gram of crude feed. The inorganic salt catalyst may include one or more alkali metals. The crude product is a liquid mixture at 25° C. and 0.101 MPa. One or more properties of the crude product may be changed by at least 10% relative to the respective properties of the crude feed.

Abstract: Disclosed is a method for selective carboxylation of naphthoic acid, or other aromatic mono-acids to form primarily 2,3-naphthalene dicarboxylic acid (2,3-NDA) or other aromatic diacids which comprises reacting said aromatic mono-acid in the presence of one or more metal oxide catalysts, alone, or in combination, and in the presence of about 0.2 to 0.8 moles excess of base over aromatic mono-acid, at a temperature of about 380° C. to about 420° C., and, in a second step, disproportionating the product of said selective carboxylation at a temperature above about 420° C. to form a product with a greatly improved yield of 2,6-naphthalene dicarboxylic acid, or other aromatic dicarboxylic acid.

Abstract: Disclosed is a process for disproportionation of potassium naphthoate to the dipotassium salt of 2,6-NDA which gives reproducible improved yields of up to 40% which comprises: a) reacting naphthoic acid in the presence of excess base to produce a disproportionation feed comprising a finely dispersed disordered salt mixture of excess base salts and naphthoic acid salts, wherein the feed is prepared by the steps of: (1) Reacting naphthoic acid in the presence of excess base selected from the group consisting of carbonates and bicarbonates to form a salt; (2) Drying said salt mixture by a method which forms a highly mixed disordered salt mixture characterized by a differential scanning calorimeter(DSC) signature characterized by low melting peaks not previously observed in the salt; and b) Disproportionating said solid salts in the presence of a disproportionation catalyst to form the dipotassium salts of 2,6-NDA.

Abstract: Disclosed is an integrated process for producing 2,6-naphthalene dicarboxylicacid comprising oxidizing a methylnaphthalene feedstock, hydrodebrominating the crude naphthoic acid product under conditions different from any work known in the art, forming a potassium salt of the acid; disproportionating the potassium salt to produce 2,6 potassium salts of NDA; selectively precipitating K2NDA; selectively precipitating the monopotassium salt of 2,6 NDA(KHNDA); disproportionating the KHNDA into 2,6 NDA and K2NDA; further reacting the 2,6 NDA in a pipe reactor; and drying the product 2,6 NDA by conventional means or directly slurrying directly into a PEN process. The process can tolerate impurities in the economical methylnaphthalene feed and the resulting 2,6 NDA is of high quality with <50 ppm potassium.

Abstract: Disclosed is a method for selective carboxylation of naphthoic acid, or other aromatic mono-acids to form primarily 2,3-naphthalene dicarboxylic acid (2,3-NDA) or other aromatic diacids which comprises reacting said aromatic mono-acid in the presence of one or more metal oxide catalysts, alone, or in combination, and in the presence of about 0.2 to 0.8 moles excess of base over aromatic mono-acid, at a temperature of about 380° C. to about 420° C., and, in a second step, disproportionating the product of said selective carboxylation at a temperature above about 420° C. to form a product with a greatly improved yield of 2,6-naphthalene dicarboxylic acid, or other aromatic dicarboxylic acid.

Abstract: A method is provided to produce dicarboxylic or tricarboxylic aromatic acid from salts of such acids, the method including the steps of providing an aqueous solution of a salt of a dicarboxylic or tricarboxylic aromatic acid, the aqueous solution having a pH of about 7 or greater; contacting the aqueous solution with sufficient carbon dioxide to lower the pH of the aqueous solution resulting in precipitation of at least a portion of the dicarboxylic or tricarboxylic aromatic acid; separating precipitated dicarboxylic or tricarboxylic aromatic acid from the solution; and recovering carbon dioxide from the solution.

Abstract: Disclosed is a process for manufacturing an aromatic diacid in one step with a single catalyst system which comprises: a) Introducing into a reactor an aromatic hydrocarbon containing the number of rings desired in the product diacid with one or more alkyl groups attached to the rings; b) Reacting said aromatic hydrocarbon in the presence of an oxidant supply and a single catalyst system comprising at least one catalyst selected from Group IB, IIB, VB, or VIIB of the Periodic Table, in a reaction medium capable of stabilizing the aromatic acids formed against further oxidation to water and CO2, or decarboxylation to aromatic hydrocarbons, and also capable of allowing the isomerization of the acids so formed to the desired diacids; and c) Reacting said hydrocarbon feed with said oxidant in the presence of said catalyst system until a desired amount of said feed is oxidized to carboxylic acids and isomerized to the desired diacid product.

Abstract: Disclosed is a method for selective carboxylation of naphthoic acid, or other aromatic mono-acids to form primarily 2,3-naphthalene dicarboxylic acid (2,3-NDA) or other aromatic diacids which comprises reacting said aromatic mono-acid in the presence of one or more metal oxide catalysts, alone, or in combination, and in the presence of about 0.2 to 0.8 moles excess of base over aromatic mono-acid, at a temperature of about 380° C. to about 420° C., and, in a second step, disproportionating the product of said selective carboxylation at a temperature above about 420° C. to form a product with a greatly improved yield of 2,6-naphthalene dicarboxylic acid, or other aromatic dicarboxylic acid.

Abstract: An oxidation free process for converting a hydroxy substituted aromatic to an aromatic diacid which comprises reacting a hydroxy substituted aromatic with excess basic salt in the presence of carbon dioxide at disproportionation/isomerization reaction conditions.

Abstract: Stable high internal phase water-in-oil emulsions containing polymerizable vinyl monomers, crosslinking monomers and initiators are obtained, useful in producing low density porous crosslinked polymeric materials by using a surfactant system containing (a) an anionic surfactant, the anionic surfactant having an oil soluble tail and an anionic functional group and (b) one or more quatemary salts having one or more hydrocarbon groups having greater than or equal to 8 carbon atoms. A water-in-oil emulsion can be formed with lower surfactant concentration than sorbitan fatty acid ester alone and improved surfactant performance at elevated temperatures is obtained.