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In distillation

In addition, one other feature of the prefractionator arrangement is important in reducing mixing effects. Losses occur in distillation operations due to mismatches between the composition of the column feed and the composition on the feed tray. Because the prefractionator distributes component B top and bottom, this allows greater freedom to match the feed composition with one of the trays in the column to reduce mixing losses at the feed tray. [Pg.151]

Glinos, K., and Malone, M. F., Optimality Regions for Complex Column Alternatives in Distillation Columns, Trans. IChei lE ChERD, 66 229, 1988. [Pg.157]

Various heat pumping schemes have been proposed as methods for saving energy in distillation. Of these schemes, use of the column overhead vapor as the heat pumping fluid is usually the most economically attractive. This is the vapor recompression scheme shown in outline in Fig. 14.6. [Pg.346]

Figure 14.6 Heat pumping in distillation. A vapor re-compreasion scheme. (From Smith and Linnhoff, Trans. IChemE, ChERD, 66 195, 1988 reproduced by permission of the Institution of Chemical Engineers.)... Figure 14.6 Heat pumping in distillation. A vapor re-compreasion scheme. (From Smith and Linnhoff, Trans. IChemE, ChERD, 66 195, 1988 reproduced by permission of the Institution of Chemical Engineers.)...
Distillation capital costs. The classic optimization in distillation is to tradeoff capital cost of the column against energy cost for the distillation, as shown in Fig. 3.7. This wpuld be carried out with distillation columns operating on utilities and not integrated with the rest of the process. Typically, the optimal ratio of actual to minimum reflux ratio lies in the range 1.05 to 1.1. Practical considerations often prevent a ratio of less than 1.1 being used, as discussed in Chap. 3. [Pg.349]

The pressure in distillation column 1 has been increased to allow feed vaporization by heat recovery (from the distillation column condenser). Inspection of the new curves in Fig. 14.9a raises further possibilities. With the proposed modification, the overheads from the... [Pg.352]

Kayihan, F., Optimum Distribution of Heat Load in Distillation Columns Using Intermediate Condensers and Reboilers, AfC/iS Symp. Ser., 192(76) 1, 1980. [Pg.354]

These compounds can be malodorous as in the case of quinoline, or they can have a plecisant odor as does indole. They decompose on heating to give organic bases or ammonia that reduce the acidity of refining catalysts in conversion units such as reformers or crackers, and initiate gum formation in distillates (kerosene, gas oil). [Pg.326]

Weigh out accurately about 2-5 g. of pure powdered succinic acid, transfer to a 100 ml. graduated flask, dissolve in distilled water, make the solution up to the graduation mark and mix well. Now, by means of a pipette, transfer 25 ml. of the solution to a 150 ml. conical flask, add a drop of phenolphthalein solution and titrate with A/ 2 NaOH or KOH solution to obtain consistent results. [Pg.448]

Wider passages are provided for vapours and the comparatively narrow tubes, which are usually fitted through holes bored in cork or rubber stoppers, are absent this considerably diminishes danger in violent reactions and also tends to give better results in distillation under reduced pressure as well as diminishing the hazard of choking. ... [Pg.207]

Another method of purihcation consists in distillation under reduced pressure. The fraction of b.p. I40-I50°/20 mm. is collected separately, - it solidihes on standing, melts at 76-76-5°, and is practically pure-... [Pg.762]

Indicator solutions 1, 1% solution in ethanol 2, 0.1% solution in ethanol 3, 0.05% solution in 90% ethanol 4, sodium or potassium salt in distilled water 5, 0.2% solution in 70% ethanol 6, distilled water. [Pg.947]

Accurately weigh about 6 g NaCl and dissolve in distilled water. Pass the solution through a well-rinsed cation exchange column (Dowex 50W) in the hydrogen form. The equivalent amount of HCl is washed from the column (in 10 column volumes) into a volumetric flask and made up to volume. Equivalent weight is the formula weight. [Pg.1152]

Sodium thiosulfate, O.IA. Weigh 24.818 g of fresh crystals of Na2S203 5H2O, dissolve in distilled water. Add 0.5 g of Na2C03 and 0.5 mL of chloroform as preservative. Dilute to 1 L. [Pg.1160]

BaCl IH O 244.28 Dissolve clear crystals of the salt in distilled water. Standardize against K2SO4 or Na2S04. [Pg.1171]

Hg(N03)2 H3O 342.62 Dissolve the reagent grade salt in distilled water and dilute to desired volume. Standardize against NaCl. [Pg.1171]

K4[Fe(CN)], 3H3O 422.41 Dissolve the high-purity commercial salt in distilled water containing 0.2 g/L of Na2C03. Kept in an amber container and away from direct sunlight, solutions are stable for a month or more. Standardize against zinc metal. [Pg.1171]

K3SO3 (P) 174.26 Dissolve about 17.43 g, previously dried at 150°C and accurately weighed, in distilled water and dilute exactly to 1 L. [Pg.1171]

Na3S04 (P) 142.04 Weigh accurately 14.204 g, dried at 150°C, and dissolve in distilled water. Dilute to exactly 1 L. [Pg.1171]

Calculating the solubility of Pb(I03)2 in distilled water is a straightforward problem since the dissolution of the solid is the only source of Pb + or lOa. How is the solubility of Pb(I03)2 affected if we add Pb(I03)2 to a solution of 0.10 M Pb(N03)2 Before we set up and solve the problem algebraically, think about the chemistry occurring in this system, and decide whether the solubility of Pb(I03)2 will increase, decrease, or remain the same. This is a good habit to develop. Knowing what answers are reasonable will help you spot errors in your calculations and give you more confidence that your solution to a problem is correct. [Pg.157]

This is a more difficult equation to solve than that for the solubility of Pb(I03)2 in distilled water, and its solution is not immediately obvious. A rigorous solution to equation 6.34 can be found using available computer software packages and spreadsheets. [Pg.157]

A 0.3619-g sample of tetrachloropicolinic acid, C6HNO2CI4, is dissolved in distilled water, transferred to a 1000-mL volumetric flask, and diluted to volume. An exhaustive controlled-potential electrolysis of a 10.00-mL portion of this solution at a spongy silver cathode requires 5.374 C of charge. What is the value of n for this reduction reaction ... [Pg.506]

Equation 55 is a tigoious expression for the number of overall transfer units for equimolar counterdiffusion, in distillation columns, for instance. [Pg.26]

General Situation. Both unidirectional diffusion through stagnant media and equimolar diffusion are idealizations that ate usually violated in real processes. In gas absorption, slight solvent evaporation may provide some counterdiffusion, and in distillation counterdiffusion may not be equimolar for a number of reasons. This is especially tme for multicomponent operation. [Pg.28]

The situation is very much poorer for stmctured rather than random packings, in that hardly any data on Hq and have been pubHshed. Based on a mechanistic model for mass transfer, a way to estimate HETP values for stmctured packings in distillation columns has been proposed (91), yet there is a clear need for more experimental data in this area. [Pg.39]

The vapor density of acetic acid suggests a molecular weight much higher than the formula weight, 60.06. Indeed, the acid normally exists as a dimer (4), both in the vapor phase (5) and in solution (6). This vapor density anomaly has important consequences in engineering computations, particularly in distillations. [Pg.64]

An adsorbent can be visualized as a porous soHd having certain characteristics. When the soHd is immersed in a Hquid mixture, the pores fill with Hquid, which at equilibrium differs in composition from that of the Hquid surrounding the particles. These compositions can then be related to each other by enrichment factors that are analogous to relative volatiHty in distillation. The adsorbent is selective for the component that is more concentrated in the pores than in the surrounding Hquid. [Pg.291]

Table 8. UOP Sorbex Separation of Fatty Acids from Rosin Acids in Distilled Tall Oil... Table 8. UOP Sorbex Separation of Fatty Acids from Rosin Acids in Distilled Tall Oil...
Dissolved matter lowers oxygen solubihty. At 20°C and 101.3 kPa (1 atm), the equihbrium concentration of dissolved oxygen in seawater is 7.42 mg/L. It is 9.09 mg/L in chloride-free water and 9.17 mg/L in clean water. This lessening of oxygen solubihty is of importance to wastewater treatment. The solubihty of atmospheric oxygen in a domestic sewage is much less than in distilled water (12). [Pg.339]


See other pages where In distillation is mentioned: [Pg.322]    [Pg.346]    [Pg.358]    [Pg.478]    [Pg.69]    [Pg.57]    [Pg.291]    [Pg.47]    [Pg.103]    [Pg.871]    [Pg.914]    [Pg.159]    [Pg.201]    [Pg.183]    [Pg.364]    [Pg.398]    [Pg.434]    [Pg.573]    [Pg.586]   
See also in sourсe #XX -- [ Pg.7 ]

See also in sourсe #XX -- [ Pg.422 , Pg.426 , Pg.427 , Pg.428 , Pg.429 , Pg.430 , Pg.450 , Pg.451 , Pg.452 ]




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A Fundamental Model of Mass Transfer in Multicomponent Distillation

Application 1. Steady-state Entropy Production Profile in a MTBE Reactive Distillation Column

Application of NLP Based Techniques in Batch Distillation

Application of Reactive Distillation and Strategies in Process Design

BINARY DISTILLATION IN PACKED TOWERS

Benzophenone as indicator in THF distillation

Binary Distillation in Tray Columns

Categories of information resulting from the design process in reactive distillation

Condenser, in distillation

Control loops in a reactive distillation stage column

Crossflow plate in a distillation column

Design variables in distillation

Determination of water content in bitumen emulsions - azeotropic distillation method

Determination of water in bitumen by distillation method

Distillation in packed columns

Distillation in packed towers

Distillation in vacuo

Distillation under diminished pressure refinements in technique

Distillation, in situ

Efficiency in distillation

Electric heating mantles (for use in fractional distillation, etc

Enthalpy in distillation

Entrainer in distillation

Entrainers in Extractive Distillation

Entropy production in distillation

Entropy production in separation process distillation

Fixed points in reactive distillation

Heat Pumping in Distillation

In Ponchon-Savarit distillation method

In distillate fuel

Internal Mass Flows in Sequences of Simple Distillation Columns

Key components in multicomponent distillation

Mass transfer in distillation

Methods for determining the plate number in batch distillation arithmetically

Moisture Determination in Ammonium Nitrate by Azeotropic Distillation

Multicomponent Distillation in Tray Columns

Nonequimolar Effects in Multicomponent Distillation

Operational fractions of batch extractive distillation in a middle vessel column

Phase rule in distillation

Photolysis in distilled water

Pinch point in distillation

Pressure in distillation

Qualitative fingerprint of the design methods used in reactive distillation

Reboilers in distillation

Reflux ratio in Ponchon-Savarit distillation method

Reflux ratio in distillation

Reflux, in distillation

Schematic representation of the relevant spatial scales in reactive distillation

Separability in Extractive Distillation Columns

Separation factor in distillation

Separation in Two Distillation Fields

Solvent Effects in Extractive Distillation

Spatial and Control Structure Design in Reactive Distillation

Species/strains used in brewing and distilling

Spectrophotometric method of analysis using barbituric acid-pyridine in the distillate

Stages in distillation

Steady States in Distillation

Stripping in distillation

Sulfur Species in Middle-Distillate Oils

Temperature control in distillation

Test Method for Water in Crude Oil by Distillation

The Phase Rule in Distillation

Trade-offs in Azeotropic Distillation

Tray efficiency in distillation

Trays in distillation columns

Vacuum distillation in laboratory

Variables in Distillation

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