Tate & Lyle Technology Limited

European Sugar Holdings S.a.r.l.

Tate & Lyle Ingredients Americas LLC

The Mcburney Corporation

John Kerr

Robert P Jansen

Anthony Baiada

Duane Leinhos

James Edwin Wiley, Jr

Raymond C Ganga

Greg Imig

Blake McBurney

Gordon Walker

David A Dentel

Steven J Reust

Carlo Maffezzoni

Sebastien Camborieux

Christian J Isaac

Robert Jensen

Steve J Reust

James Edwin Wiley

Robert Jansen

Carlo Maffezoni

A process for removing dimethylamine (DMA) before and/or during and/or after deacylation in a reaction vessel of a feed stream comprising a sucralose-6-acylate resulting from the chlorination of a sucrose-6-acylate in the presence of dimethyl formamide (DMF), wherein the deacylation is conducted at a first set of conditions of temperature, pH and pressure, the process comprising: (a) providing a side stream loop from and to the reaction vessel; (b) adjusting the conditions of one or more of temperature, pH, and pressure in the loop, and setting the flow rate through the loop, to remove DMA while minimising carbohydrate degradation.

Process for removing dimethylamine

A process for the extraction of sucralose from an aqueous solution containing at least sucralose, other chlorinated saccharides, sodium chloride and dimethylammonium chloride into an organic solvent for sucralose by contacting said organic solvent with said solution to extract sucralose into the organic solvent. The ratio of sodium chloride to dimethylammonium chloride in the aqueous solution is increased prior to or during contact so as to increase the partition coefficient of sucralose into said organic solvent.

Sucralose purification process

A method of removing a carboxylic acid from a liquid that contains a tertiary amide solvent includes a step of contacting the liquid with an extraction medium comprising an amine. The amine is immiscible with both water and the tertiary amide solvent, and the contacting step forms a de-acidified phase containing the tertiary amide solvent and a phase containing the extraction medium and the carboxylic acid. Both the liquid that contains the tertiary amide solvent and the de-acidified phase may also contain a sucrose-6-acylate.

Removal of acids from tertiary amide solvents

The present invention provides a method for producing sucralose from a feed stream resulting from the chlorination of a sucrose-6-acylate in a reaction vehicle. The feed stream includes a sucralose-6-acylate, the reaction vehicle, water, and salts. The salts include one or more selected from the group consisting of alkali metal chlorides, alkaline earth metal chlorides and ammonium chloride. The method includes:

Method for the production of sucralose

The present invention provides a method for producing sucralose from a feed stream including a sucrose-6-acylate in a reaction vehicle. The method includes:

A method of inverting sucrose, including (i) determining an initial solids concentration of an aqueous sucrose solution, an initial bed volume of a sucrose inversion resin system, a minimum target inversion percentage, a maximum target inversion percentage, a target maximum hydroxymethylfuran (HMF) concentration, a minimum target pH, or a maximum target pH; (ii) contacting the sucrose inversion resin system with the aqueous sucrose solution under conditions of aqueous solution flow rate and aqueous solution temperature to produce an inverted sucrose solution having an inversion percentage, an HMF concentration, and a pH; (iii) observing an instantaneous inversion percentage, an instantaneous HMF concentration, or an instantaneous pH of the inverted sucrose solution; and, if appropriate; (iv) changing at least one of the aqueous solution flow rate or the aqueous solution temperature to yield a product having a desired inversion percentage, HMF concentration, and/or pH. An apparatus capable of performing the method.

Sucrose inversion process

A method for extracting energy from biomass depleted of at least some carbohydrate, at least some oil, or both by a) introducing the biomass into a vertically elongated combustion chamber having i) at least one suspension burner at the top of the combustion chamber which is capable of projecting a flame down the axis of the combustion chamber, ii) a heat transfer apparatus having at least a portion of a heat collection surface located radially from the flame and below the burner, and iii) an exhaust opening located below the flame and below at least a portion of the heat collection surface; b) combusting the biomass to yield a mixture containing hot flue gas and molten ash above the exhaust opening; c) transferring heat from the hot flue gas to at least a portion of the heat collection surface substantially by radiation prior to any substantial contact of ash to a surface of the combustion chamber, to yield a mixture containing warm flue gas and non-molten ash and having a lower molten ash content than the mixture yielded by the combusting step; and d) cooling the warm flue gas with cold gas, to yield a mixture containing cool flue gas and non-molten ash and having a lower molten ash content than the mixture yielded by the transferring step.

Process for efficient energy recovery from biomass

An apparatus for extracting energy from fiber introduced as a fuel into a vertically elongated combustion chamber having a suspension burner capable of projecting a flame down the axis of the combustion chamber with a heat collection surface located radially from the flame and below the burner, and an exhaust opening located below the flame and below at least a portion of the heat collection surface, in which the combusted fiber yields a mixture containing hot flue gas and molten ash above the exhaust opening and heat transfers therefrom to the heat collection surface prior to any substantial contact of ash to a surface of the combustion chamber, to yield a mixture containing warm flue gas and non-molten ash, that is thereafter cooled to yield a mixture containing cool flue gas and non-molten ash.

Biomass energy recovery apparatus

We disclose a method of inverting sucrose, including (i) determining an initial solids concentration of an aqueous sucrose solution (solids), an initial bed volume (BV) of a sucrose inversion resin system, a minimum target inversion percentage (invert %), a maximum target inversion percentage (invert %), a target maximum hydroxymethylfuran (HMF) concentration (HMF), a minimum target pH (pH), or a maximum target pH (pH); (ii) contacting the sucrose inversion resin system with the aqueous sucrose solution under conditions of aqueous solution flow rate in BV/hr (rate) and aqueous solution temperature in &#xb0; C. (temperature) to produce an inverted sucrose solution having an inversion percentage (invert %), an HMF concentration (HMF), and a pH (pH); (iii) observing an instantaneous inversion percentage (invert %), an instantaneous HMF concentration (HMF), or an instantaneous pH (pH) of the inverted sucrose solution; and, if invert %&#x3c;invert %, invert %&#x3e;invert %, HMF&#x3e;HMF, pH&#x3c;pH, or pH&#x3e;pH; (iv) changing at least one of the aqueous solution flow rate or the aqueous solution temperature such that invert %&#x2266;invert %&#x2266;invert %, HMF&#x2266;HMF, or pH&#x2266;pH&#x2266;pH. We also disclose a computing apparatus capable of use in performing a method of inverting sucrose.

A process for the recovery of glycerol comprises contacting an aqueous feed composition that comprises water, glycerol, and at least one contaminant with a solvent extractant comprising at least one C5-C8 alkanol, optionally in admixture with at least one alkane, to form a first mixture, and separating the first mixture into a first solvent phase and a first aqueous phase. The first solvent phase comprises a majority (more than 50 wt %) of the solvent extractant and a majority of the glycerol that was present in the aqueous feed composition. The weight ratio in the first solvent phase of glycerol to a contaminant present is greater than the weight ratio of glycerol to the contaminant in the aqueous feed composition. The first aqueous phase comprises a majority of the water from the aqueous feed composition and at least some of the contaminant from the aqueous feed composition.

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South Croydon, United Kingdom

John Kerr