The way the joint production of ethyl and-phenethyl alcohols
(57) Abstract:The invention relates to the technology of organic synthesis, namely the way the joint production and ethyl-phenethyl alcohols. Describes how the joint production and ethyl-phenethyl alcohols by the catalytic hydrogenation of acetaldehyde (ACA) and acetophenone (ACP) at elevated temperature and pressure, characterized in that the hydrogenation of acetaldehyde and acetophenone are at a mass ratio of acetaldehyde to acetophenone equal to 0.05 to 0.1:1, and the surface of the catalyst continuously process the components of the hydrogenated feed is cut. The technical result is an increase in conversion act and ACA and increase the service life of the catalyst. 1 C.p. f-crystals, 1 table. The invention relates to the technology of organic synthesis, and in particular to a method for producing ethyl-phenethyl alcohols that can be used in various industries, in particular, in the production of the joint production of propylene oxide and styrene.A known method of recovering organic carboxylic compounds: aldehydes and ketones to the corresponding alcohols at a temperature of 100-300oC (150-300oC, the pressure 70,3-351,5 ATI, PBA is the process periodically at high temperatures and pressures, low conversion and selectivity to the desired products.The closest to the technical nature of the claimed method is hydrogenation of aldehydes and ketones to the corresponding alcohols on the ruthenium catalyst. The hydrogenation is carried out at a temperature of 15-150oC and a hydrogen pressure of 1-100 MPa. As solvents used alcohols, ethers or alkanes, [U.S. patent 4777302, MKI C 07 C 9/14, 1988].The disadvantage of this method is the low conversion of the ketone, wt. %.: 89-70 and 60-38 through 20 and 1,000 hours, respectively.The objective of the invention is to increase the conversion of acetophenone. (ACF) and acetaldehyde (AC) and increase the service life of the catalyst.The problem is solved by a method for simultaneous hydrogenation of acetophenone and acetaldehyde at elevated temperature and pressure over a copper-grombalia the catalyst at a mass ratio of acetaldehyde to acetophenone, 0.05 to 1.0:1.0 for the continuous surface treatment of the catalyst components of the hydrogenated feed is cut.Distinctive features of the process are the process when the ratio of acetophenone and acetaldehyde 95-50 wt.% and 5-50 wt.%, during the continuous surface treatment nepreryvnaya surface treatment of the catalyst components of the hydrogenated feed is separated from the deposition of polymer and resins, formed during the hydrogenation of acetaldehyde and acetophenone, you can simplify the process and increase the conversion of the initial products without deterioration process. The activity of the catalyst remains stable over time.Apparently here the mechanism of deactivation of the catalyst is that the polymers or resins, getting on the catalyst surface, cover the inner surface of the pores and clog the entrance into them, thus inhibiting the mass transfer in the pores, blocking the active centers of the catalyst, preventing its physico-chemical interaction with the incoming substances.The way the joint production of alcohols is carried out in a hollow bubbling reactor for heterogeneous copper-grombalia catalyst. Hydrogenation lead electrolytic hydrogen at elevated temperature and pressure in the suspension mode. The resulting hydrogenation product is sent to the column for separation. To separate the hydrogenated feed is cut into narrow fractions used rotary distillation installation, which consists of two main parts - speakers and automatic control unit, which is mechanically and functionally interrelated.Separating the de is animalsense up steam and flowing spiral down the liquid. Thermostat column provides the desired proximity to the adiabatic mass-transfer regime in the column.The reaction products are analyzed by chromatographic method. Used chromatograph "Crystal 2000". The sorbent prepared according to GOST 10003-90.The inventive method is illustrated by the following examples of its implementation.Example 1. In the hollow bubble reactor hydrogenation serves 380 g/h of pure acetophenone. In the acetophenone impose additional 20 g/hour of acetaldehyde. The process is conducted at a temperature of 165oC and a pressure of 40 ATM. The flow of catalyst is 2.3 g/hour. Hydrogenation of lead methane-hydrogen fraction composition, wt. %: hydrogen 88,2 and methane 11,8. The volumetric feed rate of 0.6 h-1. The volumetric ratio of feedstock to hydrogen is 1:3. The surface of the catalyst is continuously processed components of the hydrogenated feed is cut. Conversion of acetophenone and acetaldehyde, respectively 97,67% and 100%.Copper-jambalay catalyst has the feature according to TU-38.102 142-80. Taken at the reactor exit sample section of hydrogenated feed analyzed for content ACF, IFC, ACA, ethyl alcohol by gas chromatography.In prominently section of hydrogenated feed stable supported the activity of the catalyst.Example 2. The process is carried out in the conditions of example 1, but, unlike example 1, the mass ratio ACF and ACA is 0.1:1, flow of catalyst 1.5 g/hour. Conversion, %: ACF and ACE of 97.78 and 100, respectively.Example 3. The process is carried out in the conditions of example 1, but, unlike example 1, the mass ratio ACF and ACA is 0,18:1, flow of catalyst and 1.0 g/hour. Conversion, %, act and ACA 98,51 and 100, respectively.Example 4. The process is carried out in the conditions of example 1, but, unlike example 1, the mass ratio ACF and ACA is 0.25:1, flow of catalyst 0.5 g/hour.Conversion, %, act and ACA 98,43 and 100, respectively.Example 5. The process is carried out in the conditions of example 1, but, unlike example 1, the mass ratio ACF and ACA is 0.43:1, flow of catalyst 0.5 g/hour. Conversion, %, act and ACA 98,14 and 100, respectively.Example 6. The process is carried out in the conditions of example 1, but, unlike example 1, the mass ratio ACF and ACA is 0.67:1, flow of 0.4 g catalyst/hour. Conversion, %, act and ACA is 97,83 and 100, respectively.Example 7. The process is carried out in the conditions of example 1, but, unlike example 1, the mass ratio ACF and ACE is 1:1, flow of catalyst and 0.4 g/x example 4 but, unlike example 4, in the hydrogenation reactor is served instead of acetophenone (ACP) acetophenone fraction (ACFF) and instead of acetaldehyde (ACA) acetaldehyde fraction (ACAP), which are byproducts in a co-production of propylene oxide with styrene. The composition ACAF, wt. %: propylene oxide-1,4 and ACAF - 98,60. The composition ACFF, wt.%: light hydrocarbons-0.05; ethylbenzene-2,95; styrene-0,81; methylsterol - 0,10; benzaldehyde - 0,68; ACF-84,74; IFC-9,70; heavy hydrocarbons-0,72; unknown peaks to 0.21.Example 9. The process is carried out in the conditions of example 3, but in contrast to example 3, in the hydrogenation reactor instead of acetophenone serves acetophenone faction and instead of acetaldehyde - acetaldehyde fraction.The results presented in the table.From the above examples that the proposed method for simultaneous receiving and ethyl-phenethyl alcohols can simplify the process, increase conversion products: acetaldehyde and acetophenone, to increase the service life of the catalyst. 1. The way the joint production and ethyl-phenethyl alcohols by the catalytic hydrogenation of acetaldehyde and acetophenone at elevated temperature and pressure, characterized in that h is typ 0.05 to 0.1 : 1, and the surface of the catalyst continuously process the components of the hydrogenated feed is cut.2. The method according to p. 1, characterized in that as acetophenone and acetaldehyde using, respectively, acetophenone and acetaldehyde fraction obtained in a co-production of propylene oxide and styrene.
FIELD: hydrogenation-dehydrogenation catalysts.
SUBSTANCE: invention provides copper and silica-based catalyst containing 22.5-53.0% copper. Catalyst is prepared by reductive thermal decomposition of copper silicate in hydrogen flow at 380-450°C. catalyst is used in dihydroxyalkane production processes carried out at 180-200°C.
EFFECT: increased activity and selectivity of catalyst.
3 cl, 1 tbl, 8 ex
SUBSTANCE: method includes addition of polyoxy compound and water into reactor, removal of air from reactor, hermetisation of reactor with gaseous hydrogen with specified initial hydrogen pressure and interaction of polyoxy compound with hydrogen in presence of catalyst with mixing reaction mixture. Reaction temperature is supported equal or higher than 120°C, reaction time constitutes not less than 5 minutes, catalyst represents mixed catalyst, including catalyst A and catalyst B, where active component of catalyst A includes transition metal of 8, 9 or 10 group, selected from iron, cobalt, nickel, ruthenium, rhodium, palladium, iridium and platinum, or their mixture, active component of catalyst B includes compound of tungsten oxide, tungsten sulfide, tungsten chloride, tungsten hydroxide, tungsten oxide bronze, tungstic acid, tungstate, metatungstic acid, metatungstate, paratungstic acid, paratungstate, tungsten-containing heteropolyacid, or their mixture. In addition weight ratio of active component of catalyst A and active component of catalyst B (counted per tungsten weight) is in the interval from 0.02 to 3000.
EFFECT: method makes it possible to obtain product with high output with application of catalyst, which can be obtained in mild conditions with low expenditures.
11 cl, 6 tbl, 9 ex
FIELD: organic chemistry, in particular production of high oxoalcohols.
SUBSTANCE: invention relates to method for production of high oxoalcohol from isomeric olefin mixture containing from 5 to 24 of carbon atoms. Claimed method includes hydroformylation in presence of catalyst at elevated temperature and elevated pressure. Hydroformylation in carried out in one step, and ones-through olefin conversion is limited in range of 40-90 %. Obtained reaction mixture after catalyst separation is preferably transferred to selective hydration carrying out at 120-220°C and pressure of 5-30 bar in presence of supported catalyst containing copper, nickel and chromium as active ingredients. Hydration product mixture is separated by distillation, and olefin fraction is recycled into hydroformylation step. As starting materials for hydroformylation mixtures of C8-, C9-, C12- or C16-olefins are used.
EFFECT: high olefin conversion ratio, selectivity, and capability.
15 cl, 1 dwg, 1 tbl, 2 ex
FIELD: methods of production of 1.3 alkandiol.
SUBSTANCE: the invention is pertaining to the field of chemical industry, in particular, to production of 1.3 alkandiol by hydrogenation of the raw material, containing 3-hydroxyaldehyde at presence of a catalyst and a source of hydrogen, where as a source of hydrogen use a synthesis gas, and the catalyst represents a heterogeneous catalyst containing copper on the carrier; and also to the method of production of 1.3-alkandiol by conversion of an oxide in the process including a hydroformylation and hydrogenation. At that it is not obligatory to realize the indicated phases simultaneously in one reaction vessel. The reached technical result consists in essential reduction of the fixed value of equipment and in bringing to a "single-phase" production of 1.3-propandiol (or a similar 3-alcandil) from ethylene oxide (or a corresponding oxide).
EFFECT: the invention ensures essential reduction of the fixed value of equipment and reduction to a "single-phase" process of the propandiol or alkandiol production.
9 cl, 2 tbl, 2 ex