Disclosed is an electrocatalytic degradation device for organic wastewater, which includes an electrocatalytic oxidation reactor, a spray tower and a drying tower. The electrocatalytic oxidation reactor is provided with a hydroxyl generator, a catalyst filler and a box body. The box body of the electrocatalytic oxidation reactor is provided with a gas gathering device connected with the spray tower. An upper gas outlet of the spray tower is connected with the drying tower. The disclosure combines the electrooxidation reaction with the catalytic reaction to improve the electrooxidation efficiency of the electrocatalytic oxidation reactor and efficiently degrade the high salt high organic wastewater. The decomposed by-products are effectively utilized. The generated hydrogen is collected by the gas gathering device and enters the spray tower. The CO.sub.2 gas is absorbed after treatment. The CO.sub.2-removed gas passes through the drying tower to absorb moisture to obtain pure hydrogen.

An H.sub.2-rich fuel gas production plant comprising a syngas production unit can be advantageously integrated with an olefins production plant comprising a steam cracker in at least one of the following: (i) fuel gas supply and consumption; (ii) feed supply and consumption; and (iii) steam supply and consumption, to achieve considerable savings in capital and operational costs, enhanced energy efficiency, and reduced CO.sub.2 emissions, compared to operating the plants separately.

A polymer blend membrane includes a polyether-based copolymer and a polyether polymerized in situ and has high permeability and high selectivity for carbon dioxide. In the polymer blend membrane, the free volume of the polyether-based copolymer is greatly increased, and the adsorption capacity for carbon dioxide is enhanced. Thus, it can have excellent mechanical properties and excellent permeability and selectivity for carbon dioxide.

Hydrogen purification devices and their components are disclosed. In some embodiments, the devices may include at least one foil-microscreen assembly disposed between and secured to first and second end frames. The at least one foil-microscreen assembly may include at least one hydrogen-selective membrane and at least one microscreen structure including a non-porous planar sheet having a plurality of apertures forming a plurality of fluid passages. The planar sheet may include generally opposed planar surfaces configured to provide support to the permeate side. The plurality of fluid passages may extend between the opposed surfaces. The at least one hydrogen-selective membrane may be metallurgically bonded to the at least one microscreen structure. In some embodiments, the devices may include a permeate frame having at least one membrane support structure that spans at least a substantial portion of an open region and that is configured to support at least one foil-microscreen assembly.

The present disclosure relates to systems and methods useful for power production. In particular, a power production cycle utilizing CO.sub.2 as a working fluid may be configured for simultaneous hydrogen production. Beneficially, substantially all carbon arising from combustion in power production and hydrogen production is captured in the form of carbon dioxide. Further, produced hydrogen (optionally mixed with nitrogen received from an air separation unit) can be input as fuel in a gas turbine combined cycle unit for additional power production therein without any atmospheric CO.sub.2 discharge.

Provided are composite articles having a membrane and a porous substrate, where the porous substrate has the membrane disposed thereon. The membrane has two layers, where the first layer has the second layer disposed thereon, and each layer has a plurality of polymer chains with a plurality of silicon-oxygen groups and a plurality of silicon-carbon groups. The first layer has a silicon to oxygen ratio of about 4:1 to about 1:1.25 and a silicon to carbon ratio of about 1:2 to about 1:10, and the second layer has a silicon to oxygen ratio of about 1:1 to about 1:2 and a silicon to carbon ratio of about 2:1 to about 10:1. At least a portion of the polymer chains of the second layer am crosslinked. The composite articles may be used in gas separation methods. Also provided are methods of making the composite articles and devices utilizing the composite articles.

The present invention relates to an intensified 5-bed and 6-bed PSA process cycles features, as well as fast rate adsorbents that enable the intensified PSA system to meet cost and performance target are identified. The proposed capital efficient H.sub.2PSA system offers opportunity to reduce PSA capital expenditure by ten percent (10%).

A system and method for producing hydrogen from hydrocarbon and steam, including a membrane reformer with multiple membrane reactors each having a tubular membrane. The bore of the tubular membrane is the permeate side for the hydrogen. The region external to the tubular membrane is the retentate side for carbon dioxide. A sweep gas flows through the bore to displace hydrogen in a direction countercurrent to flow of hydrocarbon and steam in the region external to the tubular membrane. The method includes discharging hydrogen as permeate with the sweep gas from the bore, and discharging carbon dioxide in the region external to the tubular membrane as retentate from the membrane reactor.

Provided are a porous substrate structure and a manufacturing method thereof. The porous substrate structure includes a substrate, an anodic aluminum oxide layer and a double metal oxide layer. The substrate has a plurality of pores. The anodic aluminum oxide layer is disposed on the substrate. The double metal oxide layer is disposed on the anodic aluminum oxide layer.

The invention relates to a process and apparatus for separation of gas mixtures with reduced maintenance costs. The process and the apparatus consist of a feed stream separation stage (1), and a retentate separation stage (2), of which both are membrane separation stages, wherein the first retentate stream (7) is heated to temperature higher than the temperature of the feed stream (5), before it is introduced to the retentate separation stage (2), and the total capacity of the membranes used in the retentate separation stage (2) is higher than the total capacity of the membranes used in the feed stream stage (1).