Hydrocarbon material balance

The heat and material balances for an SGP-based hydrogen plant along with the associated costs have been developed for a plant sized to produce 100 X 10 scf/sd of hydrogen. The hydrocarbon material balance is contained in Tables I, IIA and IIB. A summary of the estimated capital investment, identified by plant section, is given in Table III. Table IV contains a summary of operating cost calculations. Additional economics details are given in Table V. 

Table VI shows a hydrocarbon material balance for operation of a neohexane unit. This operation is typical in that pentane and hexane are isomerized together and the recycle ratio is set by the amount of feedstock available and the capacity of the equipment.

Complete hydrocarbon material balance for feed and products. 

Hydrocarbon material balances around product strippers. 

Much later (Marcinkowsky and Berty 1973) it was proven that ethane did indeed have an effect. In the study of the inhibitor action of chlorinated hydrocarbons it was discovered that these compounds chlorinate the silver catalyst and ethane removes the chlorine from the catalyst by forming ethyl chloride. Since the inhibitor was in the 10 ppm range and similar quantities were used from the ethane present in about one volume percent, the small difference could not be calculated from material balance. The effect of ethane was only noticed as significant by the statistics, which justifies the statement made by Aris (1966) that, The need for sophistications should not be rejected unsophisticatedly. ... 

Design a packed tower splitter for a light hydrocarbon plant. The conditions of operation as determined from material balance are ... 

Equilibrium Basic Consideration, 1 Ideal Systems, 2 K-Factor Hydrocarbon Equilibrium Charts, 4 Non-Ideal Systems, 5 Example 8-1 Raoult s Law, 14 Binary System Material Balance Constant Molal Overflow Tray to Tray,... 

Environmental organic pollutants may be degraded depending on their toxicity, solubility, distribution constant Kow because physical properties of hydrophobic chemicals may affect the solubility and therefore the amount of organic carbon available in the aqueous phase for microbial assimilation and further metabolism (Schwarzenbach and Westall 1981). Chemicals are subject to volatilization and such loss is not assessed in most of the study except for physical transformation and material balance purposes. Polyaromatic hydrocarbons (PAHs) are known to volatilized during incubation even with capping and more then 40% of the initial chemicals could be found lost (Yin and Gu, unpublished data). When proper control was not included and such... 

Reaction rates for the start-of-cycle reforming system are described by pseudo-monomolecular rates of change of the 13 kinetic lumps. That is, the rates of change of the lumps are represented by first-order mass action kinetics with the same adsorption isotherm applicable to each reaction step. Following the same format as Eq. (4), steady-state material balances for the hydrocarbon lumps are derived for a plug-flow, fixed bed catalytic reformer. A nondissociation, Langmuir-Hinshelwood adsorption model is employed. Steady-state material balances written over a differential fractional catalyst volume dv are the following ... 

SimSim fills the gap between material balance techniques and complex reservoir simulation yet keeping the simplicity and speed of the material balance but providing reservoir simulation like results, i.e. pressure, saturation, hydrocarbons in place and fluid flux distribution within the reservoir. 

After reaction, the acid-hydrocarbon emulsion passes from the reactor to a baffled settler where a phase separation takes place and settled acid is pumped back to the reactor. The settled hydrocarbon phase is caustic scrubbed to remove any entrained acid and sent either to a material balance accumulator or to a product accumulation system. 

Gravimetric results of the process yields are given in Table III. The percentage of hydrocarbon gases was calculated to close the material balance on carbon and the calculated nonhydrocarbon products were derived by... 

Experiments were carried out between 720° and 985°C with 1-butene and between 760°and 925°C with the mixed isomers of 2-butene, using steam dilution corresponding to a steam hydrocarbon weight ratio of between 0.17 and 1.2 g/g. All runs were isobaric at total pressure of 1.0 psig. Material balances generally fell within dz 2% for all of the experiments. Tables I and II summarize the individual run conditions, the observed yields and conversions, and the calculated rate constants for pyrolysis of 1-butene and the 2-butenes, respectively. 

Available reaction-transport models describe the second regime (reactant transport), which only requires material balances for CO and H2. Recently, we reported preliminary results on a transport-reaction model of hydrocarbon synthesis selectivity that describes intraparticle (diffusion) and interparticle (convection) transport processes (4, 5). The model clearly demonstrates how diffusive and convective restrictions dramatically affect the rate of primary and secondary reactions during Fischer-Tropsch synthesis. Here, we use an extended version of this model to illustrate its use in the design of catalyst pellets for the synthesis of various desired products and for the tailoring of product functionality and molecular weight distribution. 

Photo-oxidation has been reported at crude-oU spills. It results in depletion of n-aUcanes below nCi5 and alkylaromatics such as C - and C2-substituted naphthalenes relative to unoxidized oil (Payne and Phillips, 1985). In terms of a material balance, photo-oxidation has been found to be a minor process (NRC, 1985) but does result in changes in the residual oil composition and can affect the subsequent behavior of an oil spill on the open ocean (Payne and Phillips, 1985). Autooxidation reactions of hydrocarbons in the absence of hght have not been well studied. 

Extractive Distillation Recovery of Isoprene. A typical flow-sketch and material balance of distillation and solvent recovery towers for extracting isoprene from a mixture of cracked products with aqueous acetonitrile appears in Figure 13.25. A description of the flowsheet of a complete plant is given in Example 2.9. In spite of the fact that several trays for washing by reflux are provided, some volatilization of solvent still occurs so that the complete plant also has water wash columns on both hydrocarbon product streams. A further complication is that acetonitrile and water form an azeotrope containing about 69 mol % solvent. Excess water enters the process in the form of a solution to control poly-... 

A conceptual material balance of a refinery producing 100,000 bbl/ day of fuel oil from coal was calculated (Table IV) based on the bench-scale data obtained by the authors and the published data available. In this projection, a coal containing 7.5% moisture, 10% ash, and 2.5% total sulfur is used as the feed. The hydrogenation can be performed in any type of reactor system in the ranges of 500°-550°C and 2000-3000 psi. The process conditions will be optimized for a coal conversion of about 80%. The hydrocarbon gases produced in the process will be used... 

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