Abstract: The present disclosure provides an integrated process and a Cu/Zn-based catalyst system for synthesizing methanol from CO2 and generating electricity from hydrocarbon feedstock. The process includes steps of gasifying hydrocarbon feedstock into syngas by using oxygen and using the produced syngas as a fuel in a power generation unit, reusing a first part of an exhaust stream of the power generation unit as a reactant in the gasification unit. Using a second part of the said exhaust stream as a reactant for methanol synthesis in a methanol reactor, wherein, the second part is treated to separate CO2 and water, and CO2 is used as the reactant for methanol synthesis. Operating an electrolyzer during non-peak hours to produce hydrogen, wherein, a required stoichiometric ratio of the produced hydrogen is transferred into the methanol reactor for methanol synthesis, wherein, a Cu/Zn-based catalyst system is used for methanol synthesis through a direct hydrogenation reaction of CO2.

Abstract: A pressure vessel for storing fluid is disclosed. The pressure vessel includes a metallic liner comprising a cylindrical portion and a pair of ellipsoidal domes positioned at opposite ends of the cylindrical portion. Further, the pressure vessel includes a composite material wrapped over the cylindrical portion and the pair of ellipsoidal domes. The composite material is formed of a polymeric matrix reinforced with fibers, the composite material comprises of a combination of hoop layers and helical layers which are positioned in predetermined order with respect to each other. A hoop layer is wrapped over a cylindrical portion of the metallic liner of the pressure vessel and a helical layer is wrapped over both the cylindrical portion and the pair of ellipsoidal domes. The helical layer is wrapped on each of the pair of ellipsoidal domes in a manner that a helical angle is defined at an intersection between the cylindrical portion and the pair of ellipsoidal domes.

Abstract: The present disclosure relates to a modified gasification system (100) for producing syngas from waste materials having moisture content. The gasification system (100) has crossflow arrangement for circulation of gases across the solids present and has well-defined drying (120), pyrolysis (130) and gasification zones (140). A burner (150) of the gasification system (100) situated downstream of the pyrolysis zone (130) is configured to receive the pyrolysis product and a secondary oxidizer to produce a burner output gas and to supply the burner output gas to the pyrolysis zone (130) and gasification zone (140). The gasification zone (140) is additionally configured to receive a primary oxidizer gas and a tertiary oxidizer gas to aid gasification. The present disclosure overcomes limitation of the prior-arts and provides means of isolating the drying, pyrolysis, and gasification zones and eliminates tar formation during gasification. The gasification system (100) disclosed herein is a fully scalable equipment.

Abstract: The present disclosure provides an integrated process and a Cu/Zn-based catalyst system for synthesizing methanol from CO2 and generating electricity from hydrocarbon feedstock. The process includes steps of gasifying hydrocarbon feedstock into syngas by using oxygen and using the produced syngas as a fuel in a power generation unit, reusing a first part of an exhaust stream of the power generation unit as a reactant in the gasification unit. Using a second part of the said exhaust stream as a reactant for methanol synthesis in a methanol reactor, wherein, the second part is treated to separate CO2 and water, and CO2 is used as the reactant for methanol synthesis. Operating an electrolyzer during non-peak hours to produce hydrogen, wherein, a required stoichiometric ratio of the produced hydrogen is transferred into the methanol reactor for methanol synthesis, wherein, a Cu/Zn-based catalyst system is used for methanol synthesis through a direct hydrogenation reaction of CO2.

Abstract: The present invention depicts a method for one pot synthesis of dimethyl ether from syngas in a simple and economical manner. The process (500A, 500B, 600) has advantages of reducing the requirement of refrigeration and at the same time producing a ready to use product. The process (500A, 500B, 600) includes the steps of separating carbon dioxide from a first stream (512, 612) comprising syngas to produce a second stream (522, 622), reacting the second stream (522, 622) in the presence of a catalyst to produce a third stream (532, 632), cooling the third stream (532, 632) to a temperature in a range from 10° C. to 40° C. to produce a fourth stream (542, 642), and washing and conducting a phase separation of the fourth stream (542, 642) to produce a product comprising at least 10% by volume of dimethyl ether.

Abstract: The present disclosure discloses an electrode (300, 400, 500). The electrode (300, 400, 500) includes a substrate (302). Further, the electrode (300, 400, 500) includes a first conducting layer (304) disposed on the substrate (302). The first conducting layer (304) is formed of at least one of an Indium Tin Oxide (ITO) and a Fluorine-doped Tin Oxide (FTO). The electrode (300, 400, 500) also includes at least one semiconductor layer (308, 502) disposed on the first conducting layer (304). Further, the electrode (300, 400, 500) includes at least one connector (120, 402, 504) distributed across the first conducting layer (304) and adapted to conduct an electric current from the electrode (300, 400, 500).

Abstract: The present subject matter describes a gasification system (100) for gasifying a variety of feedstocks. A first stage gasifier (105) receives a feedstock either from a first group of feedstocks or a second group of feedstocks or both. The first stage gasifier decomposes the received feedstock to produce a first product. A second stage gasifier (115) is connected to the first stage gasifier (105) for receiving the first product. In addition, the second stage gasifier (115) receives a feedstock either from a third group of feedstocks or a fourth group of feedstocks or both. The second stage gasifier (115) gasifies the first product and the received feedstock to produce syngas.

Abstract: A process for selective removal of mercaptan from aviation turbine fuel feed includes mixing aviation turbine fuel feed with hydrogen, at a pressure in a range from 3 bar to 20 bar to obtain a reaction mixture. The reaction mixture is heated at a temperature range of 150° C. to 350° C. to obtain a heated mixture. The heated mixture is reacted with a hydrotreating catalyst in a rector to obtain a reactor effluent, and H2S gas is stripped from the reactor effluent to obtain a stripper bottom product. Moisture is removed from the stripper bottom product to obtain aviation turbine fuel product having less than 10 ppm mercaptan. The aviation fuel product has improved properties such as color and acidity. Embodiments also relate to an aviation turbine fuel product having less than 10 ppm mercaptan prepared by the described process of the present invention.

Abstract: The present subject matter describes a gasification system (100) for gasifying a variety of feedstocks. A first stage gasifier (105) receives a feedstock either from a first group of feedstocks or a second group of feedstocks or both. The first stage gasifier decomposes the received feedstock to produce a first product. A second stage gasifier (115) is connected to the first stage gasifier (105) for receiving the first product. In addition, the second stage gasifier (115) receives a feedstock either from a third group of feedstocks or a fourth group of feedstocks or both. The second stage gasifier (115) gasifies the first product and the received feedstock to produce syngas.

Abstract: The present subject matter relates to a process of reforming a natural gas stream by steam. The reforming is carried out at a temperature within a predetermined range to form a substantially carbon monoxide free product mixture of hydrogen and natural gas. The reforming is carried out in presence of a nickel-based catalyst. The temperature is controlled in a range of about 350° C. to about 390° C. The reforming can be started or stopped or its rate can be varied, based on an outflow demand of the product mixture of hydrogen and natural gas.