Stripping column

Figure C2.7.3. Process flow diagram for hydrofoniiylation of propene 4, stripping column 5, heat exchanger.

Fig. 5. Hoechst/Rhc ne-Poulenc oxo flow scheme A, stirred tank reactor B, separator C, phase separator D, stripping column E, heat exchanger and F,...

Screw-pressed oil is aUowed to stand to settle out suspended soUds, filtered through plate filter presses, and then pumped to storage. The oil-rich solvent (miscella) from the solvent-extraction process is filtered or clarified, and most of the solvent is removed in a long tube evaporator. FinaUy, the concentrated oil passes through a stripping column where sparging steam is injected to remove the residual solvent. A metric ton of cottonseed yields ca 91... 

In both cases, the carbonate ion concentration increases and eventually equiUbrates in the system, releasing carbon dioxide in the stripping column and thereby reducing product purity. Hence, a small caustic wash tower is employed to remove any carbon dioxide that is Hberated in the stripper. 

The carbon monoxide purity from the Cosorb process is very high because physically absorbed gases are removed from the solution prior to the low pressure stripping column. Furthermore, there is no potential for oxidation of absorbed carbon monoxide as ia the copper—Hquor process. These two factors lead to the production of very high purity carbon monoxide, 99+ %. Feed impurities exit with the hydrogen-rich tail gas therefore, the purity of this coproduct hydrogen stream depends on the impurity level ia the feed gas. 

The absorbate containing the mixed ethyl sulfates is hydroly2ed with enough water to give an approximately 50—60% aqueous sulfuric acid solution. The hydrolysis mixture is separated in a stripping column to give dilute sulfuric acid bottoms and a gaseous alcohol—ether—water mixture overhead. The overhead mixture is washed with water or dilute sodium hydroxide and then purified by distillation (63,65,66,68,69). 

To illustrate this integration analytically, Eq. (22-48) becomes Eq. (22-49) for the case of a stripping column removing a colhgend which is subject to the liuear-equifibrium isotherm T = KC. 

FIG. 22-43 Graphical determination of theoretical stages for a foam-fractionation stripping column. 

By using an anionic collector and external reflux in a combined (enriching and stripping) column of 3.8-cm (1.5-in) diameter with a feed rate of 1.63 ni/n [40 gal/(h ft )] based on column cross section, D/F was reduced to 0.00027 with C JCp for Sr below 0.001 [Shou-feld and Kibbey, Nucl. AppL, 3, 353 (1967)]. Reports of the adsubble separation of 29 heavy metals, radioactive and otheiwise, have been tabulated [Lemlich, The Adsorptive Bubble Separation Techniques, in Sabadell (ed.), Froc. Conf. Traces Heavy Met. Water, 211-223, Princeton University, 1973, EPA 902/9-74-001, U.S. EPA, Reg. 11, 1974). Some separation of N from by foam fractionation has been reported [Hitchcock, Ph.D. dissertation. University of Missouri, RoUa, 1982]. 

The esterified stream, which may contain inhibitors to prevent premature polymerisation, is then passed to a stripping column which separates the methyl methacrylate, methanol and some water from the residue made up of sulphuric acid, ammonium bisulphate and the remainder of the water. The methyl methacrylate is subsequently separated and purified by further distillation. 

Liquid products are withdrawn from plates 9, 16, and 22 as sidestreams. These are contacted with steam in external stripping columns having 4 to 6 plates in order to remove light dissolved hydrocarbons. Since the liquid withdrawn from any plate in a pipe still is in equilibrium with all the lighter vapor passing that plate, it always will contain material which is lower in boiling point than the desired product. 

Tower bottoms-ACN, butadiene, with some butenes and acetylenes - are fed to a recovery/stripping column. The hydrocarbons are taken overhead and then rerun to meet product specifications. The stripping column bottoms, (ACN) is then remrned near the top of the extractive distillation tower. A small slipstream goes to the ACN recovery tower, where solvent is also recovered from the water wash streams. 

The reactions with CO2 and H2S shown are reversed in the stripping column by heating the rich MEA to approximately 245°F at 10 psig. The acid gases evolve into the vapor and are removed from the still overhead. Thus, the MEA is regenerated. 

The normal regeneration temperature in the still will not regenerate heat-stable salts or oxazolidone-2. Therefore, a reclaimer is usually included to remove these contaminants. A side stream of from 1 to 3% of the MEA circulation is drawn from the bottom of the stripping column, This stream is then heated to boil the water and MEA overhead while the heat-stable salts and oxazolidone-2 are retained in the reclaimer. The reclaimer is periodically shut in and the collected contaminants are cleaned out and removed from the system. However, any MEA bonded to them is also lost. 

TliCNC reactions are reversible. DEA reacts with carbonyl sulfide (CUS) and carbon disulfide (CS2) to form compounds that can be regenerated in the stripping column. Therefore, COS and CS2 are removed without a loss i)f DEA. Typically, DEA systems include a carbon filter but do not include a reclaimer. 

The acid-rich potassium carbonate solution from the bottom of the absorber is flashed to a flash drum, where much of the acid gas is removed. The solution then proceeds to the stripping column, which operates at approximately 245 °F and near-atmospheric pressure. The low pressure, combined with a small amount of heat input, drives off the remaining acid gases. The lean potassium carbonate from the stripper is pumped back to the absorber. The lean solution may or may not be cooled slightly before entering the absorber. The heat of reaction from the absorption of the acid gases causes a slight temperature rise in the absorber. 

The example in Figure 7-6 is a simple one in that flashing is sufficiciii to regenerate the solvent. Some solvents require a stripping column jiisi prior to the circulation pump. 

Figure 8-83. Allowable mass velocity for fractionation, absorption, and stripping columns.

Souders, M., Jr., G. G. Brotvn, Fundamental Design of 97. Absorbing and Stripping Columns for Complex Vapors, ... 

Figure 12-4. The European Vinyls Corp. process for producing polyvinyl chloride using suspension polymerization (1) reactor, (2) blow-down vessels (to separate unreacted monomer), (3) stripping column, (4) reacted monomer recovery, (5) slurry centrifuge, (6) slurry drier.

Ni-Si recovery of HP Processes involving cone. H2SO4 processes. Sulphur stripping columns. Distillation columns containing acidic chlorides. Handling acid sludges processes impellers, propeller shafts, fasteners. Demisters in desalination plants refrigerating brines. Salt production. Evaporators steel... 

FIG. 17 Alkylation of benzene with n-chloroparaffins. R, reactor ST, settling tank SC, stripping column C, condensor V, vessel. 

FIG. 19 Formation of hydrochloric acid. SC, stripping column LS, liquid separator DC, distillation column. 

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