Provided is a methanol plant that can obtain fresh water from sea water by using, in a seawater desalination device, the exhaust heat discharged in a step for producing methanol from natural gas. The methanol plant is provided with: a heat exchanger (4) that recovers into a thermal medium (for example, seawater) the exhaust heat discharged from a step for producing methanol from a feed stock (for example, natural gas); and a seawater desalinization device (6) that obtains freshwater from seawater using the exhaust heat recovered by means of the thermal medium.

The invention relates to a fuel processor component for a propylene glycol fuel processor, comprising at least one housing (G) having at least two inlets (E1, E2) and two outlets (A1, A2), wherein there is a multitude of first plates (P1) having a first side (S1) and a second side (S2) and second plates (P2) having a third side (S3) and a fourth side (S4) arranged as a stack in the housing (G), wherein the stacked first and second plates (P1, P2) form at least first cavities (H1) and second cavities (H2), wherein the first inlet (E1) has fluid connection to the first outlet (A1) via first cavities (H1) and the second inlet (E2) has fluid connection to the second outlet (A2) via second cavities (H2). The invention further relates to a propylene glycol fuel processor.

Systems and methods are provided for conversion of gas phase reactants including CO and H.sub.2 to C.sub.2+ products using multiple catalysts in a single reactor while reducing or minimizing deactivation of the catalysts. Separate catalysts can be used that correspond to a first catalyst, such as a catalyst for synthesis of methanol from synthesis gas, and a second catalyst, such as a catalyst for conversion of methanol to a desired C.sub.2+ product. The separate catalysts can be loaded into the reactor in distinct layers that are separated by spacer layers. The spacer layers can correspond to relatively inert particles, such as silica particles. Optionally, the spacer layer can include an adsorbent, such as boron supported on alumina or boron carbide particles. The adsorbent can be suitable for selective adsorption of the one or more reaction products (such as one or more reaction by-products), to allow for further reduction or minimization of the deactivation of the conversion catalysts.

Utilizing the common knowledge formula for creation of methanol CO.sub.2+3H.sub.2.fwdarw.CH.sub.3OH+H.sub.2O; for each mole of carbon dioxide, three moles of hydrogen are needed to produce one equivalent unit of methanol. Mixing two gases and producing methanol can be accomplished per the one-line diagram concept, FIG. 1, and gas mixing apparatus, FIG. 2; under high pressure (from 3250 to 5000 psi) and high temperature (750 to 800 F.) without the presence of a catalyst. The hypothesis in this case is that the closer the mixing temperature is to the auto-ignition of hydrogen, the higher is the quality of the mixing environment. The mixing temperature in my invention is guided by the auto-ignition of hydrogen in this case (auto-ignition for hydrogen is 932 F. (or 500 C.) and the auto-ignition temperature for methanol is 867 F. (or 464 C.). After mixing the two gases, the result is methanol and water. The first step in this stage is to cool the substance by way of cooling tower, followed by a pressure lowering tank. Next is a separation process to separate methanol and water. By cooling the substance/mixture about 28.4 F. (2 C.), the water will freeze, turning into ice, and ice will be removed from methanol mechanically. Water and methanol then will be stored in appropriate tanks (FIG. 1).

The invention provides a catalyst system comprising: a) one or more Group 1 metal phosphotungstate-containing species; and b) one or more catalytic species suitable for hydrogenation; and a process for the preparation of monoethylene glycol from starting material comprising one or more saccharides, by contacting said starting material with hydrogen in a reactor in the presence of a solvent and said catalyst system.

The invention provides a process for the preparation of glycols from a saccharide-containing feedstock in a reactor system, said process comprising: i) providing a first feed stream comprising said saccharide-containing feedstock in a first solvent at a N temperature of no more than 160 C.; ii) providing a second feed stream comprising a tungsten-based retro-aldol catalytic species and an alkali metal containing species in a second solvent at a temperature in the range of from 150 to 250 C.; iii) combining the first feed stream and the second feed stream, before they are provided to the reactor system, to form a combined feed stream; iv) providing the combined feed stream to the reactor system and operating the reactor at a temperature in the range of from 150 C. to 250 C.; and v) also contacting the combined feed stream with a hydrogenation catalytic species in the presence of hydrogen, wherein the molar ratio of alkali metal:tungsten in the combined feed stream is in the range of from 0.55 to 6.

Methods for utilizing carbon dioxide to produce multi-carbon products are disclosed. The systems and methods of the present disclosure involve: reducing CO.sub.2 to produce a first product mixture comprising an alcohol product mixture comprising one or more alcohols and a paraffin product mixture comprising one or more paraffins; dehydrating the alcohol product mixture to form an olefin product mixture comprising one or more olefins; oligomerizing the olefin product mixture to form a higher olefin product mixture comprising unsaturated paraffins and optionally aromatics; and reducing the higher olefin product mixture to form a higher hydrocarbon product mixture comprising unsaturated paraffins and optionally aromatics. Catalyst materials and reaction conditions for individual steps are disclosed to optimize yield for ethanol or jet fuel range hydrocarbons.

Methods for utilizing carbon dioxide to produce multi-carbon products are disclosed. The systems and methods of the present disclosure involve: reducing CO.sub.2 to produce a first product mixture comprising an alcohol product mixture comprising one or more alcohols and a paraffin product mixture comprising one or more paraffins; dehydrating the alcohol product mixture to form an olefin product mixture comprising one or more olefins; oligomerizing the olefin product mixture to form a higher olefin product mixture comprising unsaturated paraffins and optionally aromatics; and reducing the higher olefin product mixture to form a higher hydrocarbon product mixture comprising unsaturated paraffins and optionally aromatics. Catalyst materials and reaction conditions for individual steps are disclosed to optimize yield for ethanol or jet fuel range hydrocarbons.

The invention provides a continuous process for the preparation of ethylene glycol and 1, 2-propylene glycol from starting material comprising one or more saccharides, said process being carried out in a reactor system comprising a reactor vessel equipped with an external recycle loop and said process comprising the steps of: i) providing the starting material in a solvent, via an inlet, to the external recycle loop and contacting it therein with a retro-aldol catalyst composition to provide an intermediate stream; ii) then contacting said intermediate stream with hydrogen in the presence of a hydrogenation catalyst composition in the reactor vessel; iii) withdrawing a product stream comprising glycols from the reactor vessel; iv) providing a portion of said product stream, via an outlet, for separation and purification of the glycols contained therein; and v) recycling the remainder of said product stream via the external recycle loop.

During the production of methanol from inert-rich syngas, a catalytic pre-reactor is installed upstream of the single- or multi-stage synthesis loop, a first part of the syngas being converted to methanol in the catalytic pre-reactor. An inert gas separation stage, for example a pressure swing adsorption system or a membrane system, can be connected downstream of the synthesis loop, whereby a hydrogen-enriched syngas stream can be returned to the synthesis loop. In the processing of methane-rich syngas, the inert gas separation stage may also have an autothermal reformer in which methane is converted to carbon oxides and hydrogen, which are also returned into the synthesis loop.