A process of and apparatus for dehydrating an alcohol/water mixture may include pressurizing the mixture to at least 40 psig, heating the pressurized mixture to a temperature of at least 170° F., passing the heated and pressurized mixture through at least one Zeolite separator to produce separate streams of water and pressurized and heated dehydrated alcohol, and using the pressurized and heated dehydrated alcohol to at least in part heat pressurized mixture and to cool the pressurized and heated dehydrated alcohol. At least some implementations may include cooling the pressurized and heated dehydrated alcohol to a temperature below its boiling point at atmospheric pressure. At least some implementations may include applying a vacuum to the water stream side of the Zeolite separator. At least some implementations may include cooling the stream of water to a temperature of less than about 200° F.

Rapid evaporation of water for desalination and dewatering using nanobubbles and micro-droplets is disclosed. Warm nanobubbles of air are injected into seawater or another water source to be treated, and the normal stasis of the nanobubbles is disrupted with ultrasonic energy. The nanobubbles implode and violently recombine into microbubbles. Energized by the effects of the nanobubble state change, these energetic, relatively high surface area microbubbles bubbles quickly rise to the surface of the water, creating an aerosol of micro-water droplets above the surface that is drawn into a dry, warm stream of air and rapidly evaporates, precipitating out salt crystals. The air is then cooled with a chiller, condensing the moisture in the air into fresh water.

A method for synthesizing a supported molecular sieve membrane by microwaves includes the steps of aging, heating and synthesizing. The aging step is to make a support in contact with a synthetic liquid at 25° C. to 70° C. for 10 hours to 24 hours; the heating step is to raise a temperature of an aged system from an aging temperature to a synthesis temperature within 1 minute to 10 minutes; and the synthesizing step is to synthesize at 80° C. to 120° C. for 2 minutes to 15 minutes. The steps of heating and synthesizing are powered by microwaves.

A power generation system, includes: a fuel cell that includes a negative electrode and a positive electrode and is configured to generate electric power by chemical reaction between hydrogen and oxygen; a separator that includes an oxygen-permselective separation membrane and is configured to obtain permeated gas and non-permeated gas from mixed gas; and a positive electrode gas supply passage through which the mixed gas is supplied to the separator and the obtained permeated gas is supplied to the positive electrode. The separation membrane includes a porous support layer and a separation functional layer provided on the porous support layer. The separation functional layer contains at least one kind of chemical compound selected from the group consisting of polyamide, graphene, MOF (Metal Organic Framework), and COF (Covalent Organic Framework).

A power generation system, includes: a fuel cell that includes a negative electrode and a positive electrode and is configured to generate electric power by chemical reaction between hydrogen and oxygen; a separator that includes a hydrogen-permselective separation membrane and is configured to obtain permeated gas and non-permeated gas from mixed gas; and a negative electrode gas supply passage configured to supply the mixed gas containing hydrogen to the separator and supply the permeated gas obtained by the separator to the negative electrode. The separation membrane includes a porous support layer and a separation functional layer provided on the porous support layer. The separation functional layer contains at least one kind of chemical compound selected from the group consisting of polyamide, graphene, MOF (Metal Organic Framework), and COF (Covalent Organic Framework).

A power generation system, includes: a fuel cell that includes a negative electrode supplied with hydrogen-containing gas and a positive electrode supplied with oxygen-containing gas, and is configured to generate electric power by chemical reaction between hydrogen and oxygen; a separator that includes a hydrogen-permselective separation membrane and is configured to obtain permeated gas and non-permeated gas from mixed gas; and a circulating passage through which negative electrode-side exhaust gas of the fuel cell is sent to the separator, and through which the permeated gas is supplied to the negative electrode. The separation membrane includes a porous support layer and a separation functional layer provided on the porous support layer. The separation functional layer contains at least one kind of chemical compound selected from the group consisting of polyamide, graphene, MOF (Metal Organic Framework), and COF (Covalent Organic Framework).

The disclosure relates to a device for fermentation integrated with separation and purification of acetone, butanol, and ethanol (ABE) or butanol alone, including a medium tank (1), used for supplying a medium into a bioreactor; a bioreactor (2), connected with the medium tank (1), used for fermentation; a gas distributor (9), used for supplying gas bubble to the fermentation broth; a membrane separation unit (4), with gas communication to the bioreactor (2), used for receiving a gas with ABE or butanol from the bioreactor and separating ABE or butanol; a condensation unit (5), used for recovering ABE or butanol; a vacuum manometer (6) and a vacuum pump (8), used for supplying a force for driving ABE or butanol in a vapor form; and product tank (7), used for receiving a product.

A peak intensity of a (002) plane is greater than or equal to 0.5 times a peak intensity of a (100) plane in an X-ray diffraction pattern obtained by irradiation of X-rays to a membrane surface of the ERI membrane.

Disclosed are a MWW/DDR type gas separation membrane comprising at least one MWW type zeolite and at least one DDR type zeolite and a method for preparing the same. One of the MWW type zeolite and the DDR type zeolite is disposed on the other thereof, wherein at least one of the MWW type zeolite and the DDR type zeolite is epitaxially grown. In the gas separation membrane, the DDR type zeolite is epitaxially grown from the MWW type zeolite, or the MWW type zeolite is epitaxially grown from the DDR type zeolite. Thus, the MWW/DDR type gas separation membrane is synthesized using a structural continuity of the MWW type zeolite and the DDR type zeolite. Thus, the gas separation membrane has excellent separation efficiency.

Provided is a separation membrane that is suitable for use in separating one or more hydrocarbons from a hydrocarbon mixture. More specifically, the separation membrane includes a porous support for which acid content is not substantially detected by ammonia temperature programmed desorption in a temperature range of higher than 450° C. and not higher than 600° C. and a porous separation layer containing a zeolite that is disposed on the porous support.