IPC분류정보
국가/구분 |
United States(US) Patent
등록
|
국제특허분류(IPC7판) |
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출원번호 |
US-0533868
(2009-07-31)
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등록번호 |
US-8110698
(2012-02-07)
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발명자
/ 주소 |
|
출원인 / 주소 |
|
인용정보 |
피인용 횟수 :
2 인용 특허 :
24 |
초록
▼
Processes for producing diaryl carbonates are disclosed, where such processes may provide for the production of diaryl carbonates from green house gases, such as carbon dioxide. The processes disclosed advantageously integrate diethyl carbonate and diaryl carbonate production, eliminating the need f
Processes for producing diaryl carbonates are disclosed, where such processes may provide for the production of diaryl carbonates from green house gases, such as carbon dioxide. The processes disclosed advantageously integrate diethyl carbonate and diaryl carbonate production, eliminating the need for solvent-based extractive distillation, as is commonly required when producing diaryl carbonates from dimethyl carbonate, providing for the integration of separation equipment and raw material usage, and reducing the operating and capital requirements for such processes. In some embodiments, processes disclosed herein may be operated essentially closed-loop with respect to ethanol usage, for example.
대표청구항
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1. A process for production of diaryl carbonate, comprising: reacting an epoxide and carbon dioxide in a first reaction zone to form first reaction product comprising a cyclic carbonate;transesterifying the cyclic carbonate with ethanol in the presence of a first transesterification catalyst in a se
1. A process for production of diaryl carbonate, comprising: reacting an epoxide and carbon dioxide in a first reaction zone to form first reaction product comprising a cyclic carbonate;transesterifying the cyclic carbonate with ethanol in the presence of a first transesterification catalyst in a second reaction zone to form a second reaction product comprising diethyl carbonate and glycol;separating the second reaction product to recover a first diethyl carbonate fraction and a first glycol fraction;transesterifying at least a portion of the first diethyl carbonate fraction with an aryl hydroxy compound in the presence of a second transesterification catalyst in a third reaction zone to form a third reaction product comprising ethyl aryl carbonate and ethanol;separating the third reaction product to recover an ethyl aryl carbonate fraction and a first ethanol fraction;disproportionating at least a portion of the ethyl aryl carbonate fraction in the presence of a disproportionation catalyst in a fourth reaction zone to form a fourth reaction product comprising diaryl carbonate and diethyl carbonate;separating the fourth reaction product to recover a diaryl carbonate fraction and a second diethyl carbonate fraction;recycling at least a portion of the first ethanol fraction to the second reaction zone; andrecycling at least a portion of the second diethyl carbonate fraction to the third reaction zone. 2. The process of claim 1, further comprising dehydrating at least a portion of the first glycol fraction to form an epoxide and water;separating the water from the epoxide;recycling at least a portion of the epoxide to the first reaction zone. 3. The process of claim 1, wherein the first transesterification catalyst and the second transesterification catalysts each independently comprise at least one of a solid transesterification catalyst, a soluble organometallic compound, and combinations thereof. 4. The process of claim 3, wherein the first transesterification catalyst comprises a solid transesterification catalyst, the process further comprising feeding a trace amount of soluble organometallic compound to the second reaction zone. 5. The process of claim 4, wherein the soluble organometallic compound is fed at a rate in the range of 1 ppm to 200 ppm, based on a total weight of reactants. 6. The process of claim 3, wherein the second transesterification catalyst comprises a solid transesterification catalyst, the process further comprising feeding a trace amount of soluble organometallic compound to the third reaction zone. 7. The process of claim 6, wherein the soluble organometallic compound is fed at a rate in the range of 1 ppm to 200 ppm, based on a total weight of reactants. 8. The process of claim 7, further comprising maintaining a concentration of water in the third reaction zone in a range from 1 ppm to 600 ppm by weight. 9. The process of claim 3, wherein the solid transesterification catalyst and the soluble organometallic compound each independently comprise at least one Group II to Group VI element. 10. The process of claim 1: wherein the second reaction zone comprises a catalytic distillation reactor system for concurrently transesterifying the cyclic carbonate with ethanol and separating the second reaction product;wherein the third reaction zone comprises a catalytic distillation reactor system for concurrently transesterifying the diethyl carbonate with the aryl hydroxyl compound and separating the third reaction product;wherein the fourth reaction zone comprises a catalytic distillation reactor system for concurrently disproportionating the ethyl aryl carbonate and separating the fourth reaction product;wherein the first diethyl carbonate fraction comprises diethyl carbonate and ethanol, the process further comprising: separating the first diethyl carbonate fraction to recover a third diethyl carbonate fraction and a second ethanol fraction; andrecycling the second ethanol fraction to the second reaction zone;wherein the first glycol fraction comprises glycol and cyclic carbonate, the process further comprising: separating the first glycol fraction to recover a second glycol fraction and a cyclic carbonate fraction; andrecycling the cyclic carbonate fraction to the second reaction zone;wherein the diaryl carbonate fraction comprises diaryl carbonate, ethyl aryl carbonate, aryl hydroxyl compound, and reaction byproducts, the process further comprising: separating the diaryl carbonate fraction to recover a diaryl carbonate product fraction, a reaction byproduct fraction comprising compounds heavier than the diaryl carbonate, and at least one recycle fraction comprising at least one of the ethyl aryl carbonate and the aryl hydroxyl compound; andrecycling the at least one recycle to the fourth reaction zone; andwherein the first ethanol fraction comprises ethanol and diethyl carbonate, the process further comprising: separating the first ethanol fraction to recover a third ethanol fraction and a fourth diethyl carbonate fraction;recycling the fourth diethyl carbonate fraction to the third reaction zone; andfeeding at least a portion of the third ethanol fraction as the at least a portion of the first ethanol fraction recycled to the second reaction zone. 11. The process of claim 10, further comprising dehydrating at least a portion of the second glycol fraction to form an epoxide and water;separating the water from the epoxide;recycling at least a portion of the epoxide to the first reaction zone. 12. The process of claim 1, wherein at least one of the second, third, and fourth reaction zones comprise a catalytic distillation reactor system, and wherein at least one catalytic distillation reactor system comprises an internal heating exchange device promoting vapor-liquid separation and directing of vapor-liquid traffic within the catalytic distillation reactor system. 13. The process of claim 1, wherein at least one of the second reaction zone, the third reaction zone, and the fourth reaction zone comprises two or more transesterification catalysts arranged to promote catalyst longevity and limit catalyst fouling. 14. The process of claim 13, wherein the two or more transesterification catalysts comprises at least one of different active metal components, different support compositions, and different support properties. 15. The process of claim 1, wherein the process is operated essentially closed loop with respect to ethanol.
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