Abstract: A method for the production of syngas from methanol feedstock is disclosed. The methanol feed (110) is supplied to a partial oxidation reactor (112) with oxygen (114) and optionally steam (116) to yield a mixed stream (118) of hydrogen, carbon monoxide, and carbon dioxide. The carbon dioxide (122) is separated out and the hydrogen and carbon monoxide mixture (124) is fed to a cold box (126) where it is separated into hydrogen-rich and carbon monoxide-rich streams (130, 128). The separated carbon dioxide (122) can be recycled back to the partial oxidation reactor (112) as a temperature moderator if desired. The carbon monoxide-rich stream (128) can be reacted with methanol (134) in an acetic acid synthesis unit (132) by a conventional process to produce acetic acid (136) or an acetic acid precursor. Optionally, an ammonia synthesis unit (144) and/or vinyl acetate monomer synthesis unit (156) can be integrated into the plant.

Abstract: A method for the production of syngas from methanol feedstock is disclosed. The methanol feed (110) is supplied to a partial oxidation reactor (112) with oxygen (114) and optionally steam (116) to yield a mixed stream (118) of hydrogen, carbon monoxide, and carbon dioxide. The carbon dioxide (122) is separated out and the hydrogen and carbon monoxide mixture (124) is fed to a cold box (126) where it is separated into hydrogen-rich and carbon monoxide-rich streams (130, 128). The separated carbon dioxide (122) can be recycled back to the partial oxidation reactor (112) as a temperature moderator if desired. The carbon monoxide-rich stream (128) can be reacted with methanol (134) in an acetic acid synthesis unit (132) by a conventional process to produce acetic acid (136) or an acetic acid precursor. Optionally, an ammonia synthesis unit (144) and/or vinyl acetate monomer synthesis unit (156) can be integrated into the plant.

Abstract: A method for the production of syngas from methanol feedstock is disclosed. The methanol feed (110) is supplied to a partial oxidation reactor (112) with oxygen (114) and optionally steam (116) to yield a mixed stream (118) of hydrogen, carbon monoxide, and carbon dioxide. The carbon dioxide (122) is separated out and the hydrogen and carbon monoxide mixture (124) is fed to a cold box (126) where it is separated into hydrogen-rich and carbon monoxide-rich streams (130, 128). The separated carbon dioxide (122) can be recycled back to the partial oxidation reactor (112) as a temperature moderator if desired. The carbon monoxide-rich stream (128) can be reacted with methanol (134) in an acetic acid synthesis unit (132) by a conventional process to produce acetic acid (136) or an acetic acid precursor. Optionally, an ammonia synthesis unit (144) and/or vinyl acetate monomer synthesis unit (156) can be integrated into the plant.

Abstract: An integrated process for making methanol, acetic acid, and a product from an associated process is disclosed. Syngas (120) is produced by combined steam reforming (109) and autothermal reforming (118) of natural gas (102) where a portion (112) of the natural gas bypasses the steam reformer (109) and is blended with the steam reformer effluent for supply to the autothermal reformer (ATR) (118) with CO2 recycle (110). A portion of the syngas is fed to CO2 removal (122) to obtain the recycle CO2 and cold box (130) to obtain a hydrogen stream (131) and a CO stream (135). The remaining syngas, hydrogen stream (131) and CO2 from an associated process are fed to methanol synthesis (140), which produces methanol and a purge stream (124) supplied to the CO2 removal unit. The methanol is supplied to an acetic acid unit (13)6 with the CO (135) to make acetic acid, which in turn is supplied to a VAM synthesis unit (148).

Abstract: An integrated process for making methanol, acetic acid, and a product from an associated process is disclosed. Syngas (120) is produced by combined steam reforming (109) and autothermal reforming (118) of natural gas (102) where a portion (112) of the natural gas bypasses the steam reformer (109) and is blended with the steam reformer effluent for supply to the autothermal reformer (ATR) (118) with CO2 recycle (110). A portion of the syngas is fed to CO2 removal (122) to obtain the recycle CO2 and cold box (130) to obtain a hydrogen stream (131) and a CO stream (135). The remaining syngas, hydrogen stream (131) and CO2 from an associated process are fed to methanol synthesis (140), which produces methanol and a purge stream (124) supplied to the CO2 removal unit. The methanol is supplied to an acetic acid unit (13)6 with the CO (135) to make acetic acid, which in turn is supplied to a VAM synthesis unit (148).

Abstract: An integrated large capacity, single-train process for making 1,00020,000 MTPD methanol and 3006,000 MTPD acetic acid is disclosed. Syngas 120 is produced by autothermal reforming 118 of natural gas 102 where the feed 112 of the natural gas is supplied with oxygen and CO2 recycle 110 to the autothermal reformer (ATR) 118. A portion (5-50%) of the syngas is fed to CO2 removal 122 to obtain the recycle CO2 and cold box 130 to obtain a hydrogen stream 131 and a CO stream 135. The 50-95% remaining syngas, hydrogen stream 131 and optionally any CO2 from an associated process are fed to methanol synthesis 140, which produces the methanol. The methanol is supplied to an acetic acid unit 136 with the CO 135 to make the acetic acid, which in turn can be supplied to a VAM synthesis unit 148. Oxygen for the ATR and any VAM synthesis can be supplied by a single common air separation unit 116, and utilities such as steam generation can further integrate the process.

Abstract: The retrofitting of an existing methanol or methanol/ammonia plant to make acetic acid is disclosed. The existing plant has a reformer (10) to which natural gas or another hydrocarbon and steam (water) are fed. Syngas is formed in the reformer (10). All or part of the syngas is process to separate out carbon dioxide (24), carbon monoxide (30) and hydrogen (32), and the separated carbon dioxide (24) is the existing to the existing methanol synthesis loop (12) for methanol synthesis, or back into the feed to the reformer (10) to enhance carbon monoxide formation in the syngas (18). Any remaining syngas (38) not fed to the carbon dioxide separator (22) can be converted to methanol in the existing methanol synthesis loop (12) along with carbon dioxide (24) from the separator (22) and/or imported carbon dioxide (25), and hydrogen (35) from the separator (28). The separated carbon monoxide (30) is then reacted with the methanol (36) to produce acetic acid (40) or an acetic acid precursor by a conventional process.

Abstract: The retrofitting of an existing methanol or methanol/ammonia plant to make acetic acid is disclosed. The plant is retrofitted to feed carbon dioxide into a reformer to which natural gas and steam (water) are fed. Syngas is formed in the reformer wherein both the natural gas and the carbon dioxide are reformed to produce syngas with a large proportion of carbon monoxide relative to reforming without added carbon dioxide. The syngas is split into a first part and a second part. The first syngas part is converted to methanol in a conventional methanol synthesis loop that is operated at about half of the design capacity of the original plant. The second syngas part is processed to separate out carbon dioxide and carbon monoxide, and the separated carbon dioxide is fed back into the feed to the reformer to enhance carbon monoxide formation. The separated carbon monoxide is then reacted with the methanol to produce acetic acid or an acetic acid precursor by a conventional process.

Abstract: The retrofitting of an existing methanol or methanol/ammonia plant to make acetic acid is disclosed. The plant is retrofitted to feed carbon dioxide into a reformer to which natural gas and steam (water) are fed. Syngas is formed in the reformer wherein both the natural gas and the carbon dioxide are reformed to produce syngas with a large proportion of carbon monoxide relative to reforming without added carbon dioxide. The syngas is split into a first part and a second part. The first syngas part is converted to methanol in a conventional methanol synthesis loop that is operated at about half of the design capacity of the original plant. The second syngas part is processed to separate out carbon dioxide and carbon monoxide, and the separated carbon dioxide is fed back into the feed to the reformer to enhance carbon monoxide formation. The separated carbon monoxide is then reacted with the methanol to produce acetic acid or an acetic acid precursor by a conventional process.