# US 10,308,590 B2 · Quality and color of ethanolamine product streams by reduced temperature at the triethanolamine column > Agents: this data is available as JSON from the patentgrep API and MCP server — see https://patentgrep.com/llms.txt - Number: US 10,308,590 B2 - Document ID: US10308590B2 - Status: Granted - Kind: B2 - Application number: 15/313,697 - Filed: 2015-05-27 - Published: 2017-05-04 - Granted: 2019-06-04 - Earliest claimed: 2014-05-30 - Assignees: Sabic Global Technologies B.V. - Applicants: Sabic Global Technologies B.V. - Inventors: Naeem Alhazmi - Web page: https://patentgrep.com/patent/US10308590B2 ## CPC - C07C 213/10: Separation; Purification; Stabilisation; Use of additives - B01D 3/007: {Energy recuperation; Heat pumps} - B01D 3/4283: {Bottom stream} - C07C 213/04: by reaction of ammonia or amines with olefin oxides or halohydrins - Y02P 20/10: Process efficiency - C07C: ACYCLIC OR CARBOCYCLIC COMPOUNDS - B01D: SEPARATION (separating solids from solids by wet methods B03B, B03D; by pneumatic jigs or tables B03B; by other dry methods B07; magnetic or electrostatic separation of solid materials from solid materials or fluids, separation by high-voltage electric fields B03C; centrifuges, vortex apparatus B04; presses per se for squeezing-out liquid from liquid-containing material B30B9/02; treatment of water C02F, e.g. softening by ion-exchange C02F1/42; {arrangements of air intake cleaners in gas turbine plants F02C7/05} ; arrangements or mounting of filters in air-conditioning, air-humidification or ventilation F24F13/28) - Y02P: CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS ## Abstract Systems and methods for producing a colorless triethanolamine product stream with a degree of purity of greater than or equal to 99% by weight from the triethanolamine distillation columns in a non-reactive distillation process. The desired triethanolamine product stream can be obtained by increasing the bottom stream flow rate at the diethanolamine column by 80 kilograms per hour, and reducing the triethanolamine product stream flow rate by 500 kilograms per hour. This process can result in a reduction of the temperature at the triethanolamine column by up to 23.5 degrees. The reduced temperature can result in a triethanolamine product stream with an APHA color of 0 to less than 50, for example, 0 to 40, for example, 0 to 30, for example 0 to 20, and for example, 0 to 10. ## Claims ### Claim 1 A method for producing triethanolamine from a non-reactive distillation column, comprising: mixing an ammonia solution comprising 30% to 40% by weight ammonia with ethylene oxide in a reactor to create a resultant product stream, wherein said resultant product stream comprises ethanolamines, unreacted ammonia and water; removing 30% to 50% by weight of the unreacted ammonia from the resultant product stream to create a stripped product stream; transferring the stripped product stream to a stage of a diethanolamine distillation column to create a resultant product stream; adjusting a bottom stream flow rate at the diethanolamine distillation column from 1% to 4% above a base value bottom stream flow rate; transferring the resultant product stream to a stage of a triethanolamine distillation column to create a triethanolamine product stream; adjusting a flow rate for the triethanolamine product stream by 10% to 20% below a base value flow rate; and recovering the triethanolamine product stream from the triethanolamine distillation column, wherein the triethanolamine product stream comprises triethanolamine with a degree of purity greater than or equal to 99% by weight and 0.1% to 0.6% by weight of diethanolamine; wherein the base value bottom stream flow rate is 3900 kilograms per hour to 4300 kilograms per hour and wherein the base value flow rate is 3000 kilograms per hour to 4000 kilograms per hour. ### Claim 2 (depends on 1) The method of claim 1, wherein the recovered triethanolamine product stream is colorless. ### Claim 3 (depends on 1) The method of claim 1, wherein the triethanolamine product stream has an APHA color number of 0 to 50. ### Claim 4 (depends on 3) The method of claim 3, wherein the triethanolamine product stream has an APHA color number of 0 to 40. ### Claim 5 (depends on 4) The method of claim 4, wherein the triethanolamine product stream has an APHA color number of 0 to 30. ### Claim 6 (depends on 5) The method of claim 5, wherein the triethanolamine product stream has an APHA color number of 0 to 20. ### Claim 7 (depends on 6) The method of claim 6, wherein the triethanolamine product stream has an APHA color number of 0 to 10. ### Claim 8 (depends on 1) The method of claim 1, further comprising receiving TEA heavy ends from an evaporator, wherein said TEA heavy ends comprise triethanolamine and traces of diethanolamine, and wherein said TEA heavy ends are transferred to the stage of the triethanolamine column. ### Claim 9 (depends on 1) The method of Claim 1, wherein the base value bottom stream flow rate is 4085 kilograms per hour. ### Claim 10 (depends on 1) The method of Claim 1, wherein the base value flow rate is 3450 kilograms per hour. ### Claim 11 (depends on 1) The method of claim 1, wherein the adjusted flow rate for the triethanolamine product stream and the adjusted bottom flow rate at the diethanolamine column results in a decrease in temperature at the triethanolamine column by 15° C. to 40° C. ### Claim 12 (depends on 11) The method of claim 11, wherein the decreased temperature is 23.5° C. ### Claim 13 (depends on 1) The method of claim 1, wherein the triethanolamine distillation column comprises a heat exchanger selected from a thermosiphon, a reboiler, or a combination comprising at least one of the foregoing. ### Claim 14 (depends on 1) The method of claim 1, wherein the ethanolamines are selected from monoethanolamine, diethanolamine, triethanolamine, or a combination comprising at least one of the foregoing. ### Claim 15 (depends on 1) The method of claim 1, wherein a purity of a triethanolamine product is 99.9%.