Processes for converting ethane into ethylene include the steps of subjecting a water feed stream to electrolysis to form O.sub.2 and H.sub.2, subjecting a mixture of ethane and O.sub.2 to oxidative dehydrogenation to form a reaction product containing ethylene, acetic acid, water, and CO/CO.sub.2, separating the reaction product into an ethylene product stream, an acetic acid product stream, a water product stream, and a gas stream containing CO/CO.sub.2, and introducing the water product stream into the water feed stream for electrolysis. The ethylene product stream can be contacted with a suitable polymerization or oligomerization catalyst composition to produce ethylene polymers or ethylene oligomers.

Processes for converting ethane into ethylene include the steps of subjecting a water feed stream to electrolysis to form O.sub.2 and H.sub.2, subjecting a mixture of ethane and O.sub.2 to oxidative dehydrogenation to form a reaction product containing ethylene, acetic acid, water, and CO/CO.sub.2, separating the reaction product into an ethylene product stream, an acetic acid product stream, a water product stream, and a gas stream containing CO/CO.sub.2, and introducing the water product stream into the water feed stream for electrolysis. The ethylene product stream can be contacted with a suitable polymerization or oligomerization catalyst composition to produce ethylene polymers or ethylene oligomers.

Provided is a method for producing isobutylene with a high selectivity by a dehydration reaction of isobutanol. There are provided a method for producing isobutylene by dehydration of isobutanol, in which the dehydration of isobutanol is performed in a state where at least one of an organic acid and an organic acid ester is present in a reaction system, and methods for producing methacrylic acid and methyl methacrylate from the obtained isobutylene.

Provided is a method for producing isobutylene with a high selectivity by a dehydration reaction of isobutanol. There are provided a method for producing isobutylene by dehydration of isobutanol, in which the dehydration of isobutanol is performed in a state where at least one of an organic acid and an organic acid ester is present in a reaction system, and methods for producing methacrylic acid and methyl methacrylate from the obtained isobutylene.

The present invention relates to a plant for performance of heterogeneously catalyzed gas phase reactions. The plant entails a reactor, at least one line leading into the reactor for introduction of reactants into the reactor, at least one first feed for providing at least one first reactant A, which leads into the line, at least one second feed for providing at least one second reactant B, which leads into the line, at least one third feed for providing a cycle gas G, which leads into the line, a temperature control unit which is disposed in the line upstream of the reactor and is for controlling the temperature of the first reactant A and/or second reactant B and/or cycle gas G prior to entry into the reactor and at least one outlet for products, by-products and/or unreacted reactants from the gas phase reaction.

There are provided methods for the valorization of carbohydrates. The methods comprise reacting a fluid comprising at least one carbohydrate with at least one metal catalyst or at least one metal catalytic system in a fluidized bed reactor so as to obtain at least one organic acid or a derivative thereof.

There are provided methods for the valorization of carbohydrates. The methods comprise reacting a fluid comprising at least one carbohydrate with at least one metal catalyst or at least one metal catalytic system in a fluidized bed reactor so as to obtain at least one organic acid or a derivative thereof.

The invention is related to a process for production of acrylic acid comprising the following steps: a) preparation of a product gas mixture by a catalytic gas-phase oxidation of at least one C.sub.3 precursor compound to acrylic acid, wherein acrylic acid is formed as a main product of the catalytic gas-phase oxidation and glyoxal is formed as a by-product and the product gas mixture comprises acrylic acid and glyoxal, b) cooling of the product gas mixture, c) contacting the product gas mixture in countercourrent with an absorbent, wherein an absorbate A, comprising the absorbent and absorbed acrylic acid, is formed, d) introducing a feed stream F (2) comprising at least part of the absorbate A into a rectification column comprising a rectifying section and a stripping section, e) enriching the absorbent in the stripping section and enriching acrylic acid in the rectifying section, f) withdrawing a stream C of crude acrylic acid comprising at least 90% by weight of acrylic acid out of the rectifying section as a side stream,
wherein step c) is carried out in an absorption column (12) comprising at least two cooling loops, a first cooling loop (14), wherein a high boiler fraction of the product gas mixture is condensed and a second cooling loop (16), wherein a low boiler fraction of the product gas mixture is condensed,
wherein a portion of the absorbate A, which comprises the feed stream F (2), is removed from the absorption column (12) at a side take-off (20), the side take-off (20) being located at the first cooling loop (14) or at a height of the absorption column (12) between the first cooling loop (14) and the second cooling loop (16)
and wherein a temperature Tc of the absorbate A in the second cooling loop is at least 56 C.