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The report presents the economics of Dimethyl Ether (DME) production from natural gas and carbon dioxide (CO2). In the process under analysis, natural gas is reformed with CO2 yielding synthesis gas (syngas). Syngas is then fed to a one-step process for DME generation - syngas conversion into methanol and methanol dehydration into DME are carried out in a single reaction step. The economic analysis performed assumes a plant located in the United States.
This report presents the economics of Dimethyl Ether (DME) production from natural gas and carbon dioxide (CO2) in the United States. The process under analysis comprises the reforming of natural gas with CO2 for generating synthesis gas (syngas). Syngas, in turn, is used as feed for the two-step DME synthesis - the gas is first converted into methanol and methanol intermediate is dehydrated into DME in a different reactor after methanol purification.
The report presents the economics of Dimethyl Ether (DME) production from synthesis gas (syngas) through a one-step process. In this process, syngas is reacted in the presence of a bifunctional catalyst that supports methanol syntheses and the subsequent dehydration of methanol to DME within a single reactor. The economic analysis performed assumes a plant located in the United States.
This report concerns the econoimics of of Dimethyl Ether (DME) production from synthesis gas through the indirect process. Synthesis is gas is first converted into methanol, which then becomes the feed for a second step in which DME is produced through catalytic dehydration. The economic analysis is based on a United Stats-based plant.
This report analyses the economics of producing Dimethyl Ether (DME) from wood chips in the United States. In the process under analysis, the wood chips are dried and then subjected to pyrolysis and partial oxidation for generating synthesis gas (syngas). Syngas is used for methanol generation and methanol then becomes the feed for a catalytic dehydration process that yields DME.
This report examines the costs related to Dimethyl Terephthalate (DMT) production from p-xylene and methanol in the United States, via typical oxidation and esterification processes. In this process, operations theoretically take place in alternate oxidation and esterification (with methanol) phases. P-xylene is oxidized to p-toluic acid, which is converted to p-methyl toluate, then to methyl terephthalate and ,finally, to DMT.
It presents the economics of Dimethyl Terephthalate (DMT) production from toluene and methanol in a plant located in the United States. Toluene is converted to p-xylene via a catalytic disproportionation process similar to ExxonMobil PxMax. The p-xylene is oxidized to p-toluic acid, which is esterified with methanol to generate DMT.
This report provides a techno-economic analysis of Dimethylfuran (DMF) production from glucose syrup in the United States. In this process, glucose is isomerized to fructose, which is dehydrated forming hydroxymethylfurfural (HMF) intermediate. Then, HMF is converted to DMF.
This feasibility study provides an economic analysis of Dinitrotoluene (DNT) production from toluene and nitric acid in the United States via a two-step nitration process. Initially, nitric and sulfuric acids are reacted with toluene to form mononitrotoluene, which is further nitrated to produce DNT.
This study reviews the costs associated with Diphenyl Carbonate (DPC) production from ethylene oxide and phenol in the United States. The process examined is similar to Asahi Kasei process, which dimethyl carbonate (DMC) intermediate is initially produced from ethylene oxide and methanol. Then, the DMC reacts with phenol to produce phenylmethyl carbonate, followed by disproportionation to DPC.
It presents the economics of Diphenyl Carbonate (DPC) production from phenol and methanol using a process similar to the one proposed by SABIC, located in the United States. In this process, methanol undergoes an oxidative carbonylation to form dimethyl carbonate (DMC). It reacts with phenol to produce phenylmethyl carbonate, followed by disproportionation to DPC.
This report presents a techno-economic study about Diphenyl Carbonate (DPC) production from phenol and methanol in the United States. This process is similar to Ube process. Initially, methanol is submitted to oxidative coupling to produce dimethyl oxalate (DMO). The DMO is then transesterified with phenol to diphenyl oxalate, which undergoes decarbonylation to DPC.
This report presents the economics of Diphenyl Carbonate (DPC) production from phosgene and phenol using a typical interfacial process. The economic assessment assumes a plant located in the United States.
This feasibility study reviews Diphenyl Carbonate (DPC) production from phenol. The process under analysis is an oxidative carbonylation process, which involves the direct reaction of phenol with carbon monoxide to form DPC. The economic analysis is based on a plant constructed in the United States.
This report provides the economics of DL-Methionine production from methional and hydrogen cyanide (HCN) in the United States via a typical carbonate process. Initially, methional is reacted with HCN, ammonia and carbon dioxide to produce 5-(2-methylmercaptoethyl)-hydantoin (MMEH), which is hydrolyzed to potassium methioninate (KMET). Finally, the KMET is acidified, liberating methionine.
This study presents the economics of an integrated process for DL-Methionine production starting from propylene in the USA. Initially, propylene is oxidized to acrolein, which is then reacted with methyl mercaptan to generate methional. Finally, methional is reacted with hydrogen cyanide (HCN) to form methionine via a typical carbonate process.
This report presents the economics of DL-Methionine production from acrolein, methyl mercaptan, and hydrogen cyanide (HCN) in the United States. In this process, refined acrolein and methyl mercaptan are reacted to form MMP (also called methional), which is further reacted with HCN to generate DL-Methionine via a typical carbonate process.
This report presents the economics of SBR production from n-butane and styrene. In this process, 1,3-Butadiene is initially produced from n-butane via a dehydrogenation process that is similar to Lummus Catadiene. Then, styrene and butadiene are polymerized via a typical cold emulsion process for generating a non-oil extended, non-staining grade of emulsion SBR (similar to 1502).
This report presents the economics of SBR production starting from butadiene and styrene. The analysis encompasses a plant located in the United States, employing a typical cold emulsion process for generating a non-oil extended, non-staining grade of emulsion SBR (similar to 1502). In this process, an emulsion comprising water, styrene and butadiene is polymerized into a latex, which is then coagulated to form the SBR.
This study presents a techno-economic analysis of Epichlorohydrin production from propylene and chlorine in the United States. In this process, propylene is subjected to an acetoxylation reaction, followed by hydrolysis, generating allyl alcohol, which is then chlorinated, yielding glycerol dichlorohydrins. Finally, the glycerol dichlorohydrins generated are reacted with calcium hydroxide, yielding Epichlorohydrin.
This feasibility study provides an economic analysis of Epichlorohydrin (ECH) production from propylene and chlorine in the United States. Initially, propylene is chlorinated, generating allyl chloride, which is reacted with hypochlorous acid, formed by chlorine dispersion in water. Finally, the glycerol dichlorohydrins generated are hydrolyzed with calcium hydroxide, yielding ECH.
This report provides a techno-economic study of an early stage process for Epichlorohydrin production from acrolein in the United States. The process examined is a non-commercial route based on Dow Chemical patents.
This report presents a economic analysis of Epichlorohydrin production from allyl chloride and chlorine in the United States using a typical hypochlorination process. Initially, allyl chloride is reacted with hypochlorous acid, formed by chlorine dispersion in water. The glycerol dichlorohydrins generated are then treated with calcium hydroxide to promote epoxidation, yielding ECH.
This study provides an economic analysis of Epichlorohydrin production from glycerol in the United States. Initially, glycerol is reacted with hydrogen chloride in a hydrochlorination reaction, generating dichlorohydrins (DCH). Then, the DCH is hydrolyzed by caustic soda, yielding epichlorohydrin (ECH).
This report presents the economics of Epichlorohydrin (ECH) production from glycerol and sodium chloride in the United States. Initially, brine is decomposed electrolytically in a membrane cell, producing chlorine, caustic soda and hydrogen. The hydrogen and chlorine react forming hydrogen chloride (HCl). Finally, glycerol is reacted with HCl, generating dichlorohydrins (DCH), which are hydrolyzed to ECH by the caustic soda.
This study provides an economic analysis of Epoxy Cresol Novolac Resin production from epichlorohydrin and o-cresol for a plant located in the United States.
This report presents a techno-economic study of a process for Epoxy Phenol Novolac Resin production from phenol, formaldehyde and epichlorohydrin in a plant constructed in the United States. The process examined comprises two main steps: condensation of phenol and formaldehyde to produce phenol novolac resin; and (2) epoxidation of the phenol novolac resin with epichlorohydrin to form Epoxy Phenol Novolac Resin.
This report presents the feasibility analysis of an on-purpose Ethyl tert-Butyl Ether (ETBE) production plant from butane and ethanol in the United States. Initially, n-butane is isomerized to isobutane, which is then subjected to a dehydrogenation, yielding isobutylene. In the final step, generated isobutylene and ethanol react leading to the formation of ETBE. These steps are similar to Butamer, Oleflex and Ethermax processes in sequence.
This study presents an economical analysis of Ethyl tert-Butyl Ether (ETBE) production from FCC C4 raffinate and ethanol using a process similar to UOP's Ethermax process for isobutylene etherification in China. In this process, the etherification reaction of isobutylene from FCC C4 raffinate stream with ethanol is conducted in two steps, the first step being in a conventional reactor and the second in a reactive distillation column.
This study presents an economical analysis of Ethyl tert-Butyl Ether (ETBE) production from isobutylene and ethanol in the United States. In this process, isobutylene obtained from a butane hydrogenation plant is submitted to a etherification reaction with ethanol conducted in two steps. The first step is in a conventional reactor and the second in a reactive distillation column.
This study provides an economical analysis of Ethyl tert-Butyl Ether (ETBE) production from a raffinate-1 stream and ethanol using a process similar to UOP's Ethermax process for isobutylene etherification in China. In this process, isobutylene from raffinate-1 is submitted to etherification with ethanol in a conventional reactor and in a reactive distillation column.
This report presents a techno-economic study of hydrous Ethanol and raw sugar production from sugarcane using a typical process in Brazil. In this process, part of the sugarcane juice is used in the production of raw sugar and part is fermented to produce hydrous Ethanol. The sugarcane bagasse is burned for electricity generation.
This report presents a techno-economic analysis of second generation Ethanol production from corn stover in the United States using a process similar to AVAP technology, developed by American Process. In this process, biomass is fractionated into cellulose, hemicelluloses and lignin by using a sulfur dioxide-ethanol-water solution. The cellulose and hemicelluloses obtained from biomass are converted to monomeric sugars, which are then used to produce Ethanol via fermentation.
This feasibility study presents the economics of Ethanol production from corn stover in the United States using a process similar to GreenPower, developed by American Process. In this process, only hemicelluloses are extracted from biomass and used to produce hydrous ethanol via fermentation of monomer sugars.
This report presents a techno-economic study of Ethanol production from municipal solid waste (MSW) in the United States using a process similar to AVAP technology, developed by American Process. In this process, the MSW is fractionated into cellulose, hemicelluloses and lignin by using a sulfur dioxide-ethanol-water solution. The cellulose and hemicelluloses obtained from biomass are converted to monomeric sugars, which are then used to produce Ethanol via fermentation.
This report approaches the economics of second generation Ethanol production from sugarcane bagasse in Brazil using a biochemical conversion process similar to AVAP technology, developed by American Process. In this process, biomass is fractionated into cellulose, hemicelluloses and lignin by using a sulfur dioxide-ethanol-water solution. The cellulose and hemicelluloses obtained from biomass are converted to monomeric sugars, which are then used to produce Ethanol via fermentation.
This feasibility study provides the economic analysis of second generation Ethanol production from sugarcane bagasse in Brazil. The process examined is similar to GreenPower, also developed by American Process. In this process, only hemicelluloses are extracted from biomass and are used to produce hydrous Ethanol via fermentation of monomer sugars.
This feasibility study provides an economic analysis of Ethanol production from switchgrass in the United States using a biochemical conversion process similar to AVAP technology, developed by American Process. In this process, biomass is fractionated into cellulose, hemicelluloses and lignin by using a sulfur dioxide-ethanol-water solution. The cellulose and hemicelluloses obtained from biomass are converted to monomeric sugars, which are then used to produce Ethanol via fermentation.
This report presents a techno-economic analysis of Ethanol production from wood chips in the United States using a process similar to AVAP, developed by American Process. In this process, cellulose and hemicelluloses are obtained from biomass and are used to produce hydrous Ethanol via fermentation of monomer sugars.
This report provides a economic analysis of second generation Ethanol production from wood chips via a thermochemical process in the United States. In this process, biomass is subjected to gasification generating syngas, which is then converted to hydrous Ethanol.