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Side draw

The eadiest use of heat-exchange network synthesis was in the analysis of cmde distillation (qv) units (1). The cmde stream entering a distillation unit is a convenient single stream to heat while the various side draws from the column are candidate streams to be cooled in a network. So-called pumparounds present additional opportunities for heating the cmde. The successful synthesis of cmde distillation units was accompHshed long before the development of modem network-synthesis techniques. However, the techniques now available ensure rapid and accurate development of good cmde unit heat-exchange networks. [Pg.526]

Ma.nufa.cture. Mesityl oxide is produced by the Hquid-phase dehydration of diacetone alcohol ia the presence of acidic catalysts at 100—120°C and atmospheric pressure. As a precursor to MIBK, mesityl oxide is prepared ia this manner ia a distillation column ia which acetone is removed overhead and water-saturated mesityl oxide is produced from a side-draw. Suitable catalysts are phosphoric acid (177,178) and sulfuric acid (179,180). The kinetics of the reaction over phosphoric acid have been reported (181). [Pg.494]

Differential temperature as well as differential pressure can be used as a primary control variable. In one instance, it was hard to meet purity on a product in a column having close boiling components. The differential temperature across several bottom section trays was found to be the key to maintaining purity control. So a column side draw flow higher in the column was put on control by the critical temperature differential. This controlled the liquid reflux running down to the critical zone by varying the liquid drawn off at the side draw. This novel scheme solved the control problem. [Pg.69]

Problem A structured packing vacuum tower had too much heavy key in a vapor side-draw between the feed and the column bottom. The side-draw heavy key concentration was several times the design value. [Pg.308]

C02-0034. Carbon dioxide can exist as a liquid, solid (dry ice), or gas. Each carbon dioxide molecule is linear, with a carbon atom in the middle and an oxygen atom on either side. Draw molecular pictures that represent carbon dioxide in each phase. [Pg.109]

Column side-draws, methanol removal from, 18 520... [Pg.201]

Figure 11.6 illustrates the side draw-off of a fractionator. The liquid at point A is at its bubble or boiling point. We can be quite sure that this is true, because the liquid and vapor are in intimate contact at the vapor-liquid interface. We say that the vapor is at its dew point, and that the liquid is at its bubble point. [Pg.130]

It is positively my experience that the most common reason for pumps cavitation is partial plugging of draw nozzles. This problem is illustrated in Fig. 25.5. This is the side draw-off from a fractionator. Slowly opening the pump s discharge control valve increases flow up to a point. Beyond this point, the pump s discharge pressure and discharge flow become erratically low. It is obvious, then, that the pump is cavitating. [Pg.333]

Multiproduct fractionator controls, where, after dynamic correction, the boil-up, side-draw and distillate flows are ratioed to the feed flow (left). On the right, the true boiling points are controlled by throttling the product flows, while heat balance is controlled by manipulating the reflux flows. [Pg.254]

R disappearance by reaction of species, mol/hr SL liquid side draw, mol/hr... [Pg.318]

Guiding column optimization, and showing the effects of changing feed or product composition, thermal state of the feed, use of side draws, multifeed arrangements, etc. [Pg.81]

At the side draw-off points, the process comprises the follo dng supplementary oper-. atioDS ... [Pg.206]

One way to remove this inefficiency is done where the side draw from the main column is split first and returned as sub-cooled stream while the other stream is stripped in the side stripper. Therefore, the required stripping steam is reduced tremendously as the feed is reduced. The total savings in operating cost are 40,000/ for this simple modification in the piping connections. Another example of inefficiency is mixing two vapour streams with a big difference in their composition causes this inefficiency. The returned vapour from the KE side stripper is mixed with the vapour inside the main column which resulting in mixing losses. [Pg.171]

This modification suggests that the vapour must be returned to the stage of the liquid side draw where the vapour composition of this stage is similar to the returned vapour from the side stripper. Due to the reduction in the reboiler duty of the KE side stripper. [Pg.171]

The new configuration suggests increasing the bottom section by two stages which means moving the lowest side draw and pump around two stages up from the existing... [Pg.173]


See other pages where Side draw is mentioned: [Pg.80]    [Pg.38]    [Pg.219]    [Pg.80]    [Pg.229]    [Pg.231]    [Pg.93]    [Pg.959]    [Pg.147]    [Pg.147]    [Pg.204]    [Pg.130]    [Pg.93]    [Pg.135]    [Pg.433]    [Pg.434]    [Pg.435]    [Pg.435]    [Pg.435]    [Pg.318]    [Pg.228]    [Pg.184]    [Pg.71]    [Pg.219]    [Pg.115]    [Pg.313]    [Pg.313]    [Pg.313]    [Pg.316]    [Pg.48]    [Pg.122]    [Pg.280]   


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Industrial Column with Continuous Side-Stream Draw Off

Multiple Feeds, Side Draws

Multiple side-product draw-offs

Side Draw Flow Rate

Side Draw with a Practical Automatic Purging Strategy

Side draw columns

Side draw columns design

Side draw pin

Side draw stage

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