Selective Hydrogenation of Diethyl Disulfide to Ethanethiol in the Presence of Sulfide Catalysts

The gas-phase reaction of diethyl disulfide hydrogenation at atmospheric pressure in the presence of supported transition metal sulfides was studied. The reaction of diethyl disulfide with hydrogen at T = 200°C resulted in ethanethiol, and the selectivity to ethanethiol was no lower than 94%. The selectivity decreased at a higher temperature because of diethyl disulfide decomposition to ethylene and hydrogen sulfide. The reaction of diethyl disulfide in the presence of hydrogen occurred at a higher rate and selectivity than that in an atmosphere of helium. The activity of metal sulfides supported on aluminum oxide was higher than on the other studied supports—aluminosilicate, silica gel, and a carbon support. Metal sulfides supported on Al₂O₃ were arranged in the following order according to their activity: Rh > Ru > Mo Pd > Ni > W. Bimetallic catalysts were less active than monometallic catalysts. The activity of catalysts increased with the sulfide sulfur content; the partial reduction of metal sulfides also increased the catalytic activity.     

Kinetic peculiarities of the reaction of liquefied hydrogen sulfide with propylene oxide

The kinetics of the liquid-phase reaction of hydrogen sulfide with propylene oxide was studied. In the presence of excess epoxide, the reaction occurred in two successive macrostages: (1) formation of 2-hydroxypropane-1-thiol and (2) formation of 1,1′-di(2-hydroxypropyl) sulfide. Both of the stages are autocatalytic. 2-Hydroxypropane-1-thiol was mainly formed in the presence of excess H₂S. The overall third order of the reaction (the first with respect to each reagent and to 2-hydroxypropane-1-thiol) was found. A kinetic scheme was proposed, and the rate constants of particular stages were calculated. The influence of various catalysts (active carbon, ion-exchange resins, metal oxides, and others) was studied, and the relative efficiency of some of them was determined. Translated fromIzvestiya Akademii Nauk. Seriya Khimicheskaya, No. 6, pp. 1083–1089, June, 1999.     

Activity of cobalt sulfide catalysts in the hydrogenolysis of dimethyl disulfide to methanethiol: Effects of the nature of a support and the procedure of supporting a cobalt precursor

The conversion of dimethyl disulfide to methanethiol on various catalysts containing supported cobalt sulfide in an atmosphere of hydrogen was studied at atmospheric pressure and T = 190°C. On CoS introduced into the channels of zeolite HSZM-5, the process occurred at a high rate but with a low selectivity for methanethiol because the proton centers of the support participated in a side reaction with the formation of dimethyl sulfide and hydrogen sulfide. Under the action of sulfide catalysts supported onto a carbon support, aluminum oxide, silicon dioxide, and an amorphous aluminosilicate, the decomposition of dimethyl disulfide to methanethiol occurred with 95–100% selectivity. The CoS/Al₂O₃ catalysts were found to be most efficient. The specific activity of alumina-cobalt sulfide catalysts only slightly depended on the phase composition and specific surface area of Al₂O₃. The conditions of the thermal treatment and sulfurization of catalysts and, particularly, the procedure of supporting a cobalt precursor onto the support were of key importance. Catalysts prepared through the stage of supporting nanodispersed cobalt hydroxide were much more active than the catalysts based on supported cobalt salts.     

Dimethyl disulfide conversion into dimethyl sulfide in the presence of sulfidized catalysts

The conversion of dimethyl disulfide in the presence of various supported sulfidized metal-containing catalysts at atmospheric pressure and T = 150−350°C was studied. Sulfidized transition metals supported onto aluminum oxide were more active than catalysts based on a carbon support, silicon dioxide, amorphous aluminosilicate, and zeolite ZSM-5. The most active catalyst was 10% Co/Al₂O₃ prepared with the use of cobalt acetate as an active component precursor and treated with a mixture of hydrogen sulfide with hydrogen at T = 400°C. From kinetic data, it follows that all of the reaction products were formed simultaneously at a temperature of <200°C, whereas a consecutive reaction scheme took place at higher temperatures. In the presence of a sulfidized alumina-cobalt catalyst, the output of dimethyl sulfide was higher than that reached with the use of other well-known catalysts.     

A study on Zn-based catal-sorbents for the simultaneous removal of hydrogen sulfide and ammonia at high temperature

To simultaneously remove hydrogen sulfide and ammonia from hot coal gases, the ammonia decomposition abilities of various metal oxide catalysts were tested in the absence/presence of hydrogen sulfide, at 650 °C. Cobalt oxide, molybdenum oxide, and nickel oxide have high ammonia decomposition abilities (>95%) in the absence of hydrogen sulfide, but such abilities rapidly decreased during the reaction in the presence of hydrogen sulfide. To improve the simultaneous removal abilities of metal oxides, Zn-based catal sorbents were prepared via impregnation with various metals, such as cobalt, nickel, and molybdenum, on zinc oxide. The CZ-30 (promoted with 30 wt% cobalt oxide on zinc oxide) and NZ-30 (promoted with 30 wt% nickel oxide on zinc oxide) catal sorbents showed excellent sulfur removal capacities, which, calculated until the breakthrough point, were 0.35 and 0.39 g S/g catal sorbent, respectively, while MZ-30 promoted with molybdenum showed a low sulfur removal capacity of 0.08 g S/g catal sorbent. The ammonia decomposition ability of CZ-30, however, increased more than 18 times compared with Co₃O₄, whose ammonia decomposition ability was more than 95% until 465 min, even though the ammonia decomposition ability of NZ-30 sharply decreased after 30 min. The CZ catal sorbent is a good candidate for the simultaneous removal of ammonia and hydrogen sulfide.     

Synthesis of Pinenylsulfides from <Emphasis Type="Italic">cis</Emphasis>-Verbenol

The reaction of cis-verbenol with thiols in the presence of ZnCl₂ occurred stereospecifically with substitution of the hydroxyl by a sulfide. __________ Translated from Khimiya Prirodnykh Soedinenii, No. 6, pp. 565–567, November–December, 2005.     

Conversion of anisole in the presence of methanol over AlPO4?Al2O3 catalysts modified with fluoride and sulfate anions

The gas-phase microcatalytic conversion of anisole in the presence of methanol (methanol/anisole molar ratio=4) was studied at temperatures ranging from 523 to 673 K over anion treated (1–3 wt.% F or SO ₄ ^2– ) AlPO₄–Al₂O₃ (25 wt.% Al₂O₃) catalysts. Anisole conversion gave a mixture of dealkylated and C-alkylated products (C-alkylation preferentially in ortho-position) where dealkylation always predominates. The influences of the reaction temperature and both anion type and anion loading upon the conversion of anisole and the selectivities of the products were investigated. The higher increase in surface acidity by fluoride loading increases both the C-alkylation selectivity (mainly to 2-methylanisole) and dealkylation to phenol; so that a lower anisole conversion (smaller pseudokinetic constant) and higher methylanisoles selectivity is found for APAI-P-F catalysts related to unmodified one.     

Para-selectivity of SAPO-5 and mordenite catalysts in the alkylation of cumene with 2-propanol

Alkylation of cumene with 2-propanol was studied on SAPO-5 and mordenite catalysts. The primary products of the alkylation on every catalyst examined here were p- and m-diisopropylbenzene (DIPB) in a ratio of 75:25. The p-DIPB fraction in DIPB isomers (para-selectivity) decreased with increasing yield of DIPB, due to the secondary reaction of p-DIPB to m-DIPB. On SAPO-5, mordenite and silica-alumina, this secondary reaction proceeds through dealkylation of p-DIPB to cumene, followed by re-alkylation of the resultant cumene to m-DIPB. The dealkylation of p-DIPB would occur preferentially over that of m-DIPB. This was due to the higher reactivity of p-DIPB and probably to the reactant molecular shape selectivity of SAPO-5 and mordenite. The para-selectivity was improved by supporting boron oxide on SAPO-5 and mordenite; this improvement was caused by suppression of the secondary dealkylation of p-DIPB.     

Comparing the hydrodesulfurization reaction of thiophene on γ-Al2O3 supported CoMo, NiMo and NiW sulfide catalysts

The thiophene hydrodesulfurization (HDS) reaction on γ-Al₂O₃ supported CoMo, NiMo and NiW sulfide catalysts was compared in order to gain insight into the promoter effect on direct desulfurization (DDS) and hydrogenation (HYD) pathways. Ni-promoted Mo (or W) sulfide catalysts favor the hydrogen transfer reactions relative to CoMo sulfide catalyst, which facilitates the direct route instead. This different performance and also the dependence of the apparent Arrhenius parameters with the catalyst formulation were attributed to the major participation of Mo (or W) edge for the Ni-containing catalysts and S edge for CoMo sulfide catalyst upon the thiophene-HDS reaction.     

Sulfide Catalysts Supported on Al2O3: VI. Synthesis of Catalysts with the Use of Binuclear Molybdenum(V) Complexes with Sulfur-Containing Ligands

A new method was developed for the preparation of sulfide catalysts supported on aluminum oxide. The surface assembling of a direct precursor of the active component was used in this method. The method consists in the sequential immobilization of binuclear molybdenum complexes with S-containing ligands on the support surface followed by the immobilization of nickel (cobalt) compounds at the surface molybdenum complexes. The complexation and structure of the resulting complexes in solution and the structure of surface complexes were studied by ⁹⁵Mo and ¹⁷O NMR, IR, and EXAFS spectroscopy. The surface assembling of a direct precursor of the active component of sulfide hydrodesulfurization catalysts was demonstrated using IR and EXAFS spectroscopy. The activity of the resulting catalysts in a model reaction of thiophene hydrogenolysis was comparable to the activity of sulfide catalysts of the metal complex origin and was much higher than the activity of commercial catalysts and catalysts prepared by impregnation.     

Hydrogenolysis of Dimethyl Disulfide to Methanethiol in the Presence of Cobalt Sulfide Catalysts

The hydrogenolysis of dimethyl disulfide to methanethiol at T = 180–260°C and atmospheric pressure in the presence of supported cobalt sulfide catalysts has been studied. Cobalt sulfide on aluminum oxide exhibits a higher activity than that on a carbon support or silicon dioxide. The maximum reaction rate per gram of a catalyst is observed on an 8% Co/Al₂O₃ catalyst. At temperatures of up to 200°C and conversions up to 90%, methanethiol is formed with nearly 100% selectivity regardless of the cobalt content, whereas the selectivity for methanethiol under more severe conditions decreases because of its condensation to dimethyl sulfide.     

The performance of a Ru?Mo sulfide catalyst for H2S decomposition

A γ-alumina-supported bimetallic Ru-Mo sulfide catalyst preparedvia precipitation from homogeneous solution (PFHS) has been used to effect the abstraction of H₂ from H₂S. The decomposition reaction was also carried out over Al₂O₃-supported RuS₂ and MoS₂ catalysts synthesizedvia PFHS. The performance of bimetallic system exceeded (ca. 40%) the simple additive activities of the constituent monometallic sulfide catalysts and about 2–3 times the individual activities of the monometallic sulfide samples, suggesting chemical synergism between Ru and Mo in the Ru-Mo catalyst. In particular, comparison with other catalysts in the literature showed that specimens preparedvia PFHS exhibited better activities than those from direct sulfidation of the metal oxide. Kinetic study over the Ru-Mo bimetallic sulfide catalyst in a quartz micro-reactor at 110 kPa and between 783–973 K revealed a 1st order dependency on H₂S partial pressure and an activation energy of about 92 kJ mol⁻¹. The irreversible adsorption of H₂S on a coordinatively unsaturated site is thought to be the rate-limiting step.     

Regiospecific hydrogenation of quinolines and indoles in the heterocyclic ring

Quinolines, indoles, acridine, and carbazole were hydrogenated using a large variety of heterogeneous catalysts in hydrocarbon solvents in an effort to achieve selective hydrogenation of the heterocyclic ring. When quinolines were hydrogenated using supported platinum, palladium, rhodium, ruthenium, or nickel metal catalysts in the presence of hydrogen sulfide, carbon disulfide, or carbon monoxide, there was exclusive hydrogenation of the heterocyclic ring to give only 1,2,3,4-tetrahydroquinolines. Use of iridium, rhenium, molybdenum(VI) oxide, tungsten(VI) oxide, chromium(III) oxide, iron(III) oxide, cobalt(II) oxide-molybdenum(VI) oxide, or copper chromite catalysts also caused exclusive hydrogenation of the heterocyclic ring even without addition of sulfur Compounds or carbon monoxide. Hydrogenation of indoles using platinum, rhenium, or, in some cases, nickel catalysts (with or without sulfur Compounds) occurred exclusively in the heterocyclic ring to give indolines, but conversions were affected by indole-indoline equilibria.     

Investigation of the mechanism of catalytic recyclization of furan to thiophene

Investigation of the formation of thiophene from furan and hydrogen sulfide at various catalysts showed that the activity of the catalysts increases with increase in the strength and concentration of Lewis acid centers. It was found by IR spectroscopy that if the degree of coverage of the aluminum oxide surface with hydrogen sulfide is higher than monolayer its dissociative chemisorption does not occur. Mechanism was postulated wich assume that the reaction takes place through stage with the formation of a surface intermediate, including coordination of the α-carbon atoms of the furan ring with the Lewis acid center and with the sulfur atom of molecular hydrogen sulfide.     

Reaction of alkenyldichlorophosphines with ethylene oxide and ethylene sulfide

Conclusions In contrast to ethylane oxide, ethylene sulfide reacts with the styryl- and isobutenyldichlorophosphines only in the presence of catalysts. The course of the discussed reactions is facilitated by solvents with a high electron-donor capacity. The obtained results are discussed from the standpoint of primary donor-acceptor interactions of the reactants.Translated from Izvestiya Akademii Nauk SSSR, Seriya Khimicheskaya, No. 2, pp. 457–461, February, 1976.     

Propane formation by aqueous-phase reforming of glycerol over Pt/H-ZSM5 catalysts

Solid acid supports such as H-ZSM5, H-Mordenite, γ-Al₂O₃, USY and Beta catalysts were modified with Pt. These Pt/oxide catalysts were found to be active for propane formation through aqueous reforming of glycerol in the presence of hydrogen. The reforming reactions, possibly, proceeded through reaction cycles of dehydration on acid sites and hydrogenation on Pt sites over the catalysts.     

Liquid-phase hydrogenation of thiophenes on palladium sulfide catalysts

Palladium sulfide catalysts are active for the hydrogenation of thiophenes of different structure in hydrocarbons at 22O-30O‡C and 3.0-9.5 MPa. Thiophenes and benzothiophenes are close in reactivity. An increase in palladium sulfide concentration in the catalyst leads to an increase in the reaction rate per 1 g of the catalyst but has only a slight effect on the specific reaction rate of hydrogenation calculated per 1 g of Pd. The specific activity of palladium sulfide supported on aluminosilicate is one order of magnitude higher than that of PdS without a support and the catalysts supported on the aluminum oxide and carbon. The aluminosilicate-supported catalyst is also more selective.     

Effect of alkali metal additives on the activity and selectivity of structured silver catalysts in epoxidation of ethylene by nitrogen(I) oxide

We have shown that introducing Cs, K, or Na additives into the composition of silver catalysts (supported on ceramic honeycomb monoliths) for epoxidation of ethylene by nitrogen(I) oxide leads to an increase in the yield of the target product (ethylene oxide) by a factor of 1.5–2, while the presence of lithium in the composition of the composites inhibits the process. The optimal content of alkali promoters in the composition of the catalysts decreases in the series Na, K, Cs antibatically relative to the ionic radii of the elements. __________ Translated from Teoreticheskaya i éksperimental’naya Khimiya, Vol. 41, No. 6, pp. 360–363, November–December, 2005.     

A selective and direct synthesis of 2-bromo-4-alkylthiophenes: Convenient and straightforward approaches for the synthesis of head-to-tail (HT) and tail-to-tail (TT) dihexyl-2,2′-bithiophenes

A straightforward method for the synthesis of 2-bromo-4-alkylthiophenes was developed, and the desired products were obtained in the highest chemical yields (>90%) reported to date. 2-Bromo-4-alkylthiophenes were synthesized by regioselective lithiating of 3-alkylthiophenes with n-BuLi and quenching with bromine at −78 °C. Moreover, a simple and efficient protocol for the synthesis of dihexyl-2,2′-bithiophenes was developed by employing 2-bromo-4-hexylthiophene instead of the commonly used monomer, 2-bromo-3-hexylthiophene. Kumada and Suzuki cross-coupling reactions were conducted to synthesize the desired products as head-to-tail (HT) and tail-to-tail (TT) regioisomers in high yields and excellent selectivity.     

FT-IR Study of Carbon Nanotube Supported Co-Mo Catalysts

In this paper, adsorption properties of dibenzothiophene (DBT) on carbon nanotube, carbonnanotube supported oxide state and sulfide state CoMo catalysts are studied by using thermal gravi-metric analysis (TGA) technique and FT-IR spectroscopy. Activated carbon support, 7-A1203 supportand supported CoMo catalysts are also subjected to studies for comparison. It was found that sulfidestate CoMoS/MWCNT, CoMoS/AC and CoMoS/γ-A12O3 catalysts adsorbed much more DBT moleculesthan their corresponding oxide state catalysts, as well as their corresponding supports. The chemicallyadsorbed DBT aromatic molecules did not undergo decomposition on the surface of supports, supportedoxide state CoMo catalysts and sulfide state CoMo catalysts when out-gassing at 373 K. FT-IR results indicated that DBT molecules mainly stand upright on the active sites (acid sites and/or transition active phases) of CoMoS/MWCNT catalyst. However, DBT aromatic molecules mainly lie flat on MWCNT and CoMoO/MWCNT.