Effluent treatment condensation

Provision of sufficiently large buffer tanks for storage of spilled cooking and recovery liquors and dirty condensates to prevent sudden peaks of loading and occasional upsets in the external effluent treatment plant... 

Clearly, one option to reduce the add-on is to use high-efficiency size formulations. However, there is a limit to what can be achieved by this approach. Even if the add-on is reduced to only 5%, the pollution load is still substantial. The two main options to facilitate disposal are (a) recovery of size polymers and (b) biological effluent treatment. Recovery of size polymers, particularly from water-soluble synthetic sizes, is based on extraction washing using the minimum quantity of water. Recovery rates in the region of 50% have been quoted for polyfvinyl alcohol) and carboxymethylcellulose size formulations. It is necessary to apply one of three concentration techniques precipitation, condensation or ultrafiltration [205]. 

As the inert gas passes through the system, it becomes humidified, removing the water of reaction from the reaction mixture. Most of the energy required for the gas humidification comes from the heat of nitration. The wet gas is condensed and the inert gas is recycled to the nitrator. The condensed organic phase is recycled to the nitrator while the aqueous phase is sent to effluent treatment. The reaction mixture is phase separated and the sulfuric acid is returned to the nitrator. 

The first large scale application of ion exchange to effluent treatment was in the recovery of water, ammonia, and basic copper sulfate from the waste streams encountered in the cuprammonium rayon process. Originally a phenolic type condensation resin was employed, but more recently carboxylic acid acrylic-based exchangers have been introduced. A similar process exists for zinc recovery from the spinning acids of viscose rayon plants, except that in this operation a sulfonic acid resin is employed. 

Another example could be the cooling or condensation of particulate laden gases or vapours. It is possible to cool the hot gas or condense the vapours by direct contact with a cold liquid, usually water. Although this might eliminate particulate fouling of a cooler and the associated cleaning costs, it could generate other costs for effluent treatment or the need to separate the condensate from the coolant phase. The latter may not be a problem if the two liquids are immiscible. 

Removal of oil and hydrocarbon contaminations from recycled steam condensate for boiler feed water Reduction of total organic halogens and adsorbable organic halogens in industrial reserves of contaminated groundwater Process effluent treatment to meet the environmental legislation Removal of residual ozone and control of chloramine levels... 

Confirm working of all safety devices, safety interconnections, overload trip settings, working of effluent treatment plant (along with availability of chemicals for treatment) DG sets, cooling systems for reactors and condensers lire fighting pumps, gas detectors, etc. Clean (flush) all the pipelines and ducts. Check all other equipments required for the particular plant. All instmments and process controllers shall be calibrated and tested. 

Plant expansion shall be carried out with more attention to safety since some of the existing systems may get overloaded such as conveyors for materials, refrigeration plants, electrical main bus bars, cables, incoming transformer, pressure vessels, heat exchangers, condensers, effluent treatment plants, and hoists even when operated carefully—because they may be already operating near their maximum capacity— and this can create dangerous situations. 

The VCM content of PVC suspension after stripping is normally very low. In the case of latex, stripping is more difficult and the residual VCM content depends on a variety of parameters, for instance emulsifier content and type, latex particle size, latex stability, the recipe and the requirements of resin end properties. When steam is used for stripping, the overhead steam containing recovered VCM is condensed. The condensate can be returned to the stripping system, or can be transferred to the water stripper of the effluent treatment or other sections of the process, in order to recover contained VCM and thus to prevent VCM emissions from this effluent. In all cases, the non-condensed overhead gas containing stripped VCM is collected in a recovery unit. 

Particular effluents, FCC condensates and spent caustic, whose high pollution level (S , phenols) requires a specific pretreatment sequence. Sending them into the general WW would throw off treatment or make it much more expensive. 

If steam is used as stripping agent, either live steam or a reboiler can be used. The use of live steam increases the effluent volume. The volatile organics are taken overhead, condensed, and recycled to the process, if possible. If recycling is not possible, then further treatment or disposal is necessary. 

Temperature and Humidity When adsorption, absorption, or condensation is employed, the lowest inlet gas temperature is desirable. Adsorbent and absorbent capacities generally increase with the decreasing gas temperature. High waste-gas temperatures may preclude the use of adsorption or condensatit)n due to the cost of chilling. Thermal and catalytic oxidation benefit from a hot effluent gas stream, as that reduces the supplementary fuel requirement. In biological treatment, a waste-gas temperature of near 37 °C is ideal. 

Another cleaning process for the removal of tetrahydrothiophene process uses an advanced oxidation technique, consisting of water treatment by UV-radiation in combination with a dosage of hydrogen peroxide [1392]. It is possible to keep the concentrations of odorant and condensate in the effluent below 0.1 ppb. 

The two main sources of air pollutants that may be emitted from basic wastewater treatment plant operations are pulping condensates and bleach plant effluent. The pulping condensates may include total reduced sulfur (TRS) compounds as well as volatile organic compounds (VOCs) such as methanol. The primary pollutants of concern for the bleach plant effluent are chloroform and methanol. Any volatile compounds that could be released as air emissions from basic wastewater treatment plant operations are relatively minor and are generally not subject to specific regulation.65-66... 

According to the literature [3,17,33], the heterogeneous nature of fertilizer production plants precludes the possibility of presenting a typical case study of such a facility. Nevertheless, the wastewater flows, the characteristics, and the treatment systems for a phosphoric acid and N-P-K fertilizer plant were parts of a large fertilizer manufacturing facility. The full facility additionally included an ammonia plant, a urea plant, a sulfuric acid plant, and a nitric acid plant. The typical effluent flows were 183 m /hour (806 gpm) from the phosphoric plant and 4.4 m /hour (20 gpm) from the water treatment plant associated with it, whereas in the N-P-K plant they were 420 m /hour (1850 gpm) from the barometric condenser and 108 m /hour (476 gpm) from other effluent sources. 

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