SU685878A2 - Waste water open-flame disinfection method - Google Patents

Description

(54) METHOD FOR WATER DRAINAGE

The invention relates to the fire disposal of wastewater polluted with organic and mineral substances.

Basically auth. St. No. 548749 describes a method of fire disposal of waste water, including supply of evaporated waste water for incineration, separation of high-temperature products of fire disposal for a series of streams, pre-evaporation of the initial waste water at a progressive stage, stripping patterns, themes, themes, flow patterns, matching straps, matching patterns, themes, themes, temper lines, flow patterns, matching straps, matching straps, pre-steaming patterns, matching straps, fire patterns, strips, matching straps, pre-steaming patterns, matching straps. one of the streams of fire neutralization products in the first stage of evaporation, and the rest - on the calcination of the gas-vapor mixtures. Outgoing from the respective evaporation stages, and the supply of hot gases from the calcining steps to the next evaporation stage 1.

In fire disposal of wastewater containing, along with mineral and low-boiling organic substances, high-boiling organic substances (glycerin, sodium colts, organic acids, phenols, etc.) in reduced concentrations (i.e. in batches of concentrations that after pre-evaporation of waste, the latter are converted into liquids with high heat of combustion (1000 kcal / kg).

Claims (1)

This method has the disadvantage of the significant loss of mineral flue gas from the combustion stage, caused by the increased temperature of the process of disposal of evaporated effluent. The temperature level of the process in the known method 12OO1350 C is determined by the magnitude of the calorimetric temperature of the evaporated runoff, which allows the combustion process to be carried out almost autogenously with a small addition of additional fuel. The supply to the combustion stage is necessary to ensure the sustainability of the process of igniting and burning the organic substances contained in the evaporated wastewater, as well as to create a swirling stream of high-temperature flue gases, allowing for efficient centrifugal separation. The chain of the invention is to increase the efficiency and reliability of the process of disposal of wastewater containing, along with mineral and low boiling point substances, high boiling point organic compounds at their high initial concentration. The goal is achieved in that according to the proposed method, the evaporated waste water after the last evaporation stage is additionally directed to the corresponding calcination steps, from which the melt of mineral impurities is removed, and injected into the incineration stage of the original wastewater. The drawing shows an installation diagram explaining the proposed method. The scheme includes stage 1 of burning, fire disposal of stream 2 of one stripped off waste water, calcining steps 3 and 4 for calcining flows 5 and 6 of one stripped of waste water, line 1 of one stripped of waste water after the last stage 8 of evaporation, stream 9 of High Temperature gases from the stage calcining 4 stream 10 of partially evaporated waste water from stage 11 of evaporation and stream 1 of a gas-vapor mixture from the same stage of evaporation, stream 13 of partially evaporated waste water, stream 14 of High-temperature gases from calcination stage 3, stage 15 of evaporation for evaporated 16 flow chart of the initial waste water streams 17 19 .vysokotemperaturnyh products Vågå heat sterilization, the steam-gas mixture stream 20, stream 21 portion of the original one-hundred-water. The operation of the plant according to the proposed method is carried out as follows. Line 7 of the evaporated wastewater after the last stage of evaporation 8 is divided into parallel streams 2, 5, 6. Stream 2 is sent to the burning stage 1, where part of the stream 21 of the original wastewater is also supplied. At the stage of combustion, streams 21 and 2 of the initial and one stripped waste WATER are subjected to fire treatment, organic impurities burn out, and mineral substances are trapped in an overwhelming amount and released as a melt, which is facilitated by a reasonable temperature level, the process of neutralization rv 1000-1100 ° C, driven by entering part of the wastewater. High-temperature products of fire decontamination, derived from step 1, are divided into a number of parallel streams. The stream 17 is directed to the evaporation stage 15, where a part of the stream 16 of the feed from the fine water is introduced. Here, due to the heat of flow 17, part of the moisture is removed from the low-boiling organic pollutants, which, together with the vapor-gas stream 20, leave the evaporation stage 15 to the calcination stage 3, where the high-temperature disposal products stream 19 and the evaporated waste water stream 5 are directed. Due to the heat of stream 19, the volatilization of volatile impurities from stream 20 and the firing deactivation of stream 5 of the evaporated effluent with the trapping and release in the form of a melt of mineral impurities contained in the specified stream of evaporated waste water. High-temperature gases from stage 3 are transferred as a heat carrier to the second stage of evaporation 11, where a stream 13 of partially evaporated wastewater is introduced. Here, too, a part of the moisture is evaporated and the remaining part of the low boar organic contaminants are distilled off, which are sent by stream 12 to the next calcination stage 4. Here, the heat purity 18 of the high-temperature neutralization products are introduced as a heat carrier. In addition, stream 6 of the evaporated wastewater is introduced here. The process in stage 4 is similar to the process in stage 3 and also allows the removal of mineral impurities from stream 6 as a melt. Stream 9 of high-temperature gases enters the last stage of evaporation 8, where stream 1O of wastewater is directed, in which low-boiling organic impurities are already missing, which may lead to pollution of the atmosphere. In this stage, the evaporation from the waste water due to the heat of the gas stream 9 evaporates a certain amount of moisture and the final evaporated waste water (7) containing only high-boiling organic and mineral pollutants enters the fire neutralization at the incineration stage 1 and the calcining stage 3 and 4 . Flow separation of one stripped off waste water with a high concentration of high-boiling organic semectB on a series of parallel flows with the subsequent fire separation of these streams, which are close in heat of combustion and calories the metric temperature of burning to a combustible waste, on the steps of calcination, to which low-calorie streams of the steam-gas mixture from the stage of evaporation of wastewater are also served:., allows to organize the process of neutralization at a moderate temperature level, which provides mineral deposits contained in the evaporated wastewater , in vice melt. At the incineration stage, for this purpose, the source wastewater is introduced into the kiln with a relatively low calorimetric burning temperature. The ratio of the streams of one stripped off wastewater supplied to the calcination stages is selected from the conditions necessary to neutralize and reliably release the melt temperatures in the calcination stages. Example. ZOOO kg / h of waste water containing 5% methanol, 10% glycerol and 5% salt is subject to fire neutralization. After evaporation during the evaporation stages, this wastewater contains 30% glycerol, 15% salt and 55% water. When using the known method (No. 548749), after feeding one of the evaporated waste waters to the burning stage 1 (cyclone furnace), a temperature of 13OO C develops there, which leads to the complete removal of No CE. with flue gases in the form of fine (4 3.-micron) dust. In the proposed method, one of the stripped effluents (x 900 kg / h) is divided into a number of streams in a ratio of 4: 2: 3. The first stream in the amount of 40O kg / h is given for incineration, and the second (20O kg / h) and the third (ZOO kg / h) is in the pro- cedure stage. Zyhgani is also fed to the zoo kg / h of initial wastewater. When burning 100 kg / h of additional fuel and firing the original and one-stripped waste water in a cyclone furnace, the temperature of the exhaust gases is 1 ° C. The gaseous gas of 2300 nm / h is divided into three streams in a ratio of 1: 3: 6 The smallest stream (230) is introduced to the evaporation stage 15, where 116 kg / h of water and 6O kg / h of methanol are evaporated. From the residue level, 37O nm / h of the gas-vapor mixture with a temperature of 80 ° C comes out and poreite enters, calcinations 3, 6.90 high-temperature (1000 ° C) fire neutralization products and 200 kg / h of evaporated waste water are supplied to the bath. In the calcining stage 3 due to the oxidation of 60 kg / h of methanol, the oxidation contained in the UPA. The waste water of 60 kg / h of glycerin, as well as the heat of the corresponding product of fire disposal, the temperature of the waste gas is 990 ° C, which is sufficient for complete oxidation of organic substances (glycerol and methane) and reliable melt production by NSb. . From this stage, 1,740 mm / h of hot 1x gases with a temperature of 990 ° C are released, which are directed to the evaporation stage 11, where another 950 kg / h of water and the remaining 9O kg / h of methanol are evaporated. The vapor-gas mixture in the amount of 29OO aa of the evaporation stage 11 is fed to the calcining stage 4, and 9300 kg / h of waste water, already containing methanol, to the last stage 8 of evaporation. At the calcining stage 4, 300 kg / h of the evaporated waste water is introduced. Owing to the oxidation of 90 kg / h of methanol, 9O kg / h of hfrärn, and the heat of the corresponding stream of high-temperature combustion products (137O nm7h), ZOO is cleared of wastewater / kg and an effective conditions of formation and extraction of the melt are created. The temperature of the hot gases at the exit of this stage is 920. Further, this gases in quantity 55OO. nm / h is fed to the final evaporation stage, where another 4OO kg / h of water is evaporated due to their heat. Thus, favorable conditions are created at the burning stage and in the calcination stage for the removal of the NaCe melt. - temperature 95О-1ООО С and availability of the necessary moment of the quantity of gas flow movement for creating the effect of centrifugal separation. The invention of the method of fire disposal; accurate water containing organic minerals by author. St. O 548749, characterized in that, in order to ensure the reliability of the decontamination process of accurate water containing, along with low-boiling substances, high-boiling organic substances at their high initial concentration, after one last evaporation stage, the evaporated waste iodine is additionally directed to the appropriate stages of calcination, from which the melt is drawn / TanAute 6 , 7 88. mineral impurities, and part of the original wastewater is introduced into the incineration stage. Sources of information taken into account during the examination 1. USSR Author's Certificate No. 548749, cd. F 23 G 7 / OO, 1974. Spread AB 19№ -eleven Is. 17 / V Stachna - " ioaa sixteen  13 .ten