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This report examines the costs related to Polypropylene (PP) Impact Copolymer production from polymer grade (PG) propylene and ethylene in the United States, using a typical improved slurry phase polymerization process.
It presents the economics of Polypropylene (PP) Impact Copolymer production from polymer grade propylene and ethylene in the United States, using a bulk/gas phase polymerization process similar to LyondellBasell Spheripol and Mitsui Hypol II. This process occurs in loop reactors followed by a gas-phase fluidized-bed reactor, which converts homopolymer to copolymer.
It presents the economics of Polypropylene (PP) Impact Copolymer production from polymer grade (PG) propylene and ethylene in the United States, using a gas phase polymerization process similar to LyondellBasell Spherizone process. This process employs two multi-zone circulating reactors (MZCRs) connected in series, with PP Homopolymer as intermediate.
This report presents the economics of Polypropylene (PP) Impact Copolymer production from polymer grade (PG) propylene and ethylene in the United States. The process examined in this report is similar to Grace UNIPOL process. This process occurs in fluidized-bed reactors (FBRs) connected in series.
In this report, the process reviewed is an integrated gasification combined cycle (IGCC) for Electricity generation from coal. In this process, coal is gasified and the resulting syngas is used as fuel in a combined cycle power plant. The economic analysis is based on a plant located in the USA.
The process examined in this report is an integrated gasification combined cycle (IGCC) for Electricity generation from coal, including carbon capture and sequestration (CCS) system. The economic analysis performed also assumes a plant located in the USA.
This report presents the economics of Invert Sugar Syrup production from raw sugar (sucrose) using a process similar to the European Sugar Holdings S.A.R.L. technology. In the process under analysis, raw sugar is diluted and sucrose is hydrolyzed into glucose and fructose (invert sugar). This inversion reaction occurs in an ion-exchange resin bed. The economic analysis presented is based on a plant constructed in Germany
This report presents the economics of Isophorone Diisocyanate (IPDI) from isophorone and chlorine in the United States. In the process examined, isophorone is reacted with hydrogen cyanide, generating IPN. IPN obtained is then reacted with ammonia to form IPNI, which is hydrogenated with more ammonia to yield IPDA. Finally, IPDA reacts with phosgene to produce IPDI. The phosgene used is generated from chlorine and carbon monoxide.
This study examines the economics of Isophorone Diisocyanate (IPDI) production from isophorone and urea in the United States. This process is a non-phosgene route. In the non-phosgene process, IPDA reacts with urea and butanol generating a carbamate intermediate. Then, the carbamate is thermally cracked producing IPDI.
This report presents the economics of Iron Pyrite Gas production via a pyrite roasting plant in the United States.
This report examines the costs incurring from producing Isobutane via catalytic isomerization of n-butane. n-Butane is dehydrogenated to 1-butene, which is then rearranged to isobutylene. Finally, isobutylene is hydrogenated producing isobutane. The economic analysis provided assumes a plant located in the United States.
This report presents the economics of Isobutylbenzene (IBB) production from toluene and propylene based on an industrial plant located in the United States. In this process, toluene is reacted with propylene in the presence of a sodium/potassium alloy (NaK2) catalyst. A mixture of isobutylbenzene (IBB) and n-butylbenzene (NBB) are produced with IBB predominating.
This report presents the economics of Isobutylene production from isobutane in the United States. The process examined is a dehydrogenation process similar to Lummus CATOFIN. This technology uses a proprietary chromium dehydrogenation catalyst in a fixed-bed reactor.
It presents the economics of Isobutylene production from isobutane in the United States, using a dehydrogenation process similar to UOP Oleflex. This technology uses a proprietary platinum dehydrogenation catalyst in a moving-bed reactor.
This report analyses the economics of Isobutylene production from isobutane in the USA. The process examined is a dehydrogenation process similar to Uhde STAR. Initially, isobutane undergoes steam reforming, which is followed by oxyreaction, yielding isobutylene.
This study presents the economics of Isobutylene production from a crude C4s stream in the United States., using an extraction process similar to Total Isobutylene Acid Extraction process. In this process, sulfuric acid reacts with isobutylene to form an alcohol that is separated from the crude C4 raw material and, through a dehydration step, isobutylene is recovered.
This report presents the economics of Isodecanol production from nonenes in a typical industrial process based on cobalt catalyst. Initially, nonenes are submitted to hydroformylation to form the respectives C10 aldehydes. The aldehydes are then hydrogenated to the corresponding C10 alcohols. The industrial plant is located in the United States.
In this report, the economics of Isononanol production from octenes is analyzed based on a typical cobalt catalyst process, assuming a plant located in the United States. Initially, octenes are submitted to hydroformylation to form the respectives C9 aldehydes. The aldehydes are then hydrogenated to the corresponding C9 alcohols.
This report presents an economic study of Isononanol production from octenes in the presence of a rhodium catalyst. It assumes a plant located in the United States using a process similar to Johnson Matthey OXO alcohols process. Initially, octenes are submitted to hydroformylation to form the respectives C9 aldehydes. The aldehydes are then hydrogenated to the corresponding C9 alcohols.
This report presents the economics of Isophthalic Unsaturated Polyester production from maleic anhydride, isophthalic acid, propylene glycol and styrene using a two-stage batch process located in the United States. In the first stage, the glycol and isophthalic acid react to produce a cleat melt. Maleic anhydride is added subsequently and the resin is completed.
This study concerns the economics of Isoprene production from acetylene and acetone in the United States using a process similar to a Snamprogetti Acetylene-based process. Initially, acetylene and acetone undergo an addition reaction forming methylbutynol. This chemical is then subjected to a selective hydrogenation forming methylbutenol, which is finally dehydrated yielding Isoprene and water.
This study approaches the economics of Isoprene production from a crude C5s stream in the United States using a two-step extractive distillation process similar to BASF N-methylpyrrolidone (NMP) process.
This report presents the economics of Isoprene production from isobutylene (contained in a C4 cut stream) and formaldehyde in the United States via a typical two-step carbonylation process. Initially, isobutylene is reacted with formaldehyde forming 4,4-dimethyl-1,3-metadioxane (4-4 DMD). This intermediate is then cracked, producing Isoprene.
This report provides a techno-economic study of Isoprene production from propylene in the United States. Basically, this process comprises three main steps: propylene dimerization to 2-methyl-1-pentene; 2-methyl-1-pentene isomerization to 2-methyl-2-pentene; and cracking of 2-methyl-2-pentene to produce Isoprene.
In this report, it is approached the economics of Isopropyl Alcohol production from acetone in a typical acetone hydrogenation process, also assuming an industrial plant located in the United States. The reaction is carried out in liquid phase, in two fixed bed reactors in series, catalyzed by a Raney nickel catalyst.
This report approaches the economics of Isopropyl Alcohol production from Polymer Grade (PG) Propylene. This study is based on a plant located in the United States. Isopropyl Alcohol is obtained via a typical direct propylene hydration process which is carried out in the vapour phase using phosphoric acid on silica as catalyst.
This report presents an economic analysis of an integrated unit for producing Isopropyl Alcohol from propane in the United States. In a first unit, propane is converted to propylene via propane dehydrogenation. The propylene obtained is then converted to Isopropyl Alcohol via vapor phase hydration over a catalytic bed of phosphoric acid on silica.
This report presents the economics of Isopropyl Alcohol production from refinery grade (RG) propylene via a typical indirect propylene hydration process. In this process, RG propylene reacts with sulfuric acid to form isopropyl alcohol sulfates. Those sulfates are then reacted with water to form Isopropanol. The study assumes a plant located in the United States.
This report examines the costs related to Isosorbide Polycarbonate production from glucose and ethylene oxide in the USA, using a melt polymerization process similar of isosorbide and diphenyl carbonate (DPC) to the one proposed by Mitsubishi Chemical. Isosorbide is produced from glucose and DPC from ethylene oxide. Ethylene glycol is generated as a by-product.
This report presents the economics of Isosorbide production from glucose syrup. The process examined is similar to Roquette Freres process. The economic analysis provided is based on a plant located in the United States.
This study concerns Isosorbide production from sorbitol in the United States. The process reviewed in the analysis is a typical dehydration process. Sorbitol is submitted to cyclic dehydration, yielding isosorbide.
This report approaches an economic analysis of Itaconic Acid production from dimethyl succinate (DMS) and formaldehyde in the United States. In this process, Itaconic Acid is produced via a citraconate intermediate in a catalytic condensation reaction. Succinic acid is generated as a by-product.
This report presents the economics of Ketone-Alcohol (KA) Oil production from cyclohexane in the United States. In this pricess, cyclohexane is initially oxidized with air to produce a mixture of cyclohexanol and cyclohexanone, also known as KA Oil.
This report approaches the economics of L-Lysine Sulfate production from glucose syrup. In the process examined, glucose syrup is submitted to fed-batch fermentation to produce L-Lysine. The economic analysis provided assumes a plant located in the United States.
This feasibility study approaches an economic analysis of L-Lysine Monohydrochloride (or L-Lysine-HCl) production from glucose syrup in the United States using a conventional fermentation process. The L-Lysine-HCl is recovered via ion-exchange absorption and crystallization.
This report presents the economics of Lysine production from raw sugar (sucrose). Sucrose is initially hydrolyzed into glucose and fructose (invert sugar). The invert sugars are then fermented to produce L-Lysine, which is recovered as L-Lysine-HCl. The economic analysis provided assumes a plant located in Germany.
This report provides a feasibility study of Lactic Acid production from glucose syrup in the United States using a fermentation process. This process is similar to Cargill process. In this case, Lactic Acid is recovered by means of trialkylamine solvent extraction in the presence of carbon dioxide.
This study provides the economics of Lactic Acid production from glucose syrup using a fermentation process in the United States. This process is similar to Corbion process, in which Lactic Acid is recovered by acidification and purified by the use of a solvent.
This study provides a techno-economic analysis of Lactic Acid production from glucose syrup in the United States using a low pH fermentation process. In this process, glucose is directly converted to lactic acid.
This report presents the economics of Lactic Acid production from glucose syrup using a speculative, continuous, low pH, fermentation process in the United States. In this process, Lactic Acid is recovered from the fermentation broth through microfiltration and nanofiltration steps, generating an 80 wt% Technical Grade Lactic Acid, with 95 wt% purity.