Distillation condensates diagram

Fig. 69. Production diagram of the semicontinuous production of polyphenyl-silsesquioxane obtained by the hydrolytic condensation of phenyltrichlorosilane 1,7- batch boxes 2 - hydrolyser 3 - separator 4 - flusher 5 - separator settling box 6 - distillation condenser tank 8 - cooler 9, 11, 12 - collectors 10 - settling box...

From the object palette Shortcut is selected and placed in the PFD area. The reboiler and condenser in the popup window are selected. Feed stream and two product streams are connected as shown in Figure 6.8. Double clicking on the shortcut distillation block diagram, the required data windows are shown in Figure 6.9. 

FIG. 13-1 Schematic diagram and nomenclature for a simple distillation column with one feed, a total overhead condenser, and a partial rehoiler. 

A more complex unit is shown in Fig. 13-24, which is a schematic diagram of a distillation column with one feed, a total condenser, and a partial reboiler. Dotted hnes encircle the six connected elements (or units) that constitute the distillation operation. The variables N, that must be considered in the analysis of the entire process are just the sum of the Nfs for these six elements since here Nr = 0. Using Table 13-5,... 

Figure 3-1. Flow diagram of atmospheric and vacuum distillation units (1,3) heat exchangers (2) desalter, (3,4) heater (5) distillation column, (6) overhead condenser, (7-10) pump around streams, (11) vacuum distillation heater (12) vacuum tower.

Suppose you fractionated that liquid of composition A, collected a few drops of the condensed vapor at the top of the column, analyzed it by taking its refractive index, and found that this liquid had a composition corresponding to point J on our diagram. You would follow the same path as before (B-C-D, one distillation D-G-H, another distillation) and find that composition J falls a bit short of the full cycle for distillation 2. 

The sketch below shows a distillation column that is heat-integrated with an evaporator. Draw a conirot concept diagram which accomplishes the following Directives (a) In the evaporator, temperature is controlled by steam, level by liquid product, and pressure by auxiliary cooling or vapor to the rcboiler. Level in the condensate receiver is controUed by condensate. 

A flow diagram of an anhydrous phenol solvent extraction plant is shown in Figure 8. Raw distillate is passed through a tower in which it absorbs phenol from the recovery system vapor. The oil is then passed to the treating tower, generally a few sections above the bottom. Anhydrous phenol is introduced at the top of this tower. Phenolic water condensate from the solvent recovery system (about 9.5% phenol) is introduced at the bottom of the tower to effect reflux. A temperature gradient of 10° to 75° F. may be... 

We can construct a distillation column that has separate steps or plates (i.e., a bubble-cap type distillation column). Each plate would correspond to an evaporation-condensation step. The phase diagram for such a system is illustrated in Figure 2.3b. This type of a column is a useful example for describing the concept of plates. 

Otherwise expressed, the number of theoretical plates required for a given separation increases when the reflux ratio is decreased, i.e. when the amount of condensed vapour returned to the column is decreased and the amount distilled off becomes greater. The variation in the reflux ratio is achieved by the use of a suitable take-off head (or still-head), usually of the total condensation variable take-off type. In use, all the vapour is condensed and the bulk of the condensate is returned to the fractionating column, small fractions of the condensate being allowed to collect in a suitable receiver. The design may be appreciated from the line diagram shown in Fig. 2.107 in which the controlled collection of distillate is by the socket-cone screw-operated valve sited just below the condenser drip end. 

Figure 10 shows the relationship between yx and xx for different values of an calculated from Eq. (8). When two components have close boiling points, by implication they have similar vapor pressures, so that an is close to unity. Separation of mixtures by distillation becomes more difficult as an approaches unity. Figure 11 indicates some of the x, y diagrams that can be obtained for distillation systems. Also shown are corresponding temperature-composition diagrams. The saturated vapor or dewpoint curve is determined by finding the temperature at which liquid starts to condense from a vapor mixture. Similarly, the saturated liquid or bubble-point curve corresponds to the temperature at which a liquid mixture starts to boil. For ideal mixtures, the dewpoint and bubble-point curves can be calculated as follows. From Eq. (3), at the dew point, since... 

The synthesis forms a mixture of 60-80% of ethylchlorosilanes and 20-40% of unreacted ethylchloride. This mixture (condensate) is then sent to rectification. The diagram of the distillation of unreacted ethylchloride and the rectification of ethylchlorosilanes is similar to the diagram given in Fig.4. After the distillation of unreacted ethylchloride at 0.2—0.25 MPa the ethylchlorosilane mixture is rectified. The mixture has the following average composition (%) ... 

The unreacted dimethyldichlorosilane with hydrogen chloride is distilled when the temperature in the higher part of the tower is 70-72 °C. Dimethyldichlorosilane vapours condense in refluxer 8, which is cooled with water. The condensate flows into the separation box, from where the most part is returned to reflux the tower, and the rest is sent through rotameter into the chlorinator, where it is mixed with the 2% initiator solution for repeated chlorination. After refluxer 8, hydrogen chloride enters the backflow igurit condenser (not shown in the diagram), where it is purified from the impurity of dimethyldichlorosilane, and is sent for water absorption. 

Fig. 20. Production diagram of chlorinated phenyltrichlorosilanes 1 - batch box 2 - fire-resistant apparatus 3 - tower with CaCl2 4 - receiver 5 - condenser 6,1-collectors 8 - distillation tank 9 - container 10- chlorinator...

Fig. 21. Production diagram of silicon tetrachloride by ferrosilicon chlorination 1 - jaw crasher 2 - bucket elevator 3 - grate 4 - shaft hoist 5 -bin 6 - chlorinating furnace 7 - condenser 8 - scrubber 9 - boiler 10, 14 - condensers 11 - distillation tank 12 - rectification tower 13 - refluxer 15 -collector 16- apparatus for the destruction of solid chlorides 17- hydrolysis chamber 18- absorption column.

The steam and gas mixture enters water-cooled cooler 9 and through phase separator 10 enters salt-cooled cooler 77. The condensed alcohol is sent into collector 7, and hydrogen chloride vapours are sent through phase separator 12 to be purified in bubble tanks (not shown in the diagram). After the excess alcohol and hydrogen chloride are distilled, the mixture is sampled at 140°C to determine hydrogen chloride content. If HC1 content is below 0.5%, the reactive mass is cooled with water sent into the tank jacket. If hydrogen chloride content exceeds 0.5%, the distillation is continued. 

Fig. 26. Production diagram of tetraphenoxysilane and 1,3-bis(triphenoxysiloxy)benzene 1,2- batch boxes 3 - etherificator 4, 11 - backflow condensers 5, 8, 9 - collectors 6 -distillation tank 7 - direct condenser 10 -re-etherificator 12 - receptacle 13 - nutsch filter.

Fig. 35. Production diagram of oligomethylsiloxanes by separate hydrolytic condensation 1,6- backflow condensers 2, 5, 9, 14, 16 - batch boxes 3, 4 - hydrolys-ers 7- neutraliser 8, 10, 13 - collectors 11, 12 - separators 15 - reactor 17, 18 -distillation tanks 19 - pressure filter.

Fig. 39. Production diagram of high-viscosity oligomethylsiloxanes 1-4, 6- batch boxes 5- agitator 7- hydrolyser 8, 13 - condensers 9- absorption column 10, 12 - collectors 11 - vacuum distillation tank 14 - receptacle 15 - settling box 16 -nutsch filter...

In tank 25 the products of hydrolytic condensation are distilled from toluene. Cooler 26 is filled with water, and the tank jacket is filled with water vapour. The contents of the tank are heated to 80-90 °C and held at this temperature for 1 hour. The separated water and the intermediate layer are poured off into the intermediate container (not shown in the diagram) then toluene is distilled. First, the temperature in the tank at atmospheric pressure reaches 130 °C then, the tank is cooled to 70-90 °C and a residual pressure of 0.04-0.06 MPa is created in the system. Further distillation is conducted in the tank to 150 °C. The toluene vapours condensed in cooler 26 are collected in receptacle 27 and sent by compressed nitrogen flow (0.07 MPa) into flusher 28 as they accumulate. The flusher is filled with water, and the mixture is agitated for 10 minutes after that the agitator is switched off and the mixture is settled for 2 hours. The bottom layer, aqueous-alcoholic solution, is poured into neutraliser 13, and the top layer, washed toluene, is sampled for moisture content. If moisture content does not exceed 0.06%, toluene is poured into receptacle 30, sent to azeotropic drying (until the moisture content does not exceed 0.02%) and re-used in reactive mixtures. 

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