Treatment system for recycling high-concentration organic wastewater

Abstract

The utility model relates to the technical field of hazardous waste disposal and resource utilization, in particular to a treatment system for recycling high-concentration organic wastewater. According to the scheme, a mode of combining evaporation and rectification is adopted, after wastewater is preheated, light components are removed through two stages of light component removal towers, heavy components are removed through a heavy component removal tower, and high-boiling residues at the bottom of the tower enter a scraper dryer to be further dehydrated. By adopting the system and the method disclosed by the utility model, the thorough separation of organic matters, salt and water in the wastewater is realized. Compared with the prior art, the device has the advantages that the COD (Chemical Oxygen Demand) value in the wastewater is obviously reduced, two organic matters can be recovered at the same time, and the concentration of the recovered organic matters is high; moreover, the production cost is reduced, the resource recycling is realized, the pollution is reduced, the wastewater generated in the industries of medicines, semiconductors, electronic display, petrochemical engineering, coking, textile printing and dyeing and the like can be effectively treated, and the method is particularly suitable for wastewater which is relatively high in organic matter concentration, complex in component and difficult to biochemically degrade.

Description

TECHNICAL FIELD

[0001] The utility model relates to the technical field of hazardous waste disposal and resource utilization, in particular to a high-concentration organic wastewater resource treatment system. BACKGROUND

[0002] In the pharmaceutical industry, the circuit board industry, the electroplating industry, the oil refining industry or other organic chemical industry, high-concentration organic wastewater (or waste liquid) is often produced, the COD concentration of these organic wastewater is very high, COD is 2000mg / L or even as high as 400000mg / L. In addition, it often contains part of alkaline substances and dissolved salt. Such as the developing, demolding tank liquid of the circuit board industry, the rubber plastic industry reaction kettle cleaning wastewater, the production waste liquid of the organic solvent industry, the alkali residue waste liquid produced by the oil refinery, etc.

[0003] For this kind of organic waste liquid, if biological treatment method is used for treatment, due to the high salt content and high organic matter concentration, it is difficult to cultivate microorganisms, the biochemical effect is poor, and it is often mixed in other wastewater and treated after being diluted by hundreds of times, but the effect is still poor. If chemical oxidation method is used for treatment, such as Fenton oxidation, there are problems such as large amount of reagent addition, high treatment cost, and poor water quality after treatment. If this kind of organic wastewater (or waste liquid) is directly treated by high-temperature incineration, that is, the organic matter is completely decomposed by high temperature, however, the wastewater must be heated to 800 DEG C or higher, otherwise the organic matter cannot be effectively decomposed. The wastewater needs to be heated from room temperature to 800 DEG C, which consumes a large amount of heat, most of which is provided by gas or oil. Therefore, the water content in the organic wastewater has a great influence on the energy consumption of high-temperature incineration. If water and organic matter can be effectively separated, the treatment capacity and treatment cost can be greatly reduced.

[0004] The traditional multi-effect evaporation concentration system can effectively reduce the evaporation energy consumption, but there are the following disadvantages: the gas-liquid separator is used to separate the evaporated organic matter and water, which is equivalent to a theoretical plate of the rectifying column, and the separation efficiency is low. At the same time, due to the high concentration of organic matter, the separation efficiency is further reduced due to the serious entrainment phenomenon, so that the COD of the distilled wastewater is still high, and the distilled water needs to be further treated by biochemical or physical treatment to meet the discharge standard. UTILITY MODEL CONTENTS

[0005] The utility model discloses a kind of high-concentration organic wastewater resource treatment systems to overcome the defects of the above prior art, organically combine evaporation and rectification technology, effectively realize the separation of organic matter and salt in wastewater and water. Reduce subsequent processing cost, realize energy saving and consumption reduction, reduce pollution.

[0006] The purpose of the utility model can be realized by the following technical solutions:

[0007] A high-concentration organic wastewater resource treatment system, comprising a first light removal tower, a second light removal tower, a heavy removal tower, a preheater, and a scraper dryer; the cold side inlet of the preheater is connected with the outlet of a raw material lifting pump, the cold side outlet thereof is connected with the wastewater inlet of the first light removal tower, the hot side inlet thereof is connected with the gas phase pipeline at the top of the heavy removal tower through a pipeline, and the hot side outlet thereof is connected with the hot side inlet of a fifth condenser;

[0008] The gas phase outlet pipeline at the top of the first light removal tower is connected with the hot side inlet of a first condenser, the hot measuring outlet pipeline of the first condenser is connected with the hot side inlet of a second condenser, the hot measuring outlet pipeline of the second condenser is connected with the material inlet of a first product tank, the material outlet at the bottom of the first light removal tower is connected with a first light removal tower circulating pump through a pipeline;

[0009] The gas phase outlet pipeline at the top of the second light removal tower is connected with the hot side inlet of a third condenser, the hot measuring outlet pipeline of the third condenser is connected with the hot side inlet of a fourth condenser, the hot measuring outlet pipeline of the fourth condenser is connected with the material inlet of a second product tank, and the material outlet at the bottom of the second light removal tower is connected with a second light removal tower circulating pump through a pipeline;

[0010] The gas phase outlet pipeline at the top of the heavy removal tower is connected with the hot side inlet of the preheater, the hot measuring outlet pipeline of the preheater is connected with the hot side inlet of the fifth condenser, the hot side outlet pipeline of the fifth condenser is connected with the material inlet of a wastewater tank, the outlet of the wastewater tank is connected with the inlet of a reflux pump in one way as reflux in the tower and with a qualified wastewater main pipeline in the other way, and the material outlet at the bottom of the heavy removal tower is connected with a heavy removal tower circulating pump through a pipeline; the preheater uses secondary steam at the top of the tower to preheat the raw material wastewater in countercurrent.

[0011] The material inlet of the scraper dryer is connected with the heavy removal tower circulating pump, and the material is changed into solid waste salt and secondary steam condensate water after further dehydration; the scraper dryer is further provided with a primary steam inlet and a steam condensate water outlet.

[0012] Further, the outlet pipeline of the first light removal tower circulating pump is divided into two ways, one of which is connected with the tube side inlet of a first light removal heater through a pipeline, and the other of which is connected with the wastewater inlet of the second light removal tower through a pipeline; the tube side outlet of the first light removal heater is connected with the circulating liquid inlet of the first light removal tower through a pipeline; the shell side inlet thereof is connected with the gas phase outlet at the bottom of the second light removal tower, and the shell side outlet thereof is connected with the qualified wastewater main pipeline.

[0013] Further, the outlet pipeline of the secondary light removal tower circulating pump is divided into two routes, one of which is connected with the tube inlet of the secondary light removal tower heater through a pipeline, and the other is connected with the wastewater inlet of the heavy removal tower through a pipeline; the tube outlet of the secondary light removal tower heater is connected with the circulating liquid inlet of the secondary light removal tower through a pipeline; the shell inlet is connected with the gas phase outlet at the bottom of the heavy removal tower, and the shell outlet is communicated with the qualified wastewater main pipeline.

[0014] Further, the outlet pipeline of the secondary light removal tower circulating pump is divided into two routes, one of which is connected with the tube inlet of the secondary light removal tower heater through a pipeline, and the other is connected with the wastewater inlet of the heavy removal tower through a pipeline; the tube outlet of the secondary light removal tower heater is connected with the circulating liquid inlet of the secondary light removal tower through a pipeline; the shell inlet is connected with the gas phase outlet at the bottom of the heavy removal tower, and the shell outlet is communicated with the qualified wastewater main pipeline.

[0015] Further, the primary light removal tower, the secondary light removal tower and the heavy removal tower are all combined devices of evaporators and towers, the lower part of the device is a separator, and the upper part is a rectifying tower; the rectifying tower is filled with high-efficiency structured packing or tower plates.

[0016] Further, the secondary steam at the top of the secondary light removal tower separator is used as the heat source of the primary light removal heater, and after heat exchange in the heater, the secondary steam is condensed into liquid phase and discharged as qualified wastewater.

[0017] The secondary steam at the top of the heavy removal tower separator is used as the heat source of the secondary light removal tower heater, and after heat exchange in the heater, the secondary steam is condensed into liquid phase and discharged as wastewater.

[0018] Further, the heavy removal tower heater uses primary steam as the heat source, and after heat exchange in the heater, the steam is condensed into liquid phase, which can be used as system cleaning water or directly discharged out of the region.

[0019] Further, the operating pressure at the top of the primary light removal tower is-0.08 to-0.06 MPa, the top temperature is 35-50℃, and the bottom heater temperature is 45-60℃; the operating pressure at the top of the secondary light removal tower (8) is-0.07 to-0.04 MPa, the top temperature is 50-70℃, and the bottom heater temperature is 70-80℃; the operating pressure at the top of the heavy removal tower (14) is-0.04 to-0.01 MPa, the top temperature is 60-75℃, and the bottom heater temperature is 85-100℃.

[0020] Correspondingly, the utility model also provides a kind of high concentration organic wastewater resourceization processing method, using the way of evaporation and rectification combination, wastewater is preheated after passing through two-stage light component removal tower, and then the heavy component is removed by heavy component removal tower, and finally further dewatering by scraper dryer, realize the complete separation of organic matter, salt and water in wastewater.Most of the organic matter and other light components are separated from the top of the tower after the high concentration organic wastewater passes through the first light component removal tower;The kettle liquid after light component removal enters the second light component removal tower from the bottom of the tower, and realizes higher removal rate of organic matter and other light components after passing through the second light component removal tower;The material enters the heavy component removal tower from the bottom of the second light component removal tower, and the salt and other heavy components are removed in the heavy component removal tower;The gas phase at the top of the tower is condensed to obtain qualified wastewater, and the bottom of the tower is saturated or supersaturated salt solution, which is further dried and removed of salt in the scraper dryer, and finally qualified wastewater and solid impurities are obtained.

[0021] The high concentration organic wastewater resourceization processing method specifically adopts the following steps:

[0022] (1) raw material preheating: the wastewater raw material exchanges heat with the material from the top of the heavy component removal tower through the preheater, and the preheated raw material enters the first light component removal tower;

[0023] (2) initial light component removal: the secondary steam of the second light component removal tower enters the heater of the first light component removal tower, and the wastewater raw material is gradually gasified after entering the first light component removal tower from the lower separator of the first light component removal tower, and the light component, moisture and heavy component are separated through the rectification section above the separator;An internal condenser is arranged at the upper part of the rectification section of the first light component removal tower, part of the gas phase material in the tower is condensed into liquid phase by the internal condenser, the condensed liquid phase returns to the tower as reflux, and the gas phase material that is not condensed is taken out from the top of the tower as light component, which is further condensed into liquid phase after entering the condenser, and is taken out as light phase product 1;The heavy component at the bottom of the separator enters the separator of the second light component removal tower;

[0024] (3) re-removal of light component: the secondary steam of the heavy component removal tower enters the heater of the second light component removal tower, and the heavy component enters the separator of the second light component removal tower from the bottom of the separator of the first light component removal tower, and is gradually gasified, and the light component, moisture and other heavy components are effectively separated through the rectification section above the separator;An internal condenser is arranged at the upper part of the rectification section of the second light component removal tower, part of the gas phase material in the tower is condensed into liquid phase by the internal condenser, the condensed liquid phase returns to the tower as reflux, and the gas phase material that is not condensed is taken out from the top of the tower as light component, which is further condensed into liquid phase after entering the condenser, and is taken out as light phase product 2;The secondary steam is taken out from the lower separator of the second light component removal tower and enters the heater shell of the first light component removal tower;The heavy component at the bottom of the separator enters the separator of the heavy component removal tower;

[0025] (4) primary recombination components: primary steam from the heater of the de-recombination tower, and the heavy components from the bottom of the secondary de-light tower separator enter the de-recombination tower separator, are gradually gasified, and pass through the rectification section above the separator, the light components are effectively separated from the water and other heavy components, the ascending gas phase material in the tower is discharged from the top, is condensed into a liquid phase by an external preheater and a condenser, and is discharged as qualified waste water; the secondary steam from the lower separator of the de-recombination tower enters the shell side of the secondary de-light tower heater; and the heavy components at the bottom of the separator are salt solutions with low moisture content;

[0026] (5) drying and desalting: the salt solution from the bottom of the de-recombination tower enters a subsequent scraper dryer, is further removed of salt, and is discharged as qualified waste water out of the region. The primary steam is used as the heat source of the scraper dryer, and the steam condensate water can be used as cleaning water of the system or directly discharged out of the region.

[0027] (6) the secondary steam in the primary de-light tower heater, the secondary steam in the secondary de-light tower heater, and the de-recombination tower top discharge are condensed into liquid after being condensed as pre-processed qualified waste water, and are discharged out of the system.

[0028] (7) the secondary steam generated by the secondary de-light tower is used as the heat source of the primary de-light tower heater, the secondary steam of the de-recombination tower is used as the heat source of the secondary de-light tower heater, and the secondary steam at the top of the de-recombination tower is countercurrently heat-exchanged to preheat the feed waste water.

[0029] Further, the secondary steam of the secondary de-light tower is used as the heat source of the bottom heater of the primary de-light tower, the light components in the primary de-light tower are heated and gasified after heat exchange of the heater, are condensed into a liquid phase after being discharged from the top, and are used as light phase product 1; and the secondary steam of the secondary de-light tower is condensed as qualified waste water discharged out of the region.

[0030] Further, the secondary steam of the de-recombination tower is used as the heat source of the bottom heater of the secondary de-light tower, the light components in the secondary de-light tower are heated and gasified after heat exchange of the heater, are condensed into a liquid phase after being discharged from the top, and are used as light phase product 2; and the secondary steam of the de-recombination tower is condensed into a liquid phase and discharged as waste water.

[0031] Compared with the prior art, the utility model has the following beneficial effects:

[0032] The technical core of the utility model is that evaporation and rectification technologies are combined, effective separation of organic matter and salt from water is realized, and the organic matter in waste water is used as a product resource. Research on a large-scale industrialized treatment process for high-concentration organic waste water in line with the concepts of energy saving, efficiency improvement and environmental protection is a future development trend. The rectification process can efficiently separate various effective components in waste water, obtain organic product that can be recycled, and has small occupied area, low investment cost and simple operation, and meets the concepts of energy saving, efficiency improvement and environmental protection.

[0033] The utility model discloses a method for treating wastewater produced in petrochemical industry, coking, pharmaceutical industry and textile printing and dyeing industry, and is especially suitable for treating wastewater with high organic matter concentration (COD≥2000mg / L), complex composition and difficult biodegradation. Compared with traditional multi-effect evaporation concentration, the treatment method can not only significantly reduce the COD value of the wastewater, but also can recover various organic matters with high concentration, reduce production cost, realize resource recycling and reduce pollution. BRIEF DESCRIPTION OF DRAWINGS

[0034] Figure 1 The utility model discloses a process flow chart of a specific embodiment.

[0035] In the drawing: 1, raw material lifting pump; 2, first light removal tower; 3, first condenser; 4, second condenser; 5, product tank 1; 6, first light removal tower circulating pump; 7, first light removal tower heater; 8, second light removal tower; 9, third condenser; 10, fourth condenser; 11, product tank 2; 12, second light removal tower circulating pump; 13, second light removal tower heater; 14, heavy removal tower; 15, preheater; 16, fifth condenser; 17, wastewater tank; 18, heavy removal tower circulating pump; 19, heavy removal tower heater; 20, vacuum buffer tank; 21, vacuum pump; 22, scraper dryer; 23, heavy removal tower backflow pump. DETAILED DESCRIPTION

[0036] The utility model will be described in detail in combination with specific embodiments. The following embodiments will help the person skilled in the art to further understand the utility model, but do not limit the utility model in any form. It should be pointed out that for ordinary skilled in the art, without departing from the concept of the utility model, a number of variations and improvements can be made. These all belong to the protection scope of the utility model.

[0037] The utility model relates to a kind of high-concentration organic wastewater resourceization's processing system, and the separation of organic matter and salt etc.

[0038] Please refer to Figure 1 The processing system structure schematic drawing of the utility model mainly includes primary light removal tower 2, secondary light removal tower 8, heavy removal tower 14, preheater 15, scraper dryer 22.The cold side import of preheater 15 is connected with the export of raw material lifting pump 1, its cold side export is connected with the wastewater import of primary light removal tower 2, its hot side import is connected with the top gas phase pipeline of heavy removal tower 14 by pipeline, and its hot side export is connected with the hot side import of fifth condenser 10.

[0039] In the embodiment, the gas phase export pipeline of primary light removal tower 2 top is connected with the hot side import of first condenser 3, the hot measuring export pipeline of first condenser 3 is connected with the hot side import of second condenser 4, and the hot measuring export pipeline of second condenser 4 is connected with the material import of product tank 5;The material export of primary light removal tower 2 bottom is connected with primary light removal tower circulating pump 6 by pipeline;The export pipeline of primary light removal tower circulating pump 6 is divided into two routes, one is connected with the pipe passage import of primary light removal heater 7 by pipeline, and the other is connected with the wastewater import of secondary light removal tower 8 by pipeline;The pipe passage export of primary light removal heater 7 is connected with the circulating liquid import of primary light removal tower 2 by pipeline;Its shell course import is connected with the gas phase export of secondary light removal tower 8 bottom, and its shell course export is communicated with qualified wastewater main pipe.

[0040] In the embodiment, the gas phase outlet pipeline of the secondary light removal column 8 is connected with the hot side inlet of the third condenser 9, the hot side outlet pipeline of the third condenser 9 is connected with the hot side inlet of the fourth condenser 10, the hot side outlet pipeline of the fourth condenser 10 is connected with the material inlet of the product tank 11; the bottom material outlet of the secondary light removal column 8 is connected with the secondary light removal column circulating pump 6 through a pipeline; the outlet pipeline of the secondary light removal column circulating pump 6 is divided into two routes, one route is connected with the tube side inlet of the heater 13 through a pipeline, and the other route is connected with the waste water inlet of the heavy removal column 14 through a pipeline; the tube side outlet of the heater 13 is connected with the circulating liquid inlet of the secondary light removal column 8 through a pipeline; and the shell side inlet is connected with the gas phase outlet at the bottom of the heavy removal column 14, and the shell side outlet is communicated with the qualified waste water main pipeline.

[0041] In the embodiment, the gas phase outlet pipeline of the secondary light removal column 8 is connected with the hot side inlet of the third condenser 9, the hot side inlet of the third condenser 9 is connected with the hot side inlet of the fourth condenser 10, the hot side outlet pipeline of the fourth condenser 10 is connected with the material inlet of the product tank 11; the bottom material outlet of the secondary light removal column 8 is connected with the secondary light removal column circulating pump 6 through a pipeline; the outlet pipeline of the secondary light removal column circulating pump 6 is divided into two routes, one route is connected with the tube side inlet of the heater 13 through a pipeline, and the other route is connected with the waste water inlet of the heavy removal column 14 through a pipeline; the tube side outlet of the heater 13 is connected with the circulating liquid inlet of the secondary light removal column 8 through a pipeline; and the shell side inlet is connected with the gas phase outlet at the bottom of the heavy removal column 14, and the shell side outlet is communicated with the qualified waste water main pipeline.

[0042] In the embodiment, the gas phase outlet pipeline of the secondary light removal column 8 is connected with the hot side inlet of the third condenser 9, the hot side inlet of the third condenser 9 is connected with the hot side inlet of the fourth condenser 10, the hot side outlet pipeline of the fourth condenser 10 is connected with the material inlet of the product tank 11; the bottom material outlet of the secondary light removal column 8 is connected with the secondary light removal column circulating pump 6 through a pipeline; the outlet pipeline of the secondary light removal column circulating pump 6 is divided into two routes, one route is connected with the tube side inlet of the heater 13 through a pipeline, and the other route is connected with the waste water inlet of the heavy removal column 14 through a pipeline; the tube side outlet of the heater 13 is connected with the circulating liquid inlet of the secondary light removal column 8 through a pipeline; and the shell side inlet is connected with the gas phase outlet at the bottom of the heavy removal column 14, and the shell side outlet is communicated with the qualified waste water main pipeline.

[0043] Further, the primary light removal column 2, the secondary light removal column 8 and the heavy removal column 14 are all combined devices of evaporators and columns, the lower part of the device is a separator, and the upper part of the separator is a rectifying column.

[0044] Further, the secondary steam at the top of the secondary light removal column separator is used as the heat source of the primary light removal heater 7 at the bottom of the primary light removal column, and after heat exchange through the heater, the secondary steam is condensed into liquid phase and discharged as qualified waste water.

[0045] Further, the secondary steam at the top of the heavy removal column separator is used as the heat source of the heater 13 at the bottom of the secondary light removal column, and after heat exchange through the heater, the secondary steam is condensed into liquid phase and discharged as waste water.

[0046] Further, the heavy component removal column bottom heater 19 uses primary steam as a heat source, and after heat exchange through the heater, the steam is condensed into liquid phase, which can be used as system cleaning water or directly discharged out of the system.

[0047] Further, the heavy component removal column upper portion is provided with a preheater 15, which uses secondary steam from the column top to preheat the raw material wastewater in countercurrent.

[0048] Embodiment

[0049] The method for treating high-concentration organic wastewater by using the high-concentration organic wastewater resource treatment system provided by the present application has the process flow as shown in Figure 1 The method for treating high-concentration organic wastewater by using the high-concentration organic wastewater resource treatment system provided by the present application has the process flow as shown in

[0050] A pharmaceutical wastewater treatment project, with a design water treatment capacity of 13 m 3 / d, the wastewater is from a penam antibiotic reaction synthesis section. The wastewater is composed of ethyl acetate, tetrahydrofuran, DMF, potassium dihydrogen phosphate and water. The total organic content is 38%, the salt content is 2%, and the rest is water. The specific process is as follows:

[0051] (1) Raw material preheating: the raw material is preheated by a preheater and heat-exchanged with gas-phase material from the heavy component removal column top, and the preheated raw material enters the primary light component removal column;

[0052] (2) Initial light component removal: secondary steam at the bottom of the secondary light component removal column enters the heater of the primary light component removal column, and the raw material enters the primary light component removal column from the separator of the primary light component removal column, is gradually gasified, and realizes effective separation of light components such as organic matter, water and other heavy components through the rectification section above the separator. An inner condenser is arranged at the upper portion of the rectification section of the primary light component removal column, a part of the ascending gas-phase material in the column is condensed into liquid phase by the inner condenser and returns to the column as reflux, and a part of the gas phase is taken out as the column top light component (a mixture of tetrahydrofuran, ethyl acetate and water); the heavy component at the bottom of the separator enters the separator of the secondary light component removal column; the primary light component removal column top pressure is -0.08 to -0.06 MPa, the column top temperature is 35 to 50℃, and the bottom heater temperature is 45 to 60℃;

[0053] (3) Secondary light component removal: secondary steam from the heater of the secondary light component removal tower enters, the material from the bottom of the primary light component removal tower separator enters the secondary light component removal tower separator, is gradually gasified, and is separated from the light components such as organic matter, moisture and other heavy components through the rectifying section above the separator, an internal condenser is arranged at the upper part of the rectifying section of the secondary light component removal tower, part of the gas phase material rising in the tower is condensed into liquid phase by the internal condenser and returns to the tower as reflux, part of the gas phase is taken out as the light component (a mixture of tetrahydrofuran, ethyl acetate and water) at the top of the tower; the secondary steam is taken out from the lower separator of the secondary light component removal tower and enters the shell side of the primary light component removal tower heater; the heavy components at the bottom of the separator enter the heavy component removal tower separator, the pressure at the top of the secondary light component removal tower is-0.07MPa to-0.04MPa, the temperature at the top of the tower is 50℃ to 70℃, and the temperature of the bottom heater is 70℃ to 80℃;

[0054] (4) Primary heavy component removal: 0.3MPa saturated steam enters from the heater of the heavy component removal tower, the material from the bottom of the secondary light component removal tower separator enters the heavy component removal tower separator, is gradually gasified, and is separated from the light components such as organic matter, moisture and other heavy components through the rectifying section above the separator, the gas phase material rising in the tower is discharged from the top of the tower, is condensed into liquid phase by an external preheater and a condenser, part of the liquid phase returns to the tower as reflux, and part of the liquid phase is taken out as the light component (COD standard wastewater (organic matter <200ppm)) at the top of the tower; the heavy components at the bottom of the separator are potassium dihydrogen phosphate salt solution with low moisture content, the pressure of the heavy component removal tower is-0.04MPa to-0.01MPa, the temperature at the top of the tower is 60℃ to 75℃, and the temperature of the bottom heater is 85℃ to 100℃;

[0055] (5) Drying and desalination: the salt solution at the bottom of the heavy component removal tower enters the scraper dryer to further remove salt, and finally qualified wastewater and solid impure salt are obtained, and the condensate water of the secondary steam generated in the drying process is discharged as qualified wastewater;

[0056] (6) The condensate water of the secondary steam in the shell side of the primary light component removal tower heater, the condensate water of the secondary steam in the shell side of the secondary light component removal tower heater, the condensate water of the heavy component removal tower top discharge and the condensate water of the secondary steam generated by the scraper dryer are all qualified wastewater after pretreatment and are discharged from the system.

[0057] (7) The condensate water of the primary steam used in the drying process of the scraper dryer is discharged as qualified wastewater or is used for cleaning the system.

[0058] In the utility model, if no special instruction, all refer to the weight percentage; if no special instruction, all refer to the gauge pressure.

[0059] The specific embodiments of the present application are described above. It should be understood that the present application is not limited to the specific embodiments described above, and various modifications or changes can be made by those skilled in the art within the scope of the claims, which do not affect the essential content of the present application.

Claims

1. A high-concentration organic wastewater resource treatment system, comprising a first light removal column (2), a second light removal column (8), a heavy removal column (14), a preheater (15), and a scraper dryer (22); characterized in that: the cold side inlet of the preheater (15) is connected to the outlet of a raw material lifting pump (1), the cold side outlet thereof is connected to the wastewater inlet of the first light removal column (2), the hot side inlet thereof is connected to the overhead gas phase pipeline of the heavy removal column (14) through a pipeline, and the hot side outlet thereof is connected to the hot side inlet of a fifth condenser (16); the gas phase outlet pipeline at the top of the first light removal column (2) is connected to the hot side inlet of a first condenser (3), the hot side outlet pipeline of the first condenser (3) is connected to the hot side inlet of a second condenser (4), the hot side outlet pipeline of the second condenser (4) is connected to the material inlet of a first product tank (5), and the material outlet at the bottom of the first light removal column (2) is connected to a first light removal column circulating pump (6) through a pipeline; the gas phase outlet pipeline at the top of the second light removal column (8) is connected to the hot side inlet of a third condenser (9), the hot side outlet pipeline of the third condenser (9) is connected to the hot side inlet of a fourth condenser (10), the hot side outlet pipeline of the fourth condenser (10) is connected to the material inlet of a second product tank (11), and the material outlet at the bottom of the second light removal column (8) is connected to a second light removal column circulating pump (12) through a pipeline; the gas phase outlet pipeline at the top of the heavy removal column (14) is connected to the hot side inlet of the preheater (15), the hot side outlet pipeline of the preheater (15) is connected to the hot side inlet of the fifth condenser (16), the hot side outlet pipeline of the fifth condenser (16) is connected to the material inlet of a wastewater tank (17), the outlet of the wastewater tank (17) is divided into two paths, one of which is connected to the inlet of a heavy removal column backflow pump (23) as the backflow in the column, and the other of which is connected to a qualified wastewater main pipeline, and the material outlet at the bottom of the heavy removal column (14) is connected to a heavy removal column circulating pump (18) through a pipeline; the material inlet of the scraper dryer (22) is connected to the heavy removal column circulating pump (18), the material is further dehydrated to become solid waste salt and secondary steam condensate water, and the scraper dryer (22) is further provided with a primary steam inlet and a steam condensate water outlet. The outlet pipeline of the first light removal column circulating pump (6) is divided into two paths, one of which is connected to the tube side inlet of a first light removal column heater (7) through a pipeline, and the other of which is connected to the wastewater inlet of the second light removal column (8) through a pipeline; the tube side outlet of the first light removal column heater (7) is connected to the circulating liquid inlet of the first light removal column (2) through a pipeline, the shell side inlet thereof is connected to the gas phase outlet at the bottom of the second light removal column (8), and the shell side outlet thereof is in communication with the qualified wastewater main pipeline. ​ ​ ​ ​ 2. The high concentration organic wastewater resourceful treatment system according to claim 1, characterized in that, ​ 3. The high concentration organic wastewater resourceful treatment system according to claim 1, characterized in that, The outlet pipeline of the secondary light removal tower circulating pump (12) is divided into two routes, one of which is connected with the tube side inlet of the secondary light removal tower heater (13) through a pipeline, and the other is connected with the wastewater inlet of the heavy removal tower (14) through a pipeline; the tube side outlet of the secondary light removal tower heater (13) is connected with the circulating liquid inlet of the secondary light removal tower (8) through a pipeline; the shell side inlet is connected with the gas phase outlet at the bottom of the heavy removal tower (14), and the shell side outlet is communicated with the qualified wastewater main pipeline.

4. The high concentration organic wastewater resourceful treatment system according to claim 1, characterized in that, The outlet pipeline of the heavy removal tower circulating pump (18) is divided into two routes, one of which is connected with the tube side inlet of the heavy removal tower heater (19) through a pipeline, and the other is connected with the material inlet of the scraper dryer (22) through a pipeline; the tube side outlet of the heavy removal tower heater (19) is connected with the circulating liquid inlet of the heavy removal tower (14) through a pipeline; the shell side inlet is communicated with saturated steam, and the shell side outlet is steam condensate water, which can be used as system cleaning water or directly discharged out of the boundary area.

5. The high concentration organic wastewater resourceful treatment system according to claim 1, characterized in that, The primary light removal tower (2), the secondary light removal tower (8) and the heavy removal tower (14) are all combined devices of evaporators and towers, the lower part of which is a separator and the upper part of which is a rectifying tower; the rectifying tower is filled with high-efficiency structured packing or trays.

6. The high concentration organic wastewater resourceful treatment system according to claim 1, characterized in that, The secondary steam at the top of the secondary light removal tower separator is used as the heat source of the primary light removal heater (7), and after heat exchange in the heater, the secondary steam is condensed into liquid phase and discharged as qualified wastewater; The secondary steam at the top of the heavy removal tower separator is used as the heat source of the secondary light removal heater (13), and after heat exchange in the heater, the secondary steam is condensed into liquid phase and discharged as wastewater.

7. The high concentration organic wastewater resourceful treatment system according to claim 1, characterized in that, The heavy removal tower heater (19) uses primary steam as the heat source, and after heat exchange in the heater, the steam is condensed into liquid phase, which can be used as system cleaning water or directly discharged out of the boundary area.

8. The high concentration organic wastewater resourceful treatment system according to claim 1, characterized in that, The operating pressure at the top of the primary light removal tower (2) is-0.08 to-0.06 MPa, the top temperature is 35-50℃, and the bottom heater temperature is 45-60℃; the operating pressure at the top of the secondary light removal tower (8) is-0.07 to-0.04 MPa, the top temperature is 50-70℃, and the bottom heater temperature is 70-80℃; the operating pressure at the top of the heavy removal tower (14) is-0.04 to-0.01 MPa, the top temperature is 60-75℃, and the bottom heater temperature is 85-100℃.

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