Butanol from isobutene

Extraction of sec-butanol from isobutene Hydrothermal oxidation of organic wastes in water... 

In 1976 he was appointed to Associate Professor for Technical Chemistry at the University Hannover. His research group experimentally investigated the interrelation of adsorption, transfer processes and chemical reaction in bubble columns by means of various model reactions a) the formation of tertiary-butanol from isobutene in the presence of sulphuric acid as a catalyst b) the absorption and interphase mass transfer of CO2 in the presence and absence of the enzyme carboanhydrase c) chlorination of toluene d) Fischer-Tropsch synthesis. Based on these data, the processes were mathematically modelled Fluid dynamic properties in Fischer-Tropsch Slurry Reactors were evaluated and mass transfer limitation of the process was proved. In addition, the solubiHties of oxygen and CO2 in various aqueous solutions and those of chlorine in benzene and toluene were determined. Within the framework of development of a process for reconditioning of nuclear fuel wastes the kinetics of the denitration of efQuents with formic acid was investigated. 

FIG. 22-2 Process for the integrated reaction and separation of sec-butanol from isobutene. 

Molybdophosphoric acid was also used to prepare HPA-polymer composite film catalysts, using polyphenylene oxide, polyethersulfone and polysulfone as polymers [4], The membrane-like materials were tested as catalysts in the liquid-phase synthesis of tert-butanol from isobutene and water, showing higher catalytic activity than the bulk acid. 

Diphenyl carbonate from dimethyl carbonate and phenol Dibutyl phthalate from butanol and phthalic acid Ethyl acetate from ethanol and butyl acetate Recovery of acetic acid and methanol from methyl acetate by-product of vinyl acetate production Nylon 6,6 prepolymer from adipic acid and hexamethylenediamine MTBE from isobutene and methanol TAME from pentenes and methanol Separation of close boiling 3- and 4-picoline by complexation with organic acids Separation of close-boiling meta and para xylenes by formation of tert-butyl meta-xyxlene Cumene from propylene and benzene General process for the alkylation of aromatics with olefins Production of specific higher and lower alkenes from butenes... 

In France and Japan, isoprene is also produced from isobutene (or t-butanol) and formaldehyde in 1 or 2 stage processes (via a 1,3-dioxan intermediate). The overall reaction is ... 

Jesse TW et al (2002) Production of butanol from starch-based waste packing peanuts and agricultural waste. J Ind Microbiol Biotechnol 29(3) 117—23 Jhung S, Chang J-S (2009) Trimeiization of isobutene over solid acid catalysts. Catal Surv Asia 13... 

In the last few years, Idemitsu commercialized a 5000 metric ton/year integrated reaction and separation process in SCR isobutene, as shown in Rig. 22-24. The reaction of isobutene and water takes place in the water phase and is acid catalyzed. The product, sec-butanol, is extracted into the isobutene phase to drive the reversible reaction to the right. The. s c-butanol is then recovered from the isobutene by depressurizing the SCR phase, and the isobutene is recompressed and recycled. 

Fig. 3. FT-IR spectra of the adsorbed species arising from the interaction of (a) rerr-butanol and (b) isobutane over a combustion catalyst (MgCr204) at 423 K, and from rerr-butanol (373 K, c), isobutene (300 K, d) and isobutane (380 K, e) on a selective oxidation catalyst.

In the oxidation of f-butanol, acetone and isobutene appear [46] as intermediate species. Acetone can arise from two possible sequences. In one,... 

Applications of POMs to catalysis have been periodically reviewed [33 0]. Several industrial processes were developed and commercialized, mainly in Japan. Examples include liquid-phase hydration ofpropene to isopropanol in 1972, vapor-phase oxidation of methacrolein to methacrylic acid in 1982, liquid-phase hydration of isobutene for its separation from butane-butene fractions in 1984, biphasic polymerization of THE to polymeric diol in 1985 and hydration of -butene to 2-butanol in 1989. In 1997 direct oxidation of ethylene to acetic acid was industrialized by Showa Denko and in 2001 production of ethyl acetate by BP Amoco. 

Mitsubishi Rayon in Japan has commercialized a three-step process on the basis of a two-step catalytic oxidation of isobutene, preferentially through f-butanol as primary intermediate. This process suffers not only from a relatively moderate overall MMA yield ( 80%), but also from increasing isobutene cost due to its alternative use for MTBE (methyl fert.-butyl ether) production as a gasoline additive. 

Aliphatic or alicyclic fluoroformates may be prepared continuously from the reaction of the corresponding alcohols with a mixture of carbonyl halides e.g. COFj, COCIF and COClj at -20 to +80 "C in the presence of isobutene, which acts as a hydrogen halide acceptor). The process was illustrated using methanol, t-butanol and cyclohexanol as examples [1118]. 

Remark. Pentanols or amyl alcohols, and more specifically 1-pentanok 2-methyl 1-butanol, and 3-methyl 1-butanol, do not enjoy the industrial importance of the above alcohols. They are prepared by Oxo synthesis and hydrogenation from n-butenes and isobutene. They are used as solvents and their esters as perfumes. 

MTBE synthesis from /-butanol and methanol in a membrane reactor has been reported by Salomon et al. [2.453]. Hydrophilic zeolite membranes (mordenite or NaA) were employed to selectively remove water from the reaction atmosphere during the gas-phase synthesis of MTBE. This reaction was carried out over a bed of Amberlyst 15 catalyst packed in the inside of a zeolite tubular membrane. Prior to reaction, the zeolite membranes were characterized by measuring their performance in the separation of the equilibrium mixture containing water, methanol, /-butanol, MTBE, and isobutene. The results obtained with zeolite membrane reactors were compared with those of a fixed-bed reactor (FBR) under the same operating conditions. MTBE yields obtained with the PBMR at 334 K reached 67.6 %, under conditions, where the equilibrium value without product removal (FBR) would be 60.9%. 

---