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Process for converting a reactor from base-catalyzed polyol production to dmc-catalyzed polyol production

A DMC catalyst and reactor technology, applied in the preparation of organic compounds, chemical instruments and methods, organic chemistry, etc., can solve the problem of reducing the catalytic activity of DMC

Active Publication Date: 2021-02-12
COVESTRO LLC
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  • Summary
  • Abstract
  • Description
  • Claims
  • Application Information

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Problems solved by technology

The reactor must also be thoroughly dried to remove any traces of solvent and / or water remaining in the reactor, as these trace contaminants can reduce the activity of the DMC-catalyzed reaction and lead to unwanted volatiles in the polyether product. Volatile Organic Compounds (VOCs)

Method used

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  • Process for converting a reactor from base-catalyzed polyol production to dmc-catalyzed polyol production
  • Process for converting a reactor from base-catalyzed polyol production to dmc-catalyzed polyol production
  • Process for converting a reactor from base-catalyzed polyol production to dmc-catalyzed polyol production

Examples

Experimental program
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Effect test

Embodiment

[0024] Preparation of polyether polyols

[0025] The base-catalyzed polyol preparation reaction and the resulting base-catalyzed product mixture were simulated by combining a polyoxypropylene triol with a hydroxyl number of 56 mg KOH / g and a total polyoxypropylene triol and potassium hydroxide-based A 5 gallon mixture of 0.33% by weight potassium hydroxide ("base catalyzed product simulant") was charged to an 8 gallon continuously stirred tank reactor. The base-catalyzed product simulant was stirred and heated in the reactor at a temperature of 100°C for 60 minutes. The unneutralized base-catalyzed product simulant was then vented from the reactor while purging with nitrogen for 20 minutes at 60°C.

[0026] The starter mixture was charged to the vented reactor in an amount sufficient to provide a build ratio of 8.5 (2414 grams). After the base-catalyzed product simulant is drained from the reactor, the reactor is not washed, rinsed, or otherwise treated to remove residual ...

Embodiment 31

[0052] Example 23 was repeated (90 ppm catalyst, 500 ppm phosphoric acid, 140°C reaction temperature, 4% PO added for activation), except that the initiator mixture was added to the reactor instead of washing the reactor, Under conditions where the base-catalyzed product simulant was flushed or otherwise treated to remove its residue after it was withdrawn from the reactor, 0.9% of the base-catalyzed product simulant was added to the starter mixture (based on starting 177 grams based on the total weight of the reagent mixture and the added base-catalyzed product simulant). A starter mixture containing 0.9% base-catalyzed product simulant was added to a clean reactor free of residual base-catalyzed product simulant from previous base-catalyzed polyol product simulations. The activation time of the DMC catalyst was 5 minutes and the reactor was maintained at a pressure typical for DMC catalyzed polymerization with a peak pressure of 13.9 psia. The hydroxyl value of the final pr...

Embodiment 32-34

[0055] Using a "base-catalyzed product simulant" similar to that described above, the initiator mixture was charged to the vented reactor in an amount sufficient to provide a build ratio of 4 (4968 grams). After the base-catalyzed product simulant is drained from the reactor, the reactor is not washed, flushed, or otherwise treated to remove residual base-catalyzed product simulant. The starter mixture comprises a polyether polyol starter (polyoxypropylene triol with a hydroxyl value of 233-243 mg KOH / g), 30-120 ppm of hexacyanocobalt based on the total weight of the final product A zinc acid DMC catalyst, and 0 to 1000 ppm of phosphoric acid based on the total weight of the starter mixture. The starter mixture was heated to 130° C. in the reactor while purging with nitrogen under vacuum for 30 minutes. The reactor is then heated to a reaction temperature of 130-150°C, the reactor is sealed under vacuum, and 4 to 10% of propylene oxide (based on the total weight of the initia...

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Abstract

The present invention describes a process for converting a reactor from base-catalyzed polyol production to double metal cyanide (DMC)-catalyzed polyol production. The process includes withdrawing the base catalyzed and unneutralized product mixture from the reactor and adding the acidified polyether polyol starter and DMC catalyst mixture to the reactor. The DMC catalyzed polyol production reaction can then be carried out in the reactor without intermediate washing or flushing of the reactor and without catalyst deactivation due to the presence of bases or basic species.

Description

Background technique [0001] Polyether polyols are used in the polyurethane industry to prepare polyurethane products such as coatings, sealants, adhesives, elastomers and foams. The industrial preparation of polyether polyols usually involves two alternative reactions - base-catalyzed alkoxylation of starter molecules or double metal cyanide (DMC)-catalyzed alkoxylation of starter molecules . Bases and DMC catalysts used to make polyether polyols are not compatible because base catalysts deactivate the DMC catalyst. Therefore, base-catalyzed polyol production and DMC-catalyzed polyol production generally require separate and dedicated production reactors to avoid cross-contamination of basic compounds in the DMC-catalyzed reaction mixture. This increases the production cost of the polyether polyol and underutilizes the reactor. When converting base-catalyzed and DMC-catalyzed technologies in the same reactor, an option is to wash the reactor with polyols, solvents, water an...

Claims

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Application Information

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Patent Type & Authority Patents(China)
IPC IPC(8): C08G65/26
CPCC08G65/2663C08G65/2669C07C41/26
Inventor P·尤思J·R·瑞斯S·贝利
Owner COVESTRO LLC
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