AndreaBozzo/ceres-open-data-index huggingface dataset:
Fluid flow behavior through rock-slab micromodels in relation to other micromodels

A new technique was developed to visualize fluid movement and rock/fluid interaction in the pores of reservoir rocks. It consists of fabricating micromodels containing rock slabs of 3 millimeter thickness and using sensitive image acquisition, recording, and enhancement systems to perform time-and-motion analyses of high-speed events. Displacement experiments were performed using these rock-slab micromodels and two other types of micromodels: an etched-glass network model (HEG) and a chemically consolidated grain-packed (cryolite) model. The tests included several cycles of imbibition and drainage. Comprehensive steady-state tests were also performed in the two simplified (HEG and cryolite) models, which included two-phase and three-phase flows with gas/water, oil/water, and gas/oil/water systems. The results were compared to understand the scope and limitations of these micromodel techniques. 24 refs., 8 figs.

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Impact of pilot plant operations and concurrent development efforts on the projected performance and economics of a commercial EDS facility

One of the initial efforts in Phase V of the EDS Development Effort was the projection of the technical performance and economics of producing coal liquids using EDS technology. The balance of Phase V, which has included operation of the 200-ton per day Exxon Coal Liquefaction Pilot Plant, has produced data which is expected to have a major impact on the design and operation of a commercial EDS facility. In this study, MITRE performs an independent assessment of the Phase V development effort and projects its impact on projected yields, product quality, and cost of coal liquefaction produced from a commercial EDS facility.

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Degradation of polycyclic aromatic hydrocarbon compounds under various redox conditions in soil-water systems: Quarterly report, October 1987

This study evaluated microbial degradation of naphthol, naphthalene, and acenaphthene under aerobic, strict anaerobic, and denitrification conditions in soil-water systems. Chemical degradation of naphthol and naphthalene in the presence of a manganese oxide was also studied. Naphthol, naphthalene, and acenaphthene were degraded microbially under aerobic conditions from initial aqueous phase concentrations of 9, 7, and 1 mg/l to nondetectable levels in 3, 10, and 10 days respectively. Under anaerobic conditions naphthol degraded to nondetectable levels in 15 days while naphthalene and acenaphthene showed no significant degradation over time periods of 50 and 70 days respectively. Under denitrification conditions naphthol, naphthalene, and acenaphthene were degraded from initial aqueous phase concentrations of 8, 7, and 0.4 mg/l to nondetectable levels in 16, 45, and 40 days respectively. Acclimation periods of approximately 2 days under aerobic conditions, and 2 weeks under denitrification conditions, were observed for both naphthalene and acenaphthene. Abiotic degradation of naphthalene and naphthol were evaluated by reaction with manganese oxide, a minor soil constituent. In the presence of a manganese oxide naphthalene showed no abiotic degradation over a time period of nine weeks, while aqueous naphthol concentration decreased from 9 mg/l to nondetectable levels in 9 days. Results show that low molecular weight, unsubstitued polycyclic aromatic hydrocarbons are amendable to microbial degradation in soil-water systems under denitrification conditions. These type of compounds may otherwise persist in soil-water systems in the absence of nitrate and molecular oxygen, or a suitable substituent group on the aromatic ring. 27 refs., 10 figs.

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Study of high temperature removal of alkali of a pressurized gasification system: Final report. [Emathlite pellets]

Advanced coal-fueled processes that use high-temperature (1500 F or more) gas cleaning have the potential for significant cost savings. Turbine corrosion control by alkali removal may be needed in such systems. A fixed bed of emathlite pellets had been identified earlier as a promising way to remove alkali metal vapors from hot gases. In the present program we examined the fundamental chemistry of the absorption reaction, demonstrated the removal concept in a bench-scale reactor, and developed the engineering basis for process scale-up. An industrial process for making emathlite pellets by slurry extrusion was defined. Pellet cost was estimated as $0.11 to $0.82 per ton of coal, depending on scale of production. The absorption mechanism was defined and shown to result in a sorbent capacity of 18 wt % sodium. A kinetic model that allows sizing of sorbent beds was developed. It was shown that absorption is effective even at very low gas-phase concentrations. The suggested process was demonstrated in a series of fixed bed tests, using up to 12 kg sorbent, at a hot gas cleanup test facility. Alkali removal of greater than 99% was demonstrated. Kinetics and capacity data indicate that even more removal could have been achieved with deeper beds. It was concluded that reduction of gas-phase sodium to the turbine tolerance of about 20 ppb is feasible with this technique. Example calculations of typical process sorbent consumption rates and reactor size requirements are presented. 7 refs., 46 figs., 39 tabs.

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Entrained flow gasification at elevated pressure: Quarterly technical progress report No. 7 for the period 1 September 1986 to 30 November 1986

The three main tasks of this study are: (1) entrained coal gasification measurements, which include elevated pressure tests of three coal types, investigation of injector design, cold-flow measurements in simulated gasifier flows, and investigation of advanced optical diagnostic techniques that could be applied to gasification measurements; (2) improvement of the computer code for gasification processes, including improvement of physical submodels and numerical methods, and comparison of model predictions with experimental results for code validation; and (3) application of results to industrial and METC needs through technical seminars, expansion of a detailed data book, and distribution of the code to other users, including METC. Accomplishments for each of these tasks are presented. 36 refs., 11 figs., 5 tabs.

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ASPEN User Manual

ASPEN (Advanced System for Process Engineering) is a software system for computer-aided process design. ASPEN was developed at M.I.T. during the period 1976-1981 under the sponsorship of the Department of Energy and 55 industrial participants. There are four manuals and one computer tape describing the maintenance, use, and installation of ASPEN. The ASPEN User Manual is a two volume manual describing how to use ASPEN. It is intended to serve both as a reference manual for users familiar with ASPEN and as a tutorial manual for the beginning user. The User Manual contains all the information needed to create an ASPEN Input File. It does not describe how to make an ASPEN run. Run procedures are computer system dependent and are described in the four ASPEN Installation Manuals. In addition to these manuals, over 100 publications, reports, and theses were produced by the ASPEN project. The ASPEN Project Final Report serves as a guide to these documents.

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Basic studies in the displacement of residual oil by chemical flooding. Final report

Enhanced oil recovery research at the University of Houston has focused on certain aspects which are basic to the microscopic and macroscopic displacement processes occurring in low tension surfactant flooding processes. These have included: (1) Identification of the magnitude and role of dynamic interfacial effects in displacement and reconnection of low tension systems. (2) Identification of the coalescence characteristics of low tension systems and the effects on oil bank formation and oil recovery efficiency. (3) Evolution of pore level models of displacement, reconnection, and breakup phenomena in porous media. (4) Description of the displacement dynamics and interactions of oil blob populations moving through porous media. In connection with these objectives the important observations are discussed in this report. In general, this work should contribute to a more basic understanding of the dynamics of low tension immiscible displacement in porous media. 32 references, 24 figures, 2 tables.

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Hydraulic fracturing and associated stress modeling for the Eastern Gas Shales Project. Final report

Frac fluid flow, structure, and fracture mechanics simulations are developed for predicting and optimizing fracture dimensions and fluid leak-offs. Roles of in situ stress and material properties for possible vertical migration of fractures from the pay zone are discussed. Rationale for foam and dendritic fracturing experiments is presented along with numerical experiments for examining the phenomena of spalling of the fracture faces and conditions for secondary fracture initiation. Assignment of conventional, foam, cyrogenic, dendritic, and explosive fracturing treatments for specific reservoir properties is considered. Variables include fracture density and extent, shale thickness, in-situ stress gradients, energy assist mechanisms, well clean-up, shale-frac fluid interaction, proppant selection, and fracture height control. The analysis suggests that correlation with prevailing in situ stress gradients are promising diagnostic indicators for fracture treatment selection and design. In conclusion, the comprehensive development of an economical strategy requires extensive and controlled field testing with supporting predictive analyses of reservoir responses. Finite element modeling of reservoir in situ stress trajectories and the flow and fracture responses in the reservoir is recommended.

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An assessment of process modelling for fluidized bed coal gasifiers: Final report

This report presents a summary of the work accomplished in a multiyear study conducted for the US Department of Energy, Morgantown Energy Technology Center, under Contract AC21-83MC20440. The objective of this research is to assess process models of fluidized bed coal gasifiers; this assessment is based upon current and future process design and development requirements. The applicability of current models in simulating fluidized bed coal gasifiers is evaluated and the models are catalogued. Criteria for the improvement of these models are presented. There are a variety of fluidized bed gasifier models which are adequate for predictions of hydrodynamic mixing, material and energy balances and process efficiency. However, there is not a single gasifier model which can be applied to simulate all process phenomena. Future model development should be based upon the development of a data base against which the models can be compared. There is a particular need for quantitative data on ash agglomeration, bed rheology and chemical kinetics in the gasification environment. 131 references.

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Electrocyclone development program. Quarterly technical report, August-October 1981

Progress is reported in research on the use of applied electrostatics to enhance the performance of large (18-in. dia.) cyclone collectors for cleaning hot exhaust gases from pressurized fluidized bed (PFB) combustors in coal-fired power plants. Information is included on the electrocyclone cold flow test data; cyclone scaling; electrostatic component development; and redesign of the PFB test module. (LCL)

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Western Gas Sands Project. Quarterly basin activities report

A summation is presented of the coring program site identification, and drilling and testing activity in the four primary study areas of the Western Gas Sands Project (WGSP). Pertinent information for January, February, and March, 1978 is included for each study area. The areas are the Northern Great Plains Province, the Greater Green River Basin, the Piceance Basin, and the Uinta Basin.

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Coal gasification research studies. Technical progress report, January 20-February 19, 1984

The Coal Gasification Research Studies consist of three tasks: (1) Studies of Coal Ash Behavior; (2) High-Pressure Fluidization Studies; and (3) High Temperature Fluidization Studies. This month gasification runs were made in the 2-inch diameter unit at 1800/sup 0/F using 5% oxygen feed. Runs were made at steam/oxygen concentrations of 2/1 and 4/1 and reactor charges of 50g and 150g of char. Samples of Kentucky No. 9 and No. 11 coals were received and are being analyzed. Parts for the needle alignment assembly of the viscometer were received and installed. In the high-pressure fluidization studies, analysis of the test data to study the bubble characteristics was completed this month. These data were obtained using a -35 50 mesh sand in the 15-inch-diameter fluidization column at fluidizing gas velocities of 0.3, 0.36, 0.42, 0.48, and 0.54 ft/s and at various positions in the bed. Three additional tests were also conducted using -35 50 mesh sand under the same conditions as those in the earlier tests. The purpose of these tests was to check the reproducibility of the earlier test data. The results indicate that the data are indeed reproducible. Two tests were conducted in the high-temperature fluidization studies with -35 50 mesh Ottawa sand in the 6-inch-diameter Plexiglas column. The column was equipped with 12 pressure probes (4 sets of 3) and a 6-orifice gas distributor with an orifice diameter of 1/8 inch. The objective of these tests was to determine bubble charateristics at ambient temperature. Data were obtained at operating velocities of 1.5 and 1.8 times the minimum fluidization velocity, V/sub mf/, and a scanning speed of 400 scans/s. The data from these tests are being analyzed for bubble frequency, velocity and pierced lengths. 6 figures.

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Modeling of pressurized fluidized bed combustion of coal. Volume I. PFBC system model development. Final report

Fluid bed reactors were first used as catalytic reactors in the petroleum industry. This application, in order to maximize gas-solid contact, requires small particles and low gas velocities. Most empirical correlations for elutriation, gas exchange, etc. are based on data obtained with small particles. The atmospheric fluid bed coal combustor represents a significant break with this tradition. In order to maximize heat release per plane area AFBC's use large particles and high gas velocities. An absence of data on large particle systems represented a major obstacle in the development of a model to predict performance of AFBC's. However, once the need was established experimental programs were undertaken to obtain the necessary data and our present understanding of bed operation under these conditions far exceeds our knowledge 5 or 6 years ago. Unfortunately, basic information regarding flow regime, solids carry over, gas mixing, attrition, order of reaction etc. are not available. Until such information becomes available one cannot expect any PFBC model to yield accurate predictions concerning such important parameters as bed expansion, combustion efficiency, sulfur retention, etc. The approach taken in formulating the PFBC model is to incorporate basic physical principals as well as empirical relations as they are presently available to generate a mathematical framework.

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Coal gasification pilot plant support studies. Subtask 3-1. Effect of raw product gas composition on shift catalysts. [134 references]

Four sulfur-resistant high-temperature water-gas shift catalysts were evaluated, using feed compositions simulating those of coal gasifier effluents. These catalysts, G-93, United Catalysts, Inc.; UC-1870-46-1, Union Carbide Corp.; Catalysts 538, Shell Oil Co.; and Comox 207, LDI Catalyst Co., were found to be durable, easy to handle, and capable of promoting the water-gas shift reaction in the presence of CO, CO/sub 2/, H/sub 2/, CH/sub 4/, C/sub 2/H/sub 6/, C/sub 3/H/sub 8/, C/sub 4/H/sub 10/, H/sub 2/S, COS, CH/sub 3/SH, C/sub 2/H/sub 5/SH, C/sub 4/H/sub 4/S, N/sub 2/, NH/sub 3/, C/sub 6/H/sub 6/, C/sub 6/H/sub 5/OH, and H/sub 2/O. The catalysts were evaluated at the following process conditions: pressures of 50, 100, 200, 500, and 100 psig; temperatures of 400/sup 0/, 500/sup 0/, 550/sup 0/, 650/sup 0/, 750/sup 0/, 850/sup 0/, 950/sup 0/, and 1050/sup 0/F; CO concentrations of 10, 20, 30, and 80 mol % (water-free basis,7403 ); benzene concentrations of 0, 2, 10, and 20 mol %; phenol concentrations of 0, 0.1, 0.4, and 1 mol %; and an NH/sub 3/ concentration of 0.3 mol %. Life-test data were obtained with a packed-bed reactor, and rate data with a continuous-stirred tank reactor. The conditions and compositions used to obtain the data encompassed all existing gasification processes and gasifier effluents. Equations for the generalized rate of CO conversion were developed. Comparison of the values predicted by these equations with experimental data showed an average deviation of 11%.

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Corrosion in SRC-I coal liquid distillation towers. SRC-I quarterly technical report, April-June 1981. Supplement

During pilot plant operations for the SRC-I process, severe corrosion developed in the solvent fractionation towers. This high corrosion rate on carbon and types 304 and 316 stainless steel occurred when the pilot plant was processing coal with 0.15 to 0.39 wt % chloride. Subsequent stream analysis revealed that synergistic effects of inorganic chloride, phenols, and nitrogen compounds were responsible for corrosion most severe in the 200/sup 0/C (400/sup 0/F) boiling range. Liquid analysis also revealed the most likely path of chlorides to the tower. 4 figures, 9 tables.

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Advanced combined NO/sub x//SO/sub x/ removal system. Technical progress report, April 28-June 1, 1984

Previous results showed that Catalyst 100 gave the best overall performance; however, they also indicated that it will be necessary to increase the bed thickness in the existing moving bed contactor/filter in order to achieve 90% NO/sub x/ removal. During this reporting period, calculations to estimate the effect of increasing the moving bed thickness from its present value of 7/8 in. to 1.75 in. were completed under Task 2. Task 3 involves modifying the bed thickness and length of the existing contactor/filter. This will entail replacing the existing casing with a larger diameter casing. At the same time provision for a catalyst preheater will be made by increasing the length of the casing and installing additional heating elements above the bed furnace. The design of the new casing is shown. The majority of the parts have been assembled, and fabrication has been initiated. 3 figures.

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Effects of coal combustion effluent on pulmonary carcinogen metabolism

This supplement is being submitted to serve as a summary of the studies completed during the fiscal year 1979 to 1980. Because of the known deleterious effects of lipid peroxidation on microsomal xenobiotic metabolism in a variety of tissues (including lung) and the previously observed actions of heavy metals on hepatic lipid peroxidation, the following studies were carried out to characterize the process of lipid peroxidation in lung microsomes and to determine the actions of heavy metals on this process in the lung. The objective of these experiments was to evaluate potential mechanisms through which heavy metals might affect pulmonary xenobiotic (carcinogen) metabolism. To evaluate the actions of heavy metals on pulmonary microsomal metabolism, a combination of in vitro and in vivo studies was initiated. The in vitro studies included experiments to evaluate direct metal effects on enzyme activity as well as the effects of more prolonged exposure to the metals (preincubation studies). In all studies metal effects on pulmonary microsomal metabolism were compared with those in other tissues to evaluate specificity of action.

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High resolution capacitance imaging system: Technical note

The US Department of Energy's Morgantown Energy Technology Center (METC) has been developing instrumentation for improved monitoring of fluidized-bed operational parameters. This report describes the electronic system being developed to provide a real-time two-dimensional map of the bed material density with a resolution of 1 inch or better and with a map update rate of about 100 updates per second. This two-dimensional system is the major step in the development of the desired three-dimensional density mapping system. The density monitoring system uses a 6-inch inside diameter (ID) by 2-feet long plastic pipe as the fluidized-bed vessel. At a point halfway between the ends of the pipe, 16 1-inch x 1-inch metal electrodes are mounted on the inner surface of the pipe. With the pipe in a vertical position and holding 1/8-inch plastic spheres, air can be introduced at the bottom of the pipe to fluidize the spheres. By measuring the displacement currents between electrodes, equations relating the measured currents to bed density values are formed. Solving the equations produces the density values at 49 designated areas covering the bed cross section. Preliminary tests of the system have shown that single bubbles passing through the monitored bed cross section can be seen crossing the monitored region and can be located at n particular positions at times t1, t2, ..., t/sub n/ by solving the developed equations using the electrode displacement current values at times t1, t2, ..., t/sub n/. Further development is necessary to refine the computation of density values at each of the 49 designated areas and to extend the system's capability to three-dimensional, real-time bed density mapping. 5 refs., 13 figs., 7 tabs.

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Great Plains ASPEN model development. Technical progress report, April 1-April 30, 1984

During the period 4/1/84 through 4/30/84 work was performed on the following tasks: Task No. 1 simplified models and task No. 4 rigorous models (Area 4900-methanol synthesis,7404 ); and task No. 2 review of existing gasifier models. The ASPEN horizontal sizing routine, SUSOL, has been modified. Improvements have been made to the sizing calculations based on HALCON SD's own design methods. The user can also enter the maximum allowable horizontal velocity specifications.

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A feasibility study of oil shale fired pulse combustors with applications to oil shale retorting

The results of the experimental investigation performed to determine the feasibility of using pulverized Colorado oil shale to fuel a bench scale pulse combustor reveal that oil shale cannot sustain pulsations when used alone as fuel. Trace amounts of propane mixed with the oil shale enabled the pulsations, however. Up to 80% of the organic material in the oil shale was consumed when it was mixed with propane in the combustor. Beyond the feasibility objectives, the operating conditions of the combustor fuel with propane and mixtures of oil shale and propane were characterized with respect to pulsation amplitude and frequency and the internal combustor wall temperature over fuel lean and fuel rich stoichiometries. Maximum pressure excursions of 12.5 kPa were experienced in the combustor. Pulsation frequencies ranged from 50 to nearly 80 Hz. Cycle resolved laser Doppler anemometry velocities were measured at the tail pipe exit plane. Injecting inert mineral matter (limestone) into the pulse combustor while using propane fuel had only a slight effect on the pulsation frequency for the feed rates tested.

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