Preparation, Proximate Composition and Culinary Properties of Yellow Alkaline Noodles from Wheat and Raw/Pregelatinized Gadung (Dioscorea Hispida Dennst) Composite Flours

The steady increase of wheat flour price and noodle consumptions has driven researchers to find substitutes for wheat flour in the noodle making process. In this work, yellow alkaline noodles were prepared from composite flours comprising wheat and raw/pregelatinized gadung (Dioscorea hispida Dennst) flours. The purpose of this work was to investigate the effect of composite flour compositions on the cooking properties (cooking yield, cooking loss and swelling index) of yellow alkaline noodle. In addition, the sensory test and nutrition content of the yellow alkaline noodle were also evaluated for further recommendation. The experimental results showed that a good quality yellow alkaline noodle can be prepared from composite flour containing 20% w/w raw gadung flour. The cooking yield, cooking loss and swelling index of this noodle were 10.32 g, 1.20 and 2.30, respectively. Another good quality yellow alkaline noodle can be made from composite flour containing 40% w/w pregelatinized gadung flour. This noodle had cooking yield 8.93 g, cooking loss 1.20, and swelling index of 1.88. The sensory evaluation suggested that although the color, aroma and firmness of the noodles were significantly different (p ≤ 0.05) from wheat flour noodle, but their flavor remained closely similar. The nutrition content of the noodles also satisfied the Indonesian National Standard for noodle. Therefore, it can be concluded that wheat and raw/pregelatinized gadung composite flours can be used to manufacture yellow alkaline noodle with good quality and suitable for functional food

Development of a new computer model for the simulation of cooking organic aerosol formation from heated cooking oils using aspen plus

Cooking is an important source of particulate matter with adverse effects on human health, particularly in developing countries where simple stoves burning biomass (wood, animal dung, and crop waste) and coal are used [1]. Depending on the components of the food, the composition of cooking organic aerosol (COA) may vary drastically. However, due to loss of volatile organic compounds (VOC) during experiments and numbers of other uncertainties, the exact compositions and rates of COA formation are difficult to be determined. In this thesis, a simulation model for heating corn, soybean and sunflower oils and stir-frying myrcia was developed using Aspen Plus

Supercritical carbon dioxide extraction of lipids from Pythium irregulare

Lipids that contain polyunsaturated fatty acids (PUFA) have therapeutic value. Supercritical carbon dioxide extraction of PUFA from the lower fungi, Pythium irregulare was attempted for freeze-dried material in the presence of an aqueous phase. Extraction showed some success at moisture contents up to 30% (wb) and with the addition of a novel CO2 -philic surfactant. Equilibrium and kinetic data are presented. Equilibrium data were taken for the fungal oil in a flow-through apparatus at a low flow rate for two isotherms (40 and 60°C) over a pressure range of 13.7 to 27.5 MPa. Equilibrium data were also taken for pure naphthalene at 40°C to test the system. The compressed-gas model utilizing the Peng-Robinson equation of state was then applied to the data. The kinetic data portrayed three types of mass transfer behavior including an initial surface-film regime where pseudo steady-state conditions prevailed, a diffusion-controlled regime where unsteady-state conditions were evident and a temporary transition region. For tests with extraction times of 5 to 6 hours, data for the diffusion-controlled region were modeled with an analytical solution to Fick\u27s Second Law assuming the particles were spherical shaped. The models worked well for both equilibrium and kinetic data, however the physical property values for the equilibrium data were altered substantially to obtain a reasonable fit with the compressed-gas model

Equilibrium, extraction and fractionation of oil and phenolic compounds from coffee with supercritical carbon dioxide and ethanol

Orientadores: Antonio José de Almeida Meirelles, Fernando Antonio CabralTese (doutorado) - Universidade Estadual de Campinas, Faculdade de Engenharia de AlimentosResumo: Esse projeto objetivou obter dados de solubilidade de compostos fenólicos e óleo de café em dióxido de carbono supercrítico (scCO2) na presença de cossolventes, ajustar parâmetros de modelos termodinâmicos para descrever estes dados e, posteriormente, avaliar a extração e fracionamento dessas substâncias, que se destacam por seu alto valor agregado e por sua diversidade de aplicações em diferentes ramos industriais, a partir do resíduo da produção de café solúvel. As determinações experimentais de solubilidade dos ácidos cafeico e ferúlico e do óleo de café verde foram realizadas em diferentes condições de temperatura (313 a 333 K) e pressão (20 a 40 MPa), e as quantidades de cossolvente (etanol e/ou água) adicionadas ao scCO2 variaram de 0 a 10 mol%. No geral, os maiores valores de solubilidade foram obtidos nas maiores condições de pressão. Ao se adicionar aproximadamente 10 mol% de etanol ao scCO2, verificou-se aumento de 120 e 30000 vezes na solubilidade dos ácidos ferúlico e cafeico, respectivamente. Os dados experimentais dos sistemas binários foram bem representados pelas equações de Peng-Robinson, Soave-Redlich-Kwong e Cubic Plus Association (CPA). Porém, apenas a equação CPA foi capaz de predizer satisfatoriamente os dados de equilíbrio dos sistemas ternários e/ou quaternários a partir dos parâmetros de interação binária, pois, diferentemente das equações de estado cúbicas, este modelo considera as fortes interações, como ligações de hidrogênio, que ocorrem entre as moléculas do soluto e do cossolvente. A solubilidade do óleo de café verde em scCO2 mostrou-se similar à de diversos outros óleos vegetais. Ela aumentou cerca de 60% com a adição de 2,3 % (em massa) de etanol, e as amostras obtidas mostraram-se mais concentradas em ácidos graxos livres e diterpenos em relação ao óleo obtido por prensagem. Extrações com fluido supercrítico (Supercritical Fluid Extraction - SFE) e líquido pressurizado (Pressurized Liquid Extraction - PLE) em uma ou duas etapas e usando apenas dióxido de carbono e etanol como solventes foram avaliadas para obtenção de compostos fenólicos e lipídicos da borra de café. Os maiores rendimento global de extração, concentração de compostos fenólicos e taxa de extração foram verificados quando o etanol foi utilizado como solvente (extrato E). O fracionamento de E, tanto por um processo integrado de SFE + PLE ou usando o scCO2 como antissolvente por meio de quatro separadores em série, forneceu frações aproximadamente quatro vezes mais concentradas que o extrato etanólico obtido em etapa única. Contudo, o uso de cossolventes, principalmente etanol, mostrou-se fundamental para extração de compostos fenólicos por consequência do aumento da sua solubilidade em scCO2. O conhecimento da solubilidade de solutos em scCO2 + cossolventes e de como alguns parâmetros, como temperatura, pressão e tipo e concentração de cossolvente a influenciam pode ser útil para otimizar processos de separação que utilizam o scCO2 como solvente ou antissolventeAbstract: This work proposed to obtain solubility data of phenolic compounds and green coffee oil in supercritical carbon dioxide (scCO2) with cosolvents, to describe these data through thermodynamic models, and posteriorly to evaluate the extraction and fractionation of compounds from the residue of soluble coffee production. These substances are highlighted by their high value added and its diversity of applications in different industrial sectors. Experimental measurements of solubility of caffeic and ferulic acids and green coffee oil were performed at different temperatures (313 to 333 K) and pressures (20 to 40 MPa), and the amounts of cosolvent (ethanol and/or water) added to scCO2 ranged from 0 to 10 mol%. In general, the highest solubility values were obtained under the highest pressure conditions. By adding approximately 10 mol% of ethanol to scCO2, it was verified an increase up to 120 and 30,000 times on the solubility of ferulic and caffeic acids, respectively. Experimental data of the binary systems were well described by the equations of Peng-Robinson, Soave-Redlich-Kwong and Cubic Plus Association (CPA). However, CPA equation was the only one suitable to predict the equilibrium data of the ternary and/or quaternary systems from the binary interaction parameters, because unlike the cubic state equations this model describes the strong interactions, such as hydrogen bonds, that occur between the solute and cosolvent molecules. Solubility data of green coffee oil in scCO2 was similar to several other vegetable oils. It increased by up to 60% with the addition of 2.3% ethanol (w/w), and the samples obtained were more concentrated in free fatty acids and diterpenes in comparison with oil obtained by pressing. Supercritical fluid extraction (SFE) and pressurized liquid extraction (PLE) in one or two steps and using CO2 and ethanol as solvents were evaluated to extract phenolic and lipid compounds from spent coffee grounds. The highest overall extraction yield, total phenolic content and extraction rate were verified when ethanol was used as a solvent (extract E). The fractionation of E, either by an integrated process with SFE + PLE or by using scCO2 as antisolvent through four separators in series, favors obtaining fractions approximately four times more concentrated than the single-stage ethanolic extract. Therefore, the use of cosolvents, mainly ethanol, confirms to be crucial for the extraction of phenolic compounds, due to the increase of its solubility in scCO2. In addition, knowledge on the effect of the parameters, such as temperature, pressure and type and cosolvents concentration, on the solubility of solutes in scCO2 + cosolvents can be useful to optimize separation processes using scCO2 as solvent or antisolventDoutoradoEngenharia de AlimentosDoutora em Engenharia de Alimentos140345/2014-0CNP

Intensification of polyester synthesis by continuous reactive distillation

The thesis starts with a brief overview of unsaturated polyesters. In particular, the usage of raw materials, the application of unsaturated polyester resins, and, the worldwide supply and demand of the unsaturated polyester resins are discussed. Unsaturated polyester is traditionally produced in a batch-wise-operating reaction vessel connected to a distillation unit. The total production time is around 12 hours and often leads to batch-to-batch inconsistency. Process intensification is required for the unsaturated polyester process to reduce the production time and to achieve a better quality of the product. An attractive alternative to batch-wise polyester production is reactive distillation. In chapter 1, the attractiveness of reactive distillation for the synthesis of unsaturated polyester is discussed. The goal of the thesis is to develop and evaluate a reactive distillation process for the production of unsaturated polyester from anhydrides and glycols. To accurately predict the behavior of reactive distillation process, reliable kinetic and thermodynamic models are required. Therefore, in chapter 2 a dynamic model for a batch-wise operating reaction vessel connected to a flash separation unit is developed in order to validate the kinetic and thermodynamic models and their parameters. This model includes kinetics, description of the change of rate order during the reaction, the polymer NRTL non-ideal thermodynamic model based on non-random theory of liquid (NRTL) and mass balances. The reaction between maleic anhydride and propylene glycol has been taken as a case study. The reaction scheme is complex and the proposed model takes four types of reactions into account; ring opening, polyesterfication, isomerization and saturation reactions. The acid value of the polyester, number-average molecular weight, distilled mass and glycol concentration in the distillate have been subsequently used to validate the model and the model predicts these important variables reliably. The process description is improved by using the vapor liquid equilibrium data predicted from the polymer NRTL model. After successful validation of the kinetic and thermodynamic models, the feasibility of the reactive distillation process for the unsaturated polyester is presented in chapter 3. Moreover, the simulation results of reactive distillation model are compared with the batch reactor model simulation results to determine advantages gained by the reactive distillation over the traditional batch process. The simulation study shows that the total production time of polyester in a continuous reactive distillation system is reduced to 1.8-2 hours compared to the12 hours of the industrial batch reactor process. The model demonstrated that reactive distillation has the potential to intensify the process by factor of 6 to 8 in comparison to the batch reactor process. After finding that reactive distillation is an attractive alternative for the polyesters synthesis, a more in depth analysis is performed. Particularly, the influence of the liquid back mixing on the description of the reactive distillation process, product transition time, the amount of undesired product formation during the product changeover is investigated. Since the current state of the art modelling approach does not account for liquid back mixing, the rate-based model is extended to account for liquid back mixing. The simulation results of extended rate-based model demonstrated that axial dispersion significantly influences the reactive distillation process and cannot be neglected. On the basis of current research work and literature review, a novel design methodology for the economical and technical evaluation of reactive distillation is proposed in chapter 4. Moreover, the applicability of various design methods for reactive distillation is discussed. The proposed framework for the economical evaluation determines the boundary conditions (e.g. relative volatilities, target purities, equilibrium conversion and equipment restriction), checks the integrated process constrains, evaluates economical feasibility, and provides guidelines to any potential reactive distillation process application. Providing that a reactive distillation process is economically attractive, a technical evaluation is performed afterward in order to determine the technical feasibility, the process limitations, working regime and requirements for internals as well as the models needed for reactive distillation. This approach is based on dimensionless numbers such as Damkohler and Hatta numbers, as well as the kinetic, thermodynamic and mass transfer limits. The proposed framework for economical and technical evaluation of reactive distillation allows a quick and easy feasibility analysis for a wide range of chemical processes. Several industrial relevant case studies (synthesis of di-methyl carbonate (DMC), methyl acetate hydrolysis, toluene hydro-dealkylation (HDA) process, fatty acid methyl esters (FAME) process and unsaturated polyesters synthesis) are used to illustrate the validity of the proposed framework. In chapter 4, it is found that the bubble column is the potential device for producing unsaturated polyesters by the reactive distillation. Moreover, the introduction of packing or partition trays in the bubble column significantly improves the unsaturated polyester process because packing or partition trays provide a better mass transfer and the multi-stage effect in the column. But considering the lack of information about the behavior of counter-currently operated bubble columns in the presence of structured packing or partition trays and in a viscous system, a systematic investigation on the gas holdup, axial dispersion and mass transfer in the packed bubble column and the trayed bubble column is undertaken in chapter 5. Four different types of structured packings (Super-Pak, Flexipac, Mellapak and Gauze) and two types of perforated partition trays (with 25% and 40% tray open area) are used to characterize the packed and trayed bubble column, respectively. It is observed that the packed and trayed bubble columns improve the gas holdup and mass transfer compared to the empty bubble column and reduces the axial dispersion significantly. Particularly, the Gauze packing improves the gas holdup and mass transfer and, sufficiently reduces the axial dispersion. In contrast, Super-Pak offers only a modest improvement because of its open structure. Comparison of the experimental data of the packed and trayed bubble column indicates that the partition trays improve the bubble column in the same order as packing. The gas holdup, axial dispersion and mass transfer depend more strongly on the gas velocity compared to the liquid velocity. The liquid viscosity also significantly influences these parameters and therefore the empirical correlations obtained from the air-water system cannot be applied for the viscous system. Moreover, experimental data of the packed, trayed and empty bubble column are correlated by dimensionless numbers. Empirical correlations for the gas holdup, Bodenstein number (for the axial dispersion coefficient) and Stanton number (for the volumetric mass transfer coefficient) as a function of the Froude and Gallilei dimensionless numbers are proposed. In chapter 6, an experimental pilot plant validation of the reactive distillation process for the polyester synthesis is presented. Two different configurations are investigated: 1) a reactive distillation column and 2) a reactive distillation column coupled with a pre-reactor. Due to a relatively short residence time of 0.32 hours and an operating temperature of 190oC in case of the first configuration, a maximum conversion of 37% was achieved; which indicates monoester formation in the reactive distillation column. In the case of the second configuration, a 90% conversion is achieved within 0.55 hours at a temperature of 250oC in the reactive distillation column coupled with a pre-reactor; which confirms the polyester formation in the reactive distillation column. The extended rate-based model developed in chapter 3 is used to simulate the pilot reactive distillation column. The model predicted the experimental data (acid value, conversion, isomerization and saturation fraction, number-average molecular weight, the degree of polymerization and water fraction in the distillate) adequately (5-22%). Moreover, the product specifications of the polyester produced at 250oC in the reactive distillation column is in the range of polyesters produced in the traditional industrial batch reactor setup. Furthermore, discoloration of the polyester was hardly noticed even though the column was operated at 250oC. Finally in chapter 7, the validated model is used to find the best suitable internal and feed configurations of the reactive distillation process for unsaturated polyester synthesis. Moreover, multi-product simulations are performed to find the operational parameters for producing two different grades of polyester in the same equipment. Finally, the product transition time during product changeover is determined. The criteria to select the best configuration are minimum volume and energy requirement to produce 100 ktonnes/year polyester. First the best suitable internal for the column is identified and then the best suitable feed configuration is identified. From simulations, we concluded that the configuration which contains the reactive stripping section as a packed bubble column and the reactive rectifying section as a packed column requires minimum volume and energy to produce 100 ktonnes/year polyester. With respect to the feed configuration, we concluded that the feeding of monoesters to the reactive distillation column significantly intensifies the polyester process compared to an anhydrous reactant fed to the column. Moreover, the product transition time in this configuration is also significantly lower compared to the other configurations. In conclusion, a reactive distillation column coupled with a pre-reactor is the most promising alternative to continuously produce unsaturated polyesters. It requires a factor 10 (90%) lower volume, a factor 15 (93%) lower production time and a factor 3 (66%) lower energy as compared to the traditional batch reactor process to produce 100 ktonnes/year of polyester. Hence, the reactive distillation process improves the unsaturated polyester synthesis in all domains of structure, energy and time compared to the traditional batch reactor process coupled with a distillation column

Intensified processes for FAME production from waste cooking oil: a technological review

This article reviews the intensification of fatty acid methyl esters (FAME) production from waste cooking oil (WCO) using innovative process equipment. In particular, it addresses the intensification of WCO feedstock transformation by transesterification, esterification and hydrolysis reactions. It also discusses catalyst choice and product separation. FAME production can be intensified via the use of a number of process equipment types, including as cavitational reactors, oscillatory baffled reactors, microwave reactors, reactive distillation, static mixers and microstructured reactors. Furthermore, continuous flow equipment that integrate both reaction and separation steps appear to be the best means for intensifying FAME production. Heterogeneous catalysts have also shown to provide attractive results in terms of reaction performance in certain equipment, such as microwave reactors and reactive distillation

MOLECULAR DYNAMICS SIMULATION OF DICARBOXYLIC ACID COATED AQUEOUS AEROSOL: STRUCTURE AND PROCESSING OF WATER VAPOR

Low molecular weight dicarboxylic acids constitute a significant fraction of water-soluble organic aerosols in the atmosphere. They have a potential contribution to the formation of cloud condensation nuclei (CCN) and are involved in a series of chemical reactions occurring in atmosphere. In this work, molecular dynamics simulation method was used to probe the structure and the interfacial properties of the dicarboxylic acid coated aqueous aerosol. Low molecular weight dicarboxylic acids of various chain lengths and water solubility were chosen to coat a water droplet consisting of 2440 water molecules. For malonic acid coated aerosol, the surface acid molecules dissolved into the water core and form an ordered structure due to the hydrophobic interactions. For other nanoaerosols coated with low solubility acids, phase separation between water and acid molecules was observed. To study the water processing of the coated aerosols, the water vapor accommodation factors were calculated

Phase behaviour studies related to biodiesel production using supercritical methanol

Biodiesel is a promising renewable and sustainable fuel that can replace fossil fuels. Among the different techniques used to produce biodiesel, the transesterification process is currently the preferred method. The conventional transesterification process is based on acid-base catalysis, but this technique has many drawbacks including a requirement for high-purity feedstocks, and costly pre-treatment and downstream processes. A recent alternative process, using a supercritical alcohol (preferably methanol) without a catalyst, may offer some advantages. This process can utilise a wide range of potential feedstocks (especially wastes), shows high production efficiency, and requires only simple post-processing. However, this technique requires conditions of high temperature and high pressure which increase the utility costs and may restrict the economic feasibility and sustainability of the process. In order to fully explore these issues and to optimise the process conditions, better understanding of the phase behaviour of the mixtures involved in the biodiesel process is required. The components of interest include fatty acids, esters alcohols and co-solvent such as carbon dioxide and the conditions include high pressures and wide ranges of temperature. Phase equilibrium studies on systems relevant to biodiesel production with supercritical methanol available in the literature are very limited. The principal focus of this project is the experimental investigation of the phase behaviour of representative mixtures with small molecular chains, which exist during biodiesel production, over wide ranges of temperatures and pressures. In addition to the experimental work, the research will include both modelling works on the mixtures of interest supported by a simulation for the process using gPROMS, a simulation tool developed by Process Systems Enterprise (PSE) company. In this project, new fluid-phase equilibrium measurements have been carried out on two relevant representative binary systems: (methyl propanoate + carbon dioxide) and (butanoic acid + carbon dioxide) using a high-pressure quasi-static analytical apparatus with compositional analysis using a gas chromatography. The measurements for the (methyl propanoate + carbon dioxide) mixture were made along six isotherms at temperatures from (298.15 to 423.15) K and at pressures up to near the mixture critical pressure at each temperature while for the mixture (butanoic acid + carbon dioxide) the measurements were made along eight isotherms at temperatures from (323.13 to 423.2) K and pressures up to the mixture critical pressures. Vapour-liquid equilibrium (VLE) data obtained for the mixtures have been compared with the predictions of SAFT- Mie model, a group-contribution version of the Statistical Associating Fluid Theory (SAFT). The group interaction parameters in SAFT- Mie reported in literature have been revised by fitting to the new experimental VLE data. After parameters optimisation, the model was found to be in a good agreement with the measured VLE data for both bubble and dew points. The experimental data were also compared with the description of Peng Robinson equation of state (PR EoS) combined with the classical one-fluid mixing rules integrating one temperature-independent binary interaction parameter for (methyl propanoate + carbon dioxide) system and two temperature-independent binary interaction parameters for (butanoic acid + carbon dioxide) system. The results after tuning show that the PR EoS can also predict well the system measured data, except in the critical regions in which PR EoS shows overprediction. Furthermore, the phase equilibria of (methyl propanoate + propionic acid + carbon dioxide), (tert-butanol + water + carbon dioxide) and (toluene + water + carbon dioxide) ternary systems were studied by the means of the high-pressure quasi-static analytical apparatus. Compositions of present phases coexisting in vapour-liquid equilibrium (VLE) for (methyl propanoate + propionic acid + carbon dioxide) mixture were measured along six isotherms at temperatures from (323.12 to 423.11) K and pressures from (1 to 20) MPa at equal feed molar ratio of (methyl propanoate + propionic acid). Phase behaviour measurements were also collected at different compositions of the mixture (methyl propanoate + propionic acid) at fixed temperatures and pressures. Compositions of coexisting phases of the ternary system (tert-butanol + carbon dioxide + water) have been obtained along five isotherms at temperatures of (283.2, 298.18, 323.13, 373.10 and 423.17) K and at pressures of (4.0, 8.0, 12.0 and 18.0) MPa with different known feed compositions of (tert-butanol + water) while the phase behaviour of the system (toluene + water + carbon dioxide) was investigated along four isotherms at temperatures from (338.15 to 413.15) K and pressures up to the upper critical end point (UCEP). The data obtained for the ternary mixtures have been compared with the descriptions of SAFT- Mie and PR equation of states. Other cross interactions available in biodiesel systems such as (COOH - CH3OH), (OH_Gl - CH3OH), (CO2 - CH=), (CH3OH - CH=), (COOH - CH=) and (H2O - CH=) were estimated in this work by regression to fluid-phase behaviour data published in literature. The comparison between the predictions of SAFT- Mie reported in literature and those of SAFT- Mie after refining the parameters were shown. Preliminary designs of one-step process (transesterification) and two-step processes (hydrolysis and esterification) for biodiesel production under supercritical conditions were suggested and simulated using gPROMS ProcessBuilder software. The CO2 co-solvent effect on the one-step process based on literature data was also examined by a process flowsheet. The research including new phase behaviour measurements, modelling and gPROMS simulation is expected to contribute to optimisation of biodiesel production processes.Open Acces

Environmental Quality Laboratory Research Report, 1985-1987

The Environmental Quality Laboratory at Caltech is a center for research on large-scale systems problems of natural resources and environmental quality. The principal areas of investigation at EQL are: 1. Air quality management. 2. Water resources and water quality management. 3. Control of hazardous substances in the environment. 4. Energy policy, including regulation, conservation and energy-environment tradeoffs. 5. Resources policy (other than energy); residuals management. EQL research includes technical assessments, computer modeling, studies of environmental control options, policy analyses, and research on important components of the large-scale systems. Field work is also undertaken at EQL, some in collaboration with other organizations, to provide critical data needed for evaluation of systems concepts and models. EQL's objectives are as follows: 1. To do systematic studies of environmental and resources problems. The results of these studies, including the clarification of policy alternatives, are communicated to decision-makers in government and industry, to the research community, and to the public. As an organization, EQL refrains from advocating particular policies, but seeks to point out the implications of the various policy alternatives. 2. To contribute to the education and training of people in these areas through involvement of predoctoral students, postdoctoral fellows, and visiting faculty members in EQL activities. This educational effort is just as important as the results of the studies themselves, and should make lasting contributions to the nation's ability to solve its environmental and resources problems. The work at EQL goes beyond the usual academic research in that it tries to organize and develop the knowledge necessary to clarify society's alternatives by integrating relevant disciplines. EQL works on solving problems of specific localities when there is a strong element of public interest or educational value, or the concepts and results are applicable to other places. The research of EQL during this period was done under the supervision of faculty members in Environmental Engineering Science, Chemical Engineering, and Social Science. This research report covers the period from October 1985 through September 1987. The publications listed under the individual project descriptions are the new ones for the reporting period