CN212315829U - Processing system of high salt organic waste water in ion exchange resin production - Google Patents

Abstract

The utility model discloses a processing system of high salt organic waste water in ion exchange resin production. Aims to solve the problem of environmental pollution caused by methylamine/ethylamine, salt and the like in the high-salt organic wastewater produced by ion exchange resin. The treatment system of the utility model comprises an amine recovery treatment device, an oxidation and precipitation device and an evaporation recovery device which are connected in sequence; the amine recovery treatment device comprises an amine gasification tower, a multi-stage condensation mechanism, a multi-stage negative pressure absorption mechanism and a tail gas absorption tower which are sequentially communicated; the oxidation and precipitation device comprises an oxidation reaction tank, a flocculation mechanism and a precipitator which are sequentially communicated; the evaporation recovery device comprises a waste liquid storage tank and an evaporator which are sequentially communicated. The utility model is easy to operate and control, and saves energy consumption; the method has the advantages that the organic matters and salts are recovered, the wastewater is treated at the same time, the treated wastewater can be reused for production, no wastewater or waste gas is generated in the treatment process, the combined production and continuous production can be realized, the method is environment-friendly, and the economic benefit and the social benefit are extremely remarkable.

Description

Processing system of high salt organic waste water in ion exchange resin production

Technical Field

The utility model relates to a waste water treatment technical field, concretely relates to processing system of high salt organic waste water in ion exchange resin production.

Background

The waste water produced by ion exchange resin is chemical waste water with high pollution load, strong acidity, complex components and great treatment difficulty.

In the production process of anion resin such as ion exchange resin 201 x 7/D201/D301, resin white balls need amination after chlorination. Amination is also required when raw materials dimethylamine is produced by adopting a one-step method or a two-step method for PZ (zinc dimethyldithiocarbamate) in the rubber accelerator industry and raw materials diethylamine is produced by ZDC (zinc diethyldithiocarbamate) series.

Amination is carried out by adopting methylamine/ethylamine, and the content of the residual methylamine/ethylamine in the aminated mother liquor is 0.7-2.0%. Wherein trimethylamine is decomposed into dimethylamine under aerobic high temperature; while low concentration dimethylamine has a more unpleasant fish smell, higher concentrations can cause strong irritation to the eyes and respiratory tract. Therefore, if the amination mother liquor is not subjected to methylamine/ethylamine recovery, the amination mother liquor directly enters a wastewater treatment system or is discharged into a water body, so that environmental pollution is caused, the treatment difficulty of the wastewater treatment system is increased, and resources are wasted, so that effective treatment and recovery measures need to be taken.

At present, the methylamine/ethylamine wastewater is treated by adopting an incineration method in China mostly, but a low-concentration methylamine/ethylamine aqueous solution cannot be combusted and a large amount of heat must be provided for the combustion of the methylamine/ethylamine aqueous solution, so that the combustion treatment energy consumption is large and the cost is high; in addition, the amination waste water can generate harmful gases such as nitrogen dioxide, nitric oxide, carbon dioxide, carbon monoxide and the like after combustion, thereby causing secondary pollution to air.

In addition, other processing methods are as follows: the steam stripping method, the chemical precipitation method, the complex extraction method, the ion exchange method and the dimethylamine hydrochloride all have the defects of high recovery cost, large investment and running power consumption and the like, and are not suitable for industrial production treatment.

In addition, the wastewater generated in the production process of the ion exchange resin has high salt content, and the total salt content is 5-12%; the main components of the salt comprise sodium chloride, sodium sulfate and other trace ferric chloride, zinc sulfate and the like, wherein the sodium chloride content in the salt is 95-96%, the other sodium sulfate content is 2-3%, the ferric chloride content and the zinc sulfate content are 1-2%, and the rest is insoluble oligomer less than 1%. If the waste water is not recycled, the waste water is a great waste of resources, and the waste water is discharged into the environment to cause great harm.

In order to fully recover and recycle water resources, enhance the effective treatment of high-salinity organic wastewater and promote the resource utilization of high-salinity wastewater, the development of an environment-friendly and thorough-separation high-salinity wastewater treatment method is urgently needed.

SUMMERY OF THE UTILITY MODEL

The to-be-solved technical problem of the utility model is to provide a processing system of high salt organic waste water in ion exchange resin production to solution ion exchange resin that can low cost produces the purification of high salt organic waste water and the resource recycle problem of well methylamine/ethylamine, salt etc..

In order to solve the technical problem, the utility model adopts the following technical scheme:

designing a treatment system for high-salt organic wastewater in ion exchange resin production, which comprises an amine recovery treatment device, an oxidation and precipitation device and an evaporation recovery device which are sequentially connected; the amine recovery treatment device comprises an amine gasification tower, a multi-stage condensation mechanism, a multi-stage negative pressure absorption mechanism and a tail gas absorption tower which are sequentially communicated; the oxidation and precipitation device comprises an oxidation reaction tank, a flocculation mechanism and a precipitator which are sequentially communicated; the oxidation reaction tank receives the wastewater after the amine gasification treatment by the amine recovery treatment device; the evaporation recovery device comprises a waste liquid storage tank and an evaporator which are sequentially communicated; the waste tank receives the clarified solution from the settler.

Preferably: the amine gasification tower is sequentially provided with a heating unit, a liquid distribution unit and a reflux unit from bottom to top; and the outlet of the reflux unit is communicated with the corresponding multistage condensation mechanism.

Preferably: the multistage negative pressure absorption mechanism comprises at least three negative pressure absorption units; the negative pressure absorption unit comprises an absorption tank, a circulating pump and an ejector, wherein the air suction port of the ejector of the primary negative pressure absorption unit is connected with the front-stage treated incoming air, and the air suction ports of the rest stages of ejectors are communicated with the exhaust port of the front-stage collecting tank; the liquid inlet of each stage of ejector is communicated to the circulating liquid outlet of the absorption tank of the stage through a corresponding circulating pump, and the liquid outlet of each stage of ejector is communicated to the liquid inlet of the absorption tank of the stage.

Preferably: and the part of the wastewater receiving inlet of the oxidation reaction tank is also provided with 1-3 sealed stirring devices, and the added oxidant and the catalyst are fully stirred and mixed at the rotating speed of 80-130 r/min.

Preferably: the middle part of the oxidation reaction tank is provided with a corresponding sewage return pipe to realize 100-400% of return proportion, and the upper part of the oxidation reaction tank is provided with a foam spraying device consisting of a nozzle and a water distribution pipe to realize 250-300% of coverage rate of a spraying area.

Preferably: the precipitator comprises an overflow section, a blocking sedimentation section, a water supplementing distribution section, a conical sludge storage section, a water inlet, a water distribution disc and an exhaust pipe, wherein the overflow section, the blocking sedimentation section, the water supplementing distribution section and the conical sludge storage section are arranged from top to bottom; the blocking and settling section is provided with an inclined plate structure, a herringbone plate structure, a fin structure, a labyrinth structure or a honeycomb structure.

Preferably: the flocculation mechanism comprises at least two stages of stirring with a stirrer, the first stage stirring speed is controlled to be 110-130 r/min, and the rest stirring speeds are controlled to be 5-15 r/min.

Compared with the prior art, the utility model discloses a main beneficial technological effect lies in:

1. the utility model has simple equipment and process flow, easy operation and control and energy saving; through delicate rectification operation, methylamine or ethylamine with the mass percentage of 10-20% is recovered and reused while aminated pollutants in the discharged wastewater are removed.

2. The treatment method of the utility model obtains condensed water with salt content of 150-300 mg/L, and the evaporator obtains crystallized salt which can be reused in white ball workshops or sold; the evaporated condensed water is reused in the production system to clean the resin which is separated from the mother liquor just after amination.

3. The utility model discloses the waste water has been handled to the method when having retrieved organic matter and salt, and handles back waste water and can recycle in production, and the processing procedure does not produce waste water waste gas, can realize joint production and continuous production, and environmental friendly moreover, economic benefits and social are showing very much.

Drawings

FIG. 1 is a schematic structural diagram of a treatment system for producing high-salt organic wastewater by using ion exchange resin.

FIG. 2 is a schematic view of an amination waste water treatment apparatus.

FIG. 3 is a schematic structural view of a reaction mechanism.

Fig. 4 is a schematic structural view of the precipitation mechanism.

In the above figures, 1 is an amination wastewater treatment device; 11 is an amine gasification tower; 111 is a heating unit, 112 is a liquid distribution unit, and 113 is a reflux unit; 12 is a multi-stage condensing mechanism; 121 is a first condenser, 122 is a second condenser, 123 is a third condenser; 13 is a multi-stage negative pressure absorption mechanism; 131 is a first absorption tower, 1311 is a first absorption tank, 1312 is a first circulation pump, 1313 is a first ejector, 132 is a second absorption tower, 133 is a third absorption tower, 134 is a fourth absorption tower; 14 is a tail gas absorption tower; 141 is a tail gas circulating pump, 142 is a spraying unit, and 143 is a water replenishing inlet; 15 is an amine recovery box; 16 is an organic matter recycling box; 2 is a pretreatment device; 21 is a reaction mechanism, 211 is a sealed stirrer, 212 is a sewage return pipe, 213 is a foam sprayer and 214 is a water outlet; 22 is a flocculation mechanism; 23 is a precipitation mechanism; 3 is an evaporation device; 31 is a waste liquid storage tank; 32 is an evaporator;

a is a waste liquid inlet, B is an amine gasification tower emptying port, C is an oxidant feeding port, D is a catalyst feeding port, E is an outlet from an organic matter recycling bin to a recycling point, F is an outlet from the amine recycling bin to the recycling point, G is an emptying port of a reaction mechanism, H is a condensate water outlet, and I is a solid salt outlet.

Detailed Description

The following embodiments are only intended to illustrate the present invention in detail, and do not limit the scope of the present invention in any way.

The instruments and devices referred to in the following examples are conventional instruments and devices unless otherwise specified; the related reagents are all conventional reagents in the market, if not specifically indicated; the test methods involved are conventional methods unless otherwise specified.

Example 1: processing system of high salt organic waste water in ion exchange resin production

As shown in fig. 1: the system for treating the high-salt organic wastewater in the ion exchange resin production comprises an amination wastewater treatment device 1, a pretreatment device 2 and an evaporation device 3.

As shown in fig. 2, the amination waste water treatment apparatus 1 includes an amine gasification tower 11, a multistage condensation mechanism 12, a multistage negative pressure absorption mechanism 13, and a tail gas absorption tower 14, which are connected in sequence.

The amine gasification tower 11 is sequentially provided with a heating unit 111, a liquid distribution unit 112 and a reflux unit 113 from bottom to top; the heating unit 111 is heated by steam, and the heating temperature is 85-105 ℃; the liquid distribution unit 112 is provided with an empty liquid distribution pipe, and an atomizing nozzle is arranged on the empty liquid distribution pipe, so that the atomizing particle size is 100-1000 mm; the bottom of the liquid distribution unit 112 is provided with a filler layer, and the filler is conventional irregular filler, mainly stainless steel Raschig rings, pall rings, ladder rings and other amine gas corrosion resistant materials; the lower part of the packing layer is provided with a flushing mechanism, the flushing water adopts water to be treated, and is mainly used for flushing the packing through large flow, so that the blockage of the packing after long-time operation is prevented; the outlet of the reflux unit 113 is communicated with the multistage condensation device 12; an S-shaped water collector is arranged in the backflow unit 113, so that small liquid drops can be better captured, and the amine steam can be conveniently discharged from an exhaust port; the reflux unit 113 is also internally provided with a reflux inlet, and the distance between the reflux inlet and the bottom of the water collector is more than or equal to 3 m.

The multistage condensation mechanism 12 comprises a first condenser 121, a second condenser 122 and a third condenser 123 which are communicated in sequence; an ice water outlet and an ice water inlet are formed in each condenser, so that the temperature in each condenser is controlled to be 0-10 ℃; the condenser is also provided with a reflux liquid outlet which is communicated with a reflux liquid inlet in the reflux unit 113.

The multistage negative pressure absorption mechanism 13 includes a first absorption tower 131, a second absorption tower 132, a third absorption tower 133, and a fourth absorption tower 134; the absorption towers are provided with an ice water outlet and an ice water inlet, the temperature in the first absorption tower 131, the second absorption tower 132 and the third absorption tower 133 is controlled to be 4-10 ℃, and the temperature in the fourth absorption tower 134 is controlled to be 0-25 ℃.

The first absorption tower 131 includes a first absorption tank 1311, a first circulation pump 1312, and a first ejector 1313; the first absorption tank 1311 is provided with an inlet, a liquid inlet, an upper exhaust port and a lower outlet; a suction port of the first ejector 1313 communicates the outlet port of the third condenser 123 and the outlet of the first circulation pump 1312; the outlet of the first ejector 1313 is communicated with the inlet of the first absorption tank 1311; the lower outlet of the first absorption tank 1311 communicates with the inlet of the first circulation pump 1312.

The second absorption tower 132 includes a second absorption tank, a second circulation pump, and a second ejector; the second absorption tank is provided with an inlet, a liquid inlet, an upper exhaust port and a lower outlet; the air suction port of the second ejector is communicated with the upper exhaust port of the first absorption tank and the outlet of the second circulating pump; the outlet of the second ejector is communicated with the inlet of the second absorption tank; and the lower outlet of the second absorption tank is communicated with the inlet of the second circulating pump.

The third absorption tower 133 includes a third absorption tank, a third circulation pump, and a second ejector; the third absorption tank is provided with an inlet, a liquid inlet, an upper exhaust port and a lower outlet; the air suction port of the third ejector is communicated with the upper exhaust port of the second absorption tank and the outlet of the third circulating pump; the outlet of the third ejector is communicated with the inlet of the third absorption tank; and the lower outlet of the third absorption tank is communicated with the inlet of the third circulating pump.

The fourth absorption tower 134 includes a fourth absorption tank, a fourth circulation pump, and a fourth ejector; the fourth absorption tank is provided with an inlet, a liquid inlet, an upper exhaust port and a lower outlet; the air suction port of the fourth ejector is communicated with the upper exhaust port of the third absorption tank and the outlet of the fourth circulating pump; the outlet of the fourth ejector is communicated with the inlet of the fourth absorption tank; and the lower outlet of the fourth absorption tank is communicated with the inlet of the fourth circulating pump.

A tail gas circulating pump 141 and a spraying unit 142 are arranged in the tail gas absorption tower 14; an inlet of the tail gas absorption tower 14 is communicated with an exhaust port of the fourth absorption tank; the shower unit 142 is provided with a water replenishment inlet 143.

A liquid outlet of the tail gas absorption tower 14 is communicated with a liquid inlet of a fourth absorption tank; a liquid outlet of the fourth absorption tank is communicated with a liquid inlet of the third absorption tank; a liquid outlet of the third absorption tank is communicated with a liquid inlet of the second absorption tank; the liquid outlet of the second absorption tank is communicated with the liquid inlet of the first absorption tank 1311.

A liquid outlet of the third condenser 123 is communicated with an amine recovery tank 15; the liquid outlet of the first absorption tank 1311 is communicated with the inlet of the amine recovery tank 15.

The liquid outlet of the third condenser 123 is also communicated with an organic matter recycling tank 16; the liquid outlet of the reflux unit 113 in the amine gasification tower 11 is communicated with the inlet of the organic matter recovery tank 16.

The pretreatment device 2 comprises a reaction mechanism 21, a flocculation mechanism 22 and a precipitation mechanism 23 which are sequentially communicated; the reaction mechanism 21 is communicated with a waste liquid outlet of the amine gasification tower 11; the reaction mechanism 21 is provided with an oxidant adding device and a catalyst adding device; the flocculating mechanism 22 is provided with flocculating agent adding equipment.

The flocculation mechanism 22 comprises at least two stages of stirring with a stirrer, the first stage stirring speed is controlled to be 110-130 r/min, and the rest stirring speeds are controlled to be 5-15 r/min.

The evaporation device 3 comprises a waste liquid storage tank 31 and an evaporator 32; the waste liquid storage tank 31 is communicated with a liquid outlet of the precipitation mechanism 23; the evaporator 32 is connected to the liquid outlet of the waste liquid tank 31 via a water pump.

The exhaust port of the reaction mechanism 21 and the exhaust port of the evaporator 3 communicate with the multistage negative pressure absorbing mechanism 13.

Method for treating high-salt organic wastewater in ion exchange resin production by using treatment system

The treated wastewater is amination wastewater of D301 anion resin of certain ion exchange resin enterprises. The pH value of the amination waste water is 8-9, and the organic components of the amination waste water are mainly dimethylamine, methylal, methanol and the like through detection. Methylal is relatively stable to alkali, is easily decomposed into formaldehyde and methanol when heated together with dilute hydrochloric acid, reacts with concentrated hydrochloric acid to generate methyl chloride, and normally exists in the form of formaldehyde in water. The wastewater of a certain batch of production is detected, the content of dimethylamine (detection standard: methylamine solution inspection HGT 2971-1999; determination GB/T23961-. The total salt content is 5-12%; the main components of the salt comprise sodium chloride, sodium sulfate and other trace ferric chloride, zinc sulfate and the like, wherein the sodium chloride content in the salt is 95-96%, the other sodium sulfate content is 2-3%, the ferric chloride content and the zinc sulfate content are 1-2%, and the rest is insoluble oligomer less than 1%.

The specific treatment steps are as follows:

1. treatment of organic materials

(1) Filtering large-particle substances from the wastewater, then flowing into an amine gasification tower 11 for heating, wherein a bag filter is adopted for filtering, the filtering pore diameter is 0.1-0.5 mm, and the filtering material is an amine corrosion resistant material such as plastic or stainless steel. Liquid sodium hydroxide is added before the waste liquid inlet A to adjust the pH value of the waste water to 11.5. Heating units 111 of the amine gasification tower 11 are heated by steam at the heating temperature of 85-105 ℃; pumping the heated wastewater to the liquid distribution unit 112 by a circulating pump; the atomizing nozzles on the liquid distribution unit 112 atomize the heated flying waste liquid into waste liquid steam with the particle size of 100-1000 microns; because the outlet of the reflux unit 113 is communicated with the multistage condensation mechanism 12, the low temperature of the multistage condensation mechanism 12 and the high temperature of the heating unit 111 form negative pressure at the reflux unit 113, so that part of water vapor and organic matters are condensed, and then the water vapor and the organic matters flow back to the reflux unit 113 through the outlet of the reflux unit 113, and further the liquid outlet of the reflux unit 113 is communicated with the inlet of the organic matter recovery box 16.

So far, dimethylamine gas with the mass percentage of 1-5% is detected by using portable dimethylamine gas detection equipment (Shenzhen Dong Ying energy science and technology Co., Ltd.).

(2) Because methylamine/ethylamine gas has a high boiling point and a low melting point, dimethylamine gas in the amine gasification tower 11 enters the multistage condensation device 12 together with water vapor according to the theory that the solubility of gas in liquid is reduced along with the increase of temperature and the reduction of pressure according to the Henry's law; most of the water vapor is condensed into liquid, meanwhile, the condensate contains a small amount of dimethylamine oil, the condensate flows back to the top of the amine gasification tower 11 to continuously distill out dimethylamine gas, and the temperature parameters of all stages of condensers are well controlled:

the temperature in the first condenser 121, the second condenser 122 and the third condenser 123 is controlled to be 4 ℃; and (3) determining that the content of dimethylamine in the third condenser 123 is less than 300mg/L, wherein a part of condensate is recovered from a liquid outlet of the third condenser 123 and communicated with an inlet of the organic matter recovery tank 16, and a part of condensate is refluxed to the amine gasification tower 11 together with the condensates of the first condenser 121 and the second condenser 122.

At this point, water vapor and other organic matters are firstly recovered through the multistage condensing device 12, and dimethylamine gas which is not condensed and has the mass percentage of 1-5% is obtained at the outlet of the third condenser 123 through portable detection of dimethylamine gas.

(3) Enabling the methylamine/ethylamine gas obtained in the step (2) to enter a multistage negative pressure absorption device 13; the temperature in the first absorption column 131 was controlled to 10 ℃, the temperature in the second absorption column 132 was controlled to 6 ℃, the temperature in the third absorption column 133 was controlled to 2 ℃ and the temperature in the fourth absorption column 134 was controlled to 20 ℃.

Pure water is supplemented to the spraying unit 142 in the tail gas absorption tower 14, and the conductivity is less than 1 micro siemens; a liquid outlet of the tail gas absorption tower 14 is communicated with a liquid inlet of a fourth absorption tank; a liquid outlet of the fourth absorption tank is communicated with a liquid inlet of the third absorption tank; a liquid outlet of the third absorption tank is communicated with a liquid inlet of the second absorption tank; a liquid outlet of the second absorption tank is communicated with a liquid inlet of the first absorption tank; and (3) gradually conveying the supplemented water to the previous stage until the solubility of the dimethylamine solution in the first absorption tank 1311 is 10-20%, and then flowing into an amine recovery tank for recovery.

The pressure in the absorption tank is-0.05 to-0.01 MPa.

(4) Other tail gases (mainly non-condensable gas nitrogen and trace water-insoluble organic hydrocarbon gas) are discharged by the tail gas absorption tower 14 according to the discharge standard DB 41/1135-2016 Henan chemical industry water pollutant indirect discharge standard reaching the standard.

Wherein, the water vapor and the organic matter condensation backward flow of backward flow unit 113 department have guaranteed to contain a small amount of water in the methylamine/ethylamine gas in the waste liquid steam as far as possible, guarantee that multistage negative pressure absorption mechanism 13 normal water can only the moisturizing, can mix with salinity and a large amount of moisture in the dimethylamine of avoiding retrieving, lead to the unable in-production retrieval and utilization of methylamine/ethylamine of retrieving.

2. Treatment of salts

(1) The wastewater heated and refluxed by the amine gasification tower 11 flows into a reaction mechanism 21 of the pretreatment device 2; adding an oxidant and a catalyst into oxidant adding equipment and catalyst adding equipment respectively to react for 1-4 h;

as shown in fig. 3:

the inlet of the reaction mechanism 21 is provided with 1-3 sealed stirrers 211, and the rotating speed of the stirrers is 80-130 r/min.

The middle part of the reaction mechanism 21 is provided with a sewage return pipe 212, and the return proportion is 100-400%.

The upper part of the reaction mechanism 21 is provided with a foam sprayer 213 which consists of a nozzle and a water distribution pipe, so that the coverage rate of a spraying area is 250-300%.

A water outlet 214 of the reaction mechanism 21 is dripped with hydrochloric acid or sulfuric acid to adjust the pH value of the effluent to 9-11; the oxidant is hydrogen peroxide, ferrate or persulfate; the adding amount is 1.0-1.2 times of the chemical oxygen demand; ferrous sulfate, zinc sulfate or copper sulfate as catalyst; the amount added is 0.5 times of the chemical oxygen demand.

(2) The reaction liquid flows into the flocculation mechanism 22; adding 150mg/L of flocculant PAC and 5mg/L of coagulant aid PAM into the flocculant adding equipment; reacting for 4-5 hours at 20-30 ℃ to change organic oxidation products in the waste liquid from fine particles into large particles;

4-5 lattices are arranged in the flocculation mechanism 22, a stirrer is arranged in the lattices, the rotating speed of the first-stage stirrer is 110-130 r/min, and the rotating speed of the rest stirrers is 5-15 r/min;

PFS, polyferric chloride or polyaluminum ferric chloride can also be used as the flocculating agent; the coagulant aid can also be diatomite or powdered activated carbon.

(3) The waste liquid enters a precipitation mechanism 23 after flocculation for precipitation to remove precipitates, an inclined plate (herringbone/fin/labyrinth/honeycomb can also be adopted) is arranged in the precipitation mechanism 23, water enters from the bottom of the inclined plate of the precipitation mechanism, and a water distribution plate and an exhaust port are arranged in a water inlet pipe; and the effluent is delivered to a waste liquid storage tank from the upper part of the precipitation mechanism.

As shown in fig. 4, the settling mechanism 23 includes an overflow section 231, a blocking settling section 232, a water replenishing distribution section 233, a tapered sludge storage section 234, a water inlet 235 arranged on the water replenishing distribution section 233, a water distribution tray 236 positioned below the water inlet 234, and an exhaust pipe 237 extending through the overflow section 231, the blocking settling section 232, and the water replenishing distribution section 233, wherein the water inlet 234 corresponds to the expansion end of the exhaust pipe 237 and is communicated to the water outlet of the corresponding flocculation mechanism 22 through a corresponding pipe; the blocking and settling section 232 is provided with an inclined plate structure, a herringbone plate structure, a fin structure, a labyrinth structure or a honeycomb structure.

(4) The waste liquid in the waste liquid storage tank is conveyed to the evaporator 32 by a water pump;

crystallizing salt by using a mechanical compression steam evaporator/multi-effect evaporator; the product can be reused in white ball workshops or sold; the salt content in the evaporated condensed water is 150-300 mg/L, and the condensed water is reused for a production system to clean the resin which is just separated from the mother liquor after amination.

3. Tail gas treatment

The free tail gas (non-condensable gas nitrogen and trace amount of water-insoluble organic hydrocarbon gas) generated in the reaction mechanism 21 and the evaporator 32 enters the multistage negative pressure absorption mechanism 13 (or independently arranged negative pressure absorption mechanism) to adsorb a small amount of dimethylamine contained in the tail gas and recycle the dimethylamine, and the rest tail gas enters the tail gas absorption tower 14 to be treated. The tail gas absorption tower 14 discharges the water pollutants according to the indirect discharge standard of the water pollutants in the chemical industry of Henan of discharge standard DB 41/1135-2016 after reaching the standard; and finishing the wastewater treatment.

The present invention has been described in detail with reference to the accompanying drawings and embodiments, but those skilled in the art will understand that various specific parameters in the above embodiments can be changed or equivalent substitutions can be made on related components and structures without departing from the technical concept of the present invention, thereby forming a plurality of specific embodiments, which are common variations of the present invention and will not be described in detail herein.

Claims (7)

1. The utility model provides a processing system of high salt organic waste water in ion exchange resin production, includes amine recovery processing apparatus, oxidation and precipitation device and the evaporation recovery unit that links up in proper order, its characterized in that:

the amine recovery treatment device comprises an amine gasification tower, a multi-stage condensation mechanism, a multi-stage negative pressure absorption mechanism and a tail gas absorption tower which are sequentially communicated;

the oxidation and precipitation device comprises an oxidation reaction tank, a flocculation mechanism and a precipitator which are sequentially communicated; the oxidation reaction tank receives the wastewater after the amine gasification treatment by the amine recovery treatment device;

the evaporation recovery device comprises a waste liquid storage tank and an evaporator which are sequentially communicated; the waste tank receives the clarified solution from the settler.

2. The system for treating high-salt organic wastewater in ion exchange resin production according to claim 1, characterized in that: the amine gasification tower is sequentially provided with a heating unit, a liquid distribution unit and a reflux unit from bottom to top; and the outlet of the reflux unit is communicated with the corresponding multistage condensation mechanism.

3. The system for treating high-salt organic wastewater in ion exchange resin production according to claim 1, characterized in that: the multistage negative pressure absorption mechanism comprises at least three negative pressure absorption units; the negative pressure absorption unit comprises an absorption tank, a circulating pump and an ejector, wherein the air suction port of the ejector of the primary negative pressure absorption unit is connected with the front-stage treated incoming air, and the air suction ports of the rest stages of ejectors are communicated with the exhaust port of the front-stage collecting tank; the liquid inlet of each stage of ejector is communicated to the circulating liquid outlet of the absorption tank of the stage through a corresponding circulating pump, and the liquid outlet of each stage of ejector is communicated to the liquid inlet of the absorption tank of the stage.

4. The system for treating high-salt organic wastewater in ion exchange resin production according to claim 1, characterized in that: and the part of the wastewater receiving inlet of the oxidation reaction tank is also provided with 1-3 sealed stirring devices, and the added oxidant and the catalyst are fully stirred and mixed at the rotating speed of 80-130 r/min.

5. The system for treating high-salt organic wastewater in ion exchange resin production according to claim 1, characterized in that: the middle part of the oxidation reaction tank is provided with a corresponding sewage return pipe to realize 100-400% of return proportion, and the upper part of the oxidation reaction tank is provided with a foam spraying device consisting of a nozzle and a water distribution pipe to realize 250-300% of coverage rate of a spraying area.

6. The system for treating high-salt organic wastewater in ion exchange resin production according to claim 1, characterized in that: the precipitator comprises an overflow section, a blocking sedimentation section, a water supplementing distribution section, a conical sludge storage section, a water inlet, a water distribution disc and an exhaust pipe, wherein the overflow section, the blocking sedimentation section, the water supplementing distribution section and the conical sludge storage section are arranged from top to bottom; the blocking and settling section is provided with an inclined plate structure, a herringbone plate structure, a fin structure, a labyrinth structure or a honeycomb structure.

7. The system for treating high-salt organic wastewater in the ion exchange resin production according to claim 6, is characterized in that: the flocculation mechanism comprises at least two stages of stirring with a stirrer, the first stage stirring speed is controlled to be 110-130 r/min, and the rest stirring speeds are controlled to be 5-15 r/min.

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