02407nas a2200289 4500008004100000020002200041022001400063245010400077210006900181260019400250300001200444490000900456520127500465653002101740653003301761653002101794653001901815653001801834100002501852700002801877700001901905700002701924700001501951700001201966700001201978856012701990 2010 eng d a978-0-7354-0854-8 a0094-243X00aDynamic modeling of hydro- formylation of 1-decene on Rh/C catalyst in bubble colunm slurry reactor0 aDynamic modeling of hydro formylation of 1decene on RhC catalyst a2 Huntington Quadrangle, STE 1NO1, Melville, NY 11747-4501 USAbNatl Inst Technol Durgapur; SERC, Dept Sci & Technol; Caledonian Coll Engn; BRNS, Dept Atom Energy; DRDO, Minist DefencecOCT a143-1500 v12983 a

A dynamic model has been developed for the bubble column slurry reactor operating under non-isothermal conditions. The model consists of mass and heat balance equations for the gas and liquid phases and the catalyst particle. The model equations consisted of partial differential equations (PDE) which were converted to ordinary differential equations (ODE) by using finite difference relationships for the spatial derivatives and the ordinary differential equations for the time derivatives (Numerical Method of Lines-NMoL). The model was applied to describe the dynamic behaviour of bubble column slurry reactor during the hydroformylation of 1-decene on Rh/C catalyst. Model simulations were performed to obtain a meaningful path to steady state and to reproduce the other characteristics of the dynamic behaviour of the reactor. Under given conditions, the reaction required approximately 3750 seconds to reach the steady state concentrations at various reactor positions. It was observed with increase in the fluid velocities, the dynamics of the system was altered to 2500 seconds to reach the steady state condition. The effect of axial dispersion on the substrate concentration and the temperature rise along the reactor was further studied and discussed.

10aaxial dispersion10abubble column slurry reactor10aDynamic modeling10amethod of line10aPDE solutions1 aUpkare, Makarand, M.1 aRajurkar, Kalpendra, B.1 aDas, Samir, K.1 aJaganathan, Rengaswamy1 aParuya, S.1 aKar, S.1 aRoy, S. uhttps://library.ncl.res.in/content/dynamic-modeling-hydro-formylation-1-decene-rhc-catalyst-bubble-colunm-slurry-reactor-002531nas a2200169 4500008004100000020002100041022002000062245003200082210003100114260002000145300001200165520206900177100001702246700001202263700001902275856006702294 2016 eng d a978-111811576-3  a978-111924849-100aThree-phase slurry reactors0 aThreephase slurry reactors bWiley Blackwell a132-1553 a

Many of the chemical reactors employed in various sectors of the process andchemical industries, suchas petroleumrefining,downstream processing and petrochemicals, bulk and specialty chemicals, and pharmaceuticals, involve reactants and products in three phases. The ubiquitous presence of three-phase reactors comes from the fact that many of the reactants are liquids under reaction conditions, to be treated with a gas like hydrogen, and in the presence of a heterogeneous catalyst that is usually a solid. This requirement leads to two broad modes of contacting one in which the catalyst is held stationary in a "fixed" or a "packed bed" and one in which the catalyst is set free to move, along with the flowing fluid phases, during their sojourn through the reactor vessel.The choice ofwhether the catalyst should be fixed ormoving is usually dictated by the relative dominance of transport rates and intrinsic kinetics. If the reaction chemistry is intrinsically slow (when external and internalmass transfer of chemical species from the fluid phases to the porous catalyst is not rate limiting), packed bed reactor that allows very high catalyst loading is usually preferred. Packed beds, however, do not constitute the main topic of discussion in this monograph. Still, three-phase packed beds and slurry reactors are really parts of the same continuum of three-phase catalytic reactors andhave beendiscussedcomprehensively about three decades back in the classic book by P.A. Ramachandran and R.V. Chaudhari (Three Phase Catalytic Reactors. NewYork:Gordon and Breach Science Publishers; 1983). The same authors published earlier a review of three-phase slurry reactors (Chaudhari RV, Ramachandran PA. Three phase slurry reactors. AIChE J. 1980;26(2):177-199). This chapter builds on these authors' works and attempts to update the reader on developments in the field over the past few decades while retaining the essential reactionandreactorengineering aspects.The focus isonthe design, scale-up, and operation of three-phase slurry reactor systems

1 aBuwa, V., V.1 aRoy, S.1 aRanade, V., V. uhttps://library.ncl.res.in/content/three-phase-slurry-reactors01022nas a2200169 4500008004100000245009000041210006900131260002900200520038400229100001800613700001200631700002100643700001400664700001900678700003000697856012500727 2017 eng d00aOFET based H2S gas sensing among reducing and mining gases using green synthesis SnO20 aOFET based H2S gas sensing among reducing and mining gases using aMumbai, IndiabIEEEcJAN3 aIn this paper we present detection of H2S gas using an organic field effect transistor (OFET) based sensor. A low-cost green synthesis process for SnO2 nanoparticles and bi-layer approach for device fabrication have been adopted to come up with the sensor. With the help of multiparameteric analysis, selectivity towards H2S gas was proved among other reducing and mining gases. 1 aSurya, S., G.1 aRoy, S.1 aGanne, B., S. P.1 aPasam, D.1 aSastry, A., B.1 aPrasad, Bhagavatula L. V. uhttps://library.ncl.res.in/content/ofet-based-h2s-gas-sensing-among-reducing-and-mining-gases-using-green-synthesis-sno201242nas a2200193 4500008004100000022001400041245014600055210006900201260000800270300001200278520049600290653002100786653002100807653002600828653003000854653002200884100001200906856013000918 2019 eng d a1434-193X00aUnusual route to synthesize indolizines through a domino SN2/michael addition reaction between 2‐mercaptopyridine and nitroallylic acetates0 aUnusual route to synthesize indolizines through a domino SN2mich cJAN a765-7693 a

A straightforward synthesis of indolizines has been demonstrated from the reaction of 2‐mercaptopyridine and nitroallylic acetates in the presence of a base. The products were obtained in good isolated yield under relatively mild reaction conditions. The mechanistic insight of the reaction has been revealed by performing some control experiments demonstrating that the reaction is initiated by a sequential SN2/Michael addition reaction followed by removal of the sulfur moiety.

10adomino reactions10aMichael addition10anitrogen heterocycles10anucleophilic substitution10asynthetic methods1 aRoy, S. uhttps://library.ncl.res.in/content/unusual-route-synthesize-indolizines-through-domino-sn2michael-addition-reaction-between-2