02862nas a2200277 4500008004100000022001400041245010000055210006900155260009900224300001200323490000700335520195800342653002002300653000802320653001502328653001502343653001602358653001202374653000902386653001502395653001102410100001502421700001702436700001302453856011802466 2005 eng d a0140-700700aPerformance assessment of HC-290 as a drop-in substitute to HCFC-22 in a window air conditioner0 aPerformance assessment of HC290 as a dropin substitute to HCFC22 aTHE BOULEVARD, LANGFORD LANE, KIDLINGTON, OXFORD OX5 1GB, OXON, ENGLANDbELSEVIER SCI LTDcJUN a594-6040 v283 a

As per the Montreal Protocol, CFCs and HCFCs are being phased out. HCFC-22 is used in window air conditioners. This paper presents the experimental performance study of a window air conditioner with propane (HC-290), a natural refrigerant, as a drop-in substitute to HCFC-22. Experimental results showed that HC-290 had 6.6% lower cooling capacity for the lower operating conditions and 9.7% lower for the higher operating conditions with respect to HCFC-22. The coefficient of performance for HC290 was 7.9% higher for the lower operating conditions and 2.8% higher for the higher operating conditions. The energy consumption of the unit with HC-290 was lower in the range 12.4-13.5% than HCFC-22. The discharge pressures for HC-290 were lower in the range 13.7-18.2% than HCFC-22. For HC-290, the pressure drop was lower than HCFC-22 in both heat exchangers. This paper also presents simulation results for the heat exchangers of an HCFC-22 window air conditioner with HC-290 as a drop-in substitute. The simulation has been carried out using EVAP-COND, a heat exchanger model developed by NIST [National Institute of Standards and Technology. EVAP-COND: simulation models for finned-tube heat exchangers, Maryland, USA (2003). http://www2.bfrl.nist.gov/software/evap-cond/ [18]]. The simulated evaporator capacities are within +/- 4% of the experimentally measured cooling capacities for both refrigerants. Simulation results for HC-290 and HCFC-22 are compared. The exit temperatures of HC-290 are lower by 0.3-1.2 degrees C in the condenser and are higher by 2.1-2.4 degrees C in the evaporator than HCFC-22. Evaporating pressures of HC-290 are lower by 2.1-3.3% as compared to HCFC-22. The pressure drops of HC-290 are lower in both the evaporator and the condenser as compared to HCFC-22. The outlet temperatures of air for HCFC-22 and HC-290 in both heat exchangers are nearly the same. (c) 2005 Elsevier Ltd and IIR. All rights reserved.

10aair conditioner10aCOP10aEvaporator10aexperiment10aperformance10apropane10aR-2210asimulation10awindow1 aDevotta, S1 aPadalkar, AS1 aSane, NK uhttps://library.ncl.res.in/content/performance-assessment-hc-290-drop-substitute-hcfc-22-window-air-conditioner-102227nas a2200349 4500008004100000022001400041245015800055210006900213260000800282300001200290490000700302520101400309653002601323653001401349653002201363653001701385653002401402653002301426653002801449653002801477653002301505653002501528653003301553653002501586653001501611653003901626653001301665100002201678700002101700700001901721856013701740 2017 eng d a0019-450600aStudy of the effect of operating parameters on the extractive distillation of isopropyl alcohol–water mixture using dimethyl sulphoxide as an entrainer0 aStudy of the effect of operating parameters on the extractive di cMAY a141-1610 v603 a

Abstract: In this paper, the simulation analysis of separation of isopropyl alcohol (IPA)–water via extractive distillation by using dimethyl sulphoxide as an entrainer is presented. The steady-state simulation for this process was done using Aspen Plus simulator. The aim of this work is to study the effect of various operating parameters such as number of stages, molar reflux ratio, binary feed stage number, entrainer feed stage number, temperature of entrainer feed and entrainer to feed molar ratio on the purity and energy consumption. The sensitivity of these parameters serves as a basis to choose the optimum operating conditions to maximize the IPA purity and minimize the energy requirement. In this analysis, among various operating parameters, those which directly affect the IPA purity and the parameters which affect the reboiler duty, for the given separation task, are identified. Simulation results with optimum operating conditions and their economic analysis are also presented.

10aAspen Plus Simulators10aAzeotrope10aComputer software10aDistillation10aEnergy requirements10aEnergy utilization10aExtractive distillation10aIsopropyl alcohol/water10aIsopropyl alcohols10aOperating parameters10aOptimum operating conditions10aSensitivity analysis10asimulation10aSimulationSteady-state simulations10aSolvents1 aGhuge, Pravin, D.1 aMali, Nilesh, A.1 aSirsam, R., S. uhttps://library.ncl.res.in/content/study-effect-operating-parameters-extractive-distillation-isopropyl-alcohol%E2%80%93water-mixture01804nas a2200229 4500008004100000022001400041245008600055210006900141260000800210300001200218490000700230520107600237653001701313653002101330653001201351653001501363653002201378100001701400700001701417700002601434856011401460 2017 eng d a0256-249900aStudy of thermally coupled distillation systems for energy-efficient distillation0 aStudy of thermally coupled distillation systems for energyeffici cJAN a119-1280 v423 a

Distillation is one of the most widely used separation unit operations in process industries, although it is quite energy intensive. In many cases, the enormous energy requirements for distillation make it economically infeasible to carry out the separation. Thermally coupled distillation system (TCDS) is an advanced distillation method that provides significant energy savings of about 30% as compared with conventional distillation column sequences. The most well-known TCDS sequence, the Petlyuk configuration, has some operational challenges due to bidirectional vapour flow, which makes its implementation difficult in two-column mode. To overcome these limitations, a number of unidirectional vapour flow configurations have been proposed in the literature. The work on simulation analysis for such configurations is limited. In this paper, simulation models for two such configurations are developed, analyzed and compared with the Petlyuk and conventional distillation column sequences for separation of equimolar mixture of benzene-toluene-ethylbenzene.

10aDistillation10aenergy efficient10aPetlyuk10asimulation10athermally coupled1 aSaxena, Neha1 aMali, Nilesh1 aSatpute, Satchidanand uhttps://library.ncl.res.in/content/study-thermally-coupled-distillation-systems-energy-efficient-distillation02344nas a2200289 4500008004100000022001400041245008000055210006900135260000900204300001100213490000800224520144400232653002501676653003301701653001501734653001201749100002301761700002201784700002101806700001901827700002101846700002101867700001701888700002201905700002101927856010601948 2021 eng d a0959-652600aEnergy and life cycle impact assessment for xylitol production from corncob0 aEnergy and life cycle impact assessment for xylitol production f cJAN  a1232170 v2783 a

The conversion of biobased feedstocks into energy and value-added chemicals is one main approach to address the current global challenge for waste mitigation through the biorefinery mode. Corncob biomass which is one of the most abundant agricultural residue in India with a high hemicellulose content, can serve as a potential low-cost raw material for food-grade xylitol production. The present study demonstrates a process for xylitol production from corncob biomass with detailed energy and life cycle analysis for viability assessment. The major highlight of the process is the use of microbial fermentation, where biomass-derived D-xylose is converted to xylitol with high selectivity. Overall, 0.502 kg of xylitol crystals could be produced from 3.5 kg of corncob biomass. Simulation analysis revealed that the evaporators are the primary consumers of energy, and the process of heat integration can significantly reduce the energy requirements of the overall process. Environmental impacts of the system evaluated showed emission results of 8.68 kg CO2 equivalent and revealed that marine aquatic and freshwater eco-toxicity are the only possible contributors to the environment. The results suggest that the process would have favourable energy balances, which can be used in pilot plant and heat exchanger network design and operation for xylitol production scale up to 500 L. (C) 2020 Elsevier Ltd. All rights reserved.

10abiomass valorization10aLife cycle impact assessment10asimulation10axylitol1 aDasgupta, Diptarka1 aSidana, Arushdeep1 aGhosh, Prasenjit1 aSharma, Tripti1 aSingh, Jasvinder1 aPrabhune, Asmita1 aMore, Snehal1 aBhaskar, Thallada1 aGhosh, Debashish uhttps://library.ncl.res.in/content/energy-and-life-cycle-impact-assessment-xylitol-production-corncob02210nas a2200265 4500008004100000022001400041245011100055210006900166260000800235300001400243490000700257520132700264653001501591653003001606653002601636653001401662653001501676100002601691700002001717700002501737700001801762700001901780700001701799856012801816 2022 eng d a0268-257500aMechanistic modeling of continuous capture step purification of biosimilar monoclonal antibody therapeutic0 aMechanistic modeling of continuous capture step purification of  cSEP a2404-24190 v973 a

{BACKGROUND Continuous multicolumn Protein A chromatography offers various advantages for capture stage purification of monoclonal antibody therapeutics, like higher productivity and resin capacity utilization, lower buffer consumption, small footprint, etc. Due to the complexity of the continuous process, experimental optimization is time-consuming and cost-intensive. This investigation proposes a hybrid process development approach integrating experimental and mechanistic modeling for time- and cost-effective development and optimization of continuous Protein A affinity chromatography. RESULTS Productivity and capacity utilization of the continuous CaptureSMB process under varying operating conditions were predicted using the Chromatography Analysis and Design Toolkit (CADET) framework and validated with experimental results. Effects of critical process parameters like feed concentration (c(0)), loading breakthrough (s) and residence time (RT) on productivity and capacity utilization were evaluated. Model predictions were validated using the experimental results proving the reliability and feasibility of the modeling approach. At 15.00 +/- 0.20 mg mL(-1) feed model mAb concentration, the model-based approach predicted the best performance giving 27.56 g L-1 h(-1) productivity (RT = 2 min

10aCaptureSMB10acontinuous chromatography10aMathematical modeling10aProtein A10asimulation1 aDeulgaonkar, Prashant1 aBhambure, Rahul1 aPrasad, Bhaskarjyoti1 aMishra, Ashok1 aTiwari, Sanjay1 aMody, Rustom uhttps://library.ncl.res.in/content/mechanistic-modeling-continuous-capture-step-purification-biosimilar-monoclonal-antibody02181nas a2200241 4500008004100000022001400041245008200055210006900137260000800206300001600214490000700230520143400237653002001671653001001691653000901701653002801710653001101738653001501749100001501764700002101779700002701800856011201827 2022 eng d a0360-319900aOptimization of Liquid Organic Hydrogen Carrier (LOHC) dehydrogenation system0 aOptimization of Liquid Organic Hydrogen Carrier LOHC dehydrogena cAUG a28530-285470 v473 a

In this paper, the perhydrodibenzyltoluene dehydrogenation flowsheet has been simulated. Modelling of the dehydrogenation reactor has been performed using the 1-D model. External and internal mass transfer resistances are also considered. Non-isothermal pellet condition has been considered for simulating the dehydrogenation reactor. The flowsheet simulation has been carried out in DW-Sim v 6.5.2 integrated with the reactor model coded in Python. NET. The dehydrogenation reactor is operated at a feed temperature between 523 K -613 K, a wall temperature of 623 K and 653 K, and a reactor pressure maintained at 1.2 atm. The amount of catalyst required for the perhydrodibenzyltoluene (PDBT) dehy-drogenation reactor is evaluated such that the conversion reaches 99%. The process flowsheet has been simulated to produce 10 Nm(3)/hr of industrial-grade hydrogen. The effects of feed temperature, wall temperature, and hydrogen burner efficiency on various system requirements, including catalyst weight, energy supplied to the dehydrogenation reactor, areas of the heat exchanger, and hydrogen production from the reactor, have been discussed. Preliminary cost optimization based on the heat exchangers and catalyst at various feed temperatures, reactor wall temperature, and hydrogen burner efficiency has been carried out. (C) 2022 Hydrogen Energy Publications LLC. Published by Elsevier Ltd. All rights reserved.

10aDehydrogenation10aDWSim10aLOHC10aPerhydrodibenzyltoluene10aPython10asimulation1 aRao, Nihal1 aLele, Ashish, K.1 aPatwardhan, Ashwin, W. uhttps://library.ncl.res.in/content/optimization-liquid-organic-hydrogen-carrier-lohc-dehydrogenation-system