Tate & Lyle Technology Limited

Tate & Lyle Ingredients Americas LLC

European Sugar Holdings S.a.r.l.

T&l Sugars Limited

Globalfoundries Inc.

Tate & Lyle Ingredidents Americas, Inc.

A E Staley Manufacturing Company

Anthony Baiada

Robert P Jansen

Avraham Baniel

Asher Vitner

Avraham M Baniel

John Kerr

Duane Leinhos

Gordon Walker

James Edwin Wiley, Jr

Tommaso Bartalucci

Tim Windebank

Matthew Shue

Sebastien Camborieux

Carlo Maffezzoni

Robert Jansen

James Edwin Wiley

Asher Vittner

Carlo Maffezoni

The invention relates to a process for the removal of contaminants from a liquor, the process comprising: introducing a metal or ammonium hydroxide into the liquor; introducing the liquor into a reaction vessel; bubbling a carbon dioxide gas comprising at least 25% carbon dioxide through the liquor within the reaction vessel; and separating the precipitate formed by the carbonatation of the metal hydroxide from the liquor, the precipitate comprising at least some of the contaminants from the liquor; wherein, on average, the liquor is resident within the reaction vessel for a period of no more than about 60 minutes. The invention also relates to a process for the removal of contaminants from a liquor, the process comprising: introducing a metal or ammonium hydroxide into the liquor and bubbling a carbon dioxide gas comprising at least 25% carbon dioxide through the liquor to form a precipitate by carbonatation in a period of no more than about 60 minutes. The carbonatation processes may be included in sugar refining or water softening and/or decontamination processes. A use of a carbon dioxide gas comprising at least 25% carbon dioxide in a carbonatation process for removing contaminants from a hydroxide-treated liquor is also provided, wherein the process forms a precipitate in a period of no more than about 60 minutes.

Process including a carbonation step

A process for the removal of contaminants from a liquor, including two or more of carbonatation, phosphatation and sulphitation of the liquor to form a precipitate having at least some of the contaminants from the liquor, and separating the precipitate from the liquor. The processes may be included in sugar refining or water decontamination processes.

Purification processes

The present invention relates to a process and, more specifically, to a process for the removal of components from a starting material. Optionally, the process is used for the removal of contaminants from ion exchange regenerant material.

Removal of components from a starting material

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

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

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

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.

Process for purification of glycerol

Disclosed herein are processes for the recovery of 1,3-propanediol from an aqueous feed stream. The present invention involves contacting an aqueous feed stream that comprises water, 1,3-propanediol, and at least one contaminant with at least one solvent extractant to form a mixture. The mixture is separated into a first phase and a second phase. The second phase comprises a majority of the water from the aqueous feed stream. The first phase comprises solvent extractant and at least some of the 1,3-propanediol that was present in the aqueous feed stream. The weight ratio in the first phase of 1,3-propanediol to any one contaminant present is greater than the weight ratio of 1,3-propanediol to the same contaminant in the aqueous feed stream prior to the aqueous feed stream being contacted with the solvent extractant. The first phase can be removed from the separated second phase in order to recover the 1,3-propanediol.

Growing community of inventors

Dagenham, United Kingdom

Anthony Baiada