Separation recovery factor

Recovery factor Reduced column length Reduced plate height Reduced velocity Relative retention ratio Retardation factor d Retention time Retention volume Selectivity coefficient Separation factor... 

The most common approach to fixed cost estimation iavolves the use of a capital recovery factor to give the annual depreciation and return on capital. This factor typically is between 15 and 20% of the total capital investment. Property taxes are taken as 1—5% of the fixed capital and iasurance is assumed to be 1—2% of the fixed capital. If annual depreciation is estimated separately, it is assumed to be about 10% of the fixed capital investment. The annual iaterest expense is sometimes neglected as an expense ia preliminary studies. Some economists even beHeve that iaterest should be treated as a return on capital and not as part of the manufactufing expense. 

We must consider the laminar and turbulent portions of the boundary layer separately because the recovery factors, and hence the adiabatic wall temperatures, used to establish the heat flow will be different for each flow regime. It turns out that the difference is rather small in this problem, but we shall follow a procedure which would be used if the difference were appreciable, so that the general method of solution may be indicated. The free-stream acoustic velocity is calculated from... 

The fundamental purpose of a separation operation is to obtain efficiently a component in a state of high purity. Sandell defined a recovery factor Rf for a substance I by... 

Kolthoff and Noponen mixed 25 ml of 0.11 Af barium nitrate, 10 ml of 0.1 M lead nitrate, and 25 ml of 0.1 M sodium sulfate. After precipitation and digestion for 1 h, 59% of the lead remained in the precipitate. Calculate the recovery and separation (enrichment) factors for barium. 

Figure 23-9 is a set of curves, calculated from (23-19) and (23-23), for enrichment factor [Equation (22-2)] as a function of the number of equilibrations and transfers under several conditions. The number of equilibrations and transfers for quantitative recovery (recovery factor = 0.999) of component A and for its quantitative separation (enrichment factor = 0.001) from component B is indicated by the intersections of the lines with the 0.001 line for termination at the upper edge of the curves... 

On the basis of the data from the various tests, the net recovery factors were estiniatcd for the four routes A to D. It should be remembered that these are, in many cases, very preliminary tests and that there is still room for further improvements in the recovery of trash. It is important to remember that whatever the method of trash separation from the cane, a certain amount of vegetal impurity (trash) will remain with the cane and it will be crushed with the cane at the mill. This vegetal iti urity should be considered in the industrial process as it will influence the amount of bagasse produced. 

The term Downstream Processing in Biotechnology the chain of unit operations that are combined tern for the recovery, purification, separation tration of the products at the lowest possible highest possible recovery factor and quality. The recovery step generally represents a large... 

To overcome these shortcomings, steaming by block-cyclic technique has been developed at the Zybza field through both experimental work and field testing. In this variant of steam soak, separate closed and relatively stable high temperature fields are created by the thermodynamic process. Each one of these fields encloses a descrete block of the petroleum reservoir. Each field is confined within pre-selected boundaries beyond which the heat front does not extend. This method insures both maximum distance of penetration by the heat carrier into the individual reservoir sections of microporosity type and high oil recovery factors for this type of reservoir. 

The principal reservoir characteristics and technical data on the field prior to the commencement of steam flooding were as follows depth down to the producing horizon was variable-ffom 90 to 150 m average thickness of the bed-iSO m bed porosity-28% permeability-1 Darcy oil fill-80% speciric gravity of crude oil under surface conditions-0.93 g/cmh oil viscosity-165 centipoise tar content of crude-45% formation pressure immediately prior to the commencement of steam Ireatment-from 1 to 3 kg/cm temperature from 4 to 6°C oil recovery factor during the 40 years of conventional production prior to EOR work-14% number of wells drilled into the block X of the field-52 number of separate unit areas-9 area of each unit-from 0.34 to 0.87 ha. 

The cell recovery process was characterized by the cell enrichment factor E, cell separation factor S and cell recovery factor R ... 

Unless values of SF are about 10 or above, absorption and stripping operations cannot achieve sharp separation between two components. Nevertheless, these operations are used widely for preliminary or partial separations where the separation of one key component is sharp, but only a partial separation of the other key component is adequate. The degree of sharpness of separation is given by the recovery factor RF,... 

Despite the good efficiency and recovery factors of SFC, it cannot achieve a respectable status in separation science. This is due to its high cost and its inability to handle simultaneous and parallel extraction. Moreover, the high solubility of water in supercritical carbon dioxide makes it unfit for routine applications [92], Another problem in SFC... 

Catalyst development in hydroformylation started with the discovery of the reaction in 1938 and has led to several major new developments during intensive industrial appUcation of the reaction. Thereby, irmovations in catalyst and process technologies went hand-in-hand. The introduction of Rh-based hydroformylation required, for example, much stricter requirements with regard to catalyst separation, recovery, and recycle compared to Co-based technologies due to the much higher price of the catalytic metal (by about a factor of 1000). 

An analysis to determine the concentration of Cu in an industrial plating bath uses a procedure for which Zn is an interferent. When a sample containing 128.6 ppm Cu is carried through a separation to remove Zn, the concentration of Cu remaining is 127.2 ppm. When a 134.9-ppm solution of Zn is carried through the separation, a concentration of 4.3 ppm remains. Calculate the recoveries for Cu and Zn and the separation factor. 

Recoveries and separation factors are useful ways to evaluate the effectiveness of a separation. They do not, however, give a direct indication of the relative error introduced by failing to remove all interferents or failing to recover all the analyte. The relative error introduced by the separation, E, is defined as... 

A sample contains a weak acid analyte, HA, and a weak acid interferent, HB. The acid dissociation constants and partition coefficients for the weak acids are as follows Ra.HA = 1.0 X 10 Ra HB = 1.0 X f0 , RpjHA D,HB 500. (a) Calculate the extraction efficiency for HA and HB when 50.0 mF of sampk buffered to a pH of 7.0, is extracted with 50.0 mF of the organic solvent, (b) Which phase is enriched in the analyte (c) What are the recoveries for the analyte and interferent in this phase (d) What is the separation factor (e) A quantitative analysis is conducted on the contents of the phase enriched in analyte. What is the expected relative erroi if the selectivity coefficient, Rha.hb> is 0.500 and the initial ratio ofHB/HA was lO.O ... 

For the countercurrent extraction in Example A6.2, calculate the recovery and separation factor for solute A if the contents of tubes 85-99 are pooled together. 

To calculate the separation factor, we must determine the recovery of solute B in tubes 85-99. This is determined by calculating the fraction of solute B in tubes 85-100 and subtracting the fraction of solute B in tube 100. By calculating z and using Appendix lA, we find that approximately 10.6% of solute B is in tubes 85-100, and that essentially no solute B is in tube 100. The separation factor, Sb,a therefore, is... 

In contrast to trace impurity removal, the use of adsorption for bulk separation in the liquid phase on a commercial scale is a relatively recent development. The first commercial operation occurred in 1964 with the advent of the UOP Molex process for recovery of high purity / -paraffins (6—8). Since that time, bulk adsorptive separation of liquids has been used to solve a broad range of problems, including individual isomer separations and class separations. The commercial availability of synthetic molecular sieves and ion-exchange resins and the development of novel process concepts have been the two significant factors in the success of these processes. This article is devoted mainly to the theory and operation of these Hquid-phase bulk adsorptive separation processes. 

The component C in the separated extract from the stage contact shown in Eigure 1 may be separated from the solvent B by distillation (qv), evaporation (qv), or other means, allowing solvent B to be reused for further extraction. Alternatively, the extract can be subjected to back-extraction (stripping) with solvent A under different conditions, eg, a different temperature again, the stripped solvent B can be reused for further extraction. Solvent recovery (qv) is an important factor in the economics of industrial extraction processes. 

DifficultSepa.ra.tions, Difficult separations, characterized by separation factors in the range 0.95 to 1.05, are frequentiy expensive because these involve high operating costs. Such processes can be made economically feasible by reducing the solvent recovery load (260) this approach is effective, for example, in the separation of m- and -cresol, Hnoleic and abietic components of tall oil (qv), and the production of heavy water (see Deuteriumand TRITIUM, deuterium). 

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