Process for treating waste water from cumene hydroperoxide condensation

Abstract

The application provides a cumene hydroperoxide condensation wastewater treatment process, which comprises the following steps: (1) adjusting the pH of cumene hydroperoxide condensation washing wastewater to 2-8 by using an acid, and then transferring the wastewater to an extraction tower; (2) adding an oil phase containing an oil-soluble surfactant into an aqueous phase A containing a water-soluble surfactant A, and mechanically stirring until foam is generated to obtain CLA; (3) using mechanical stirring to stir an aqueous phase B containing a surfactant B until a sustained volume of foam is generated to obtain CGA; (4) diluting the obtained CLA with water, and then feeding the CLA into the bottom of the extraction tower; after standing for a period of time, feeding the obtained CGA into the bottom of the extraction tower, and after the feeding is completed, performing liquid separation to separate the wastewater from the extraction layer. The cumene hydroperoxide condensation wastewater treatment process has high extraction efficiency, short treatment time, and low wastewater post-treatment cost, the extractant does not contain benzene / dimethylbenzene and other harmful substances to human body, the environmental and economic benefits are remarkable, and the cumene hydroperoxide condensation wastewater treatment process can be applied to large-scale industrial production devices.

Description

TECHNICAL FIELD

[0001] The application belongs to the technical field of wastewater treatment, and particularly relates to a cumene hydroperoxide condensation wastewater treatment process. BACKGROUND

[0002] Cumene hydroperoxide (DCP) is a commonly used symmetrical di-tert-alkyl peroxide, and is an important additive in polymer materials. As a vulcanizing agent in natural rubber and synthetic rubber, and as an initiator or crosslinking agent in the polymerization reaction of olefin monomers, DCP can enhance the mechanical strength, heat resistance, crack resistance and corrosion resistance of polymers, and is widely used in the industries of electric wires and cables, shoemaking and building materials.

[0003] In industry, DCP is usually produced by condensation reaction of cumene hydroperoxide and α,α-dimethylbenzyl alcohol under acidic conditions, and then the excess isopropylbenzene in the solution is evaporated by heating under reduced pressure in the subsequent section to concentrate the DCP condensate to more than 90%, and finally the finished product is obtained by crystallization. Since high-concentration DCP is extremely prone to violent decomposition under heat in an acidic environment, which may cause safety hazards, therefore, before concentration, sodium hydroxide solution is used for alkaline washing to adjust the pH of the solution to neutral, and the wastewater generated by washing contains not only a large amount of by-product phenol, but also α,α-dimethylbenzyl alcohol, isopropylbenzene, DCP and α-methylstyrene, etc., thus resulting in high chemical oxygen demand (COD) of the wastewater, and the phenol in the wastewater not only causes harm to the human body and the environment, but also causes death of bacterial flora in sewage plants, so that the cost of wastewater treatment is increased. Therefore, the DCP condensation wastewater needs to be pretreated to reduce the treatment pressure of the sewage plant.

[0004] CN103787441A discloses a pretreatment method for cumene hydroperoxide wastewater, which uses isopropylbenzene as an extractant to mix and separate the wastewater:extractant=4-1:1 to reduce the COD of the wastewater discharged. Isopropylbenzene has a certain effect on the extraction of dimethylbenzyl alcohol and part of the organic matter in the wastewater, but has no significant reduction on the phenol content in the wastewater. CN103787442A discloses a treatment method for cumene hydroperoxide condensation wastewater, which uses a mixed solution of N-503 and isopropylbenzene as an extractant to carry out multi-stage reverse extraction treatment on the DCP wastewater, to reduce the COD and the phenol content of the wastewater. Wastewater:extractant

[0005] =1:1-1.5, the volume ratio of the organic phase to the aqueous phase (PVR) is high, and emulsification is prone to occur in the case of low external temperature, which leads to difficult separation of oil and water and loss of the extractant. CN103613159A discloses a treatment process for phenol-containing wastewater in the production of dicumyl peroxide, adopts benzene series as the extractant, extracts the wastewater with pure toluene / xylene at a ratio of 0.5-1.5:1, and recovers and separates phenol by distillation of the oil phase, so as to realize the recycling of the extractant. Toluene / xylene has adverse effects on the central nervous system, respiratory tract and skin of human body, and needs to be used in large quantities in extraction, which is harmful to the health of the operators on site.

[0006] In summary, the existing methods for pretreating dicumyl peroxide wastewater have the following problems: isopropylbenzene is used as the extractant, which does not significantly reduce the phenol content in the wastewater; the mixture of N-503 and isopropylbenzene is used as the extractant, the volume ratio of the organic phase to the aqueous phase (PVR) is high, and emulsification is prone to occur in the case of low external temperature, which leads to difficult separation of oil and water and loss of the extractant; and benzene series is used as the extractant, and toluene / dimethylbenzene has adverse effects on the central nervous system, respiratory tract and skin of human body. SUMMARY

[0007] To solve the above technical problems, the present application provides a treatment process for dicumyl peroxide condensation wastewater.

[0008] The technical scheme adopted by the present application is as follows:

[0009] A treatment process for dicumyl peroxide condensation wastewater, comprising the following steps:

[0010] (1) adjusting the pH of dicumyl peroxide condensation and washing wastewater to 2-8 with an acid, and transferring it to an extraction column;

[0011] (2) preparing a colloidal liquid foam: adding an oil phase containing an oil-soluble surfactant to an aqueous phase A containing a water-soluble surfactant A, and mechanically stirring until a foam is generated, to obtain CLA;

[0012] (3) preparing a colloidal gas foam: using mechanical stirring to stir an aqueous phase B containing a surfactant B until a continuous volume of foam is generated, to obtain CGA;

[0013] (4) diluting the CLA prepared in step (2) with water, and then introducing it from the bottom of the extraction column; after standing for a period of time, introducing the CGA prepared in step (3) from the bottom of the extraction column, and after the introduction is completed, separating the layers to separate the wastewater from the extraction layer.

[0014] Preferably, in step (1), the acid is 20-30wt% hydrochloric acid or 50-70wt% sulfuric acid.

[0015] Preferably, in step (2), the oil-soluble surfactant is a non-ionic polyether surfactant, more preferably at least one of Tween 80, Softanol 120, Softanol 30 and Tergitol 15-s-30; and the oil phase is at least one of kerosene, N,N-bis(1-methylheptyl)acetamide and tributyl phosphate.

[0016] Preferably, in step (2), the water-soluble surfactant A is a quaternary ammonium salt cationic surfactant or a sulfonate anionic surfactant, more preferably at least one of sodium dodecyl benzene sulfonate, cetyl trimethyl ammonium bromide, dodecyl trimethyl ammonium bromide or Quadrilan BC.

[0017] Preferably, in step (3), the water-soluble surfactant B is a quaternary ammonium salt cationic surfactant or a sulfonate anionic surfactant, more preferably at least one of sodium dodecyl sulfonate, sodium dodecyl benzene sulfonate, cetyl trimethyl ammonium chloride, dodecyl trimethyl ammonium chloride, tetradecyl trimethyl ammonium bromide, cetyl pyridinium chloride, cetyl pyridinium bromide and benzyl dimethyl n-hexadecyl ammonium chloride.

[0018] Preferably, in step (1), the height-diameter ratio of the extraction column is 6.25-10.

[0019] Preferably, in step (2), the content of the oil-soluble surfactant in the oil phase is 0.05-1.2wt%, the content of the water-soluble surfactant A in the water phase A is 0.1-0.8wt%, and the mass ratio of the oil phase to the water phase is (10-25):1.

[0020] Preferably, in step (3), the content of the water-soluble surfactant B in the water phase B is 0.05-0.4wt%.

[0021] Preferably, in step (4), the dilution ratio of the CLA is 1:(10-20), and the mass ratio of the diluted CLA to the wastewater is (0.4-1):1; and the mass ratio of the CGA to the wastewater is (0.05-0.11):1.

[0022] Preferably, in the preparation of the CLA, the speed of mechanical stirring is 1000-1500rpm, and the stirring time is 30-60min; and in the preparation of the CGA, the speed of mechanical stirring is 3000-5000rpm, and the stirring time is 10-30min.

[0023] Compared with the prior art, the present application has the following advantages:

[0024] 1. The present application adopts a pre-dispersed solvent extraction (PDSE) method to treat cumene hydroperoxide condensation wastewater, which pre-treats the extractant to form a stable colloidal liquid foam, increases the mass transfer area between the two phases without relying on mechanical stirring during the extraction process, relies on the buoyancy of the foam itself for separation, has a large contact surface area, and a small amount of solvent can achieve the purpose of extraction separation, reducing the problem of emulsification of the extractant caused by mechanical stirring.

[0025] 2. The present application can reduce the COD of the condensation wastewater from 600000-900000 mg / L to below 5000 mg / L, with a removal rate of 91.7-94.4%; the phenol concentration is reduced from 2-8% to below 0.15%, with a removal rate of 92.5-98.1%; the cumene concentration is reduced from 1.5-3% to below 0.1%, with a removal rate of 93.3-96.7%; the α,α-dimethylbenzyl alcohol concentration is reduced from 1-5% to below 0.1%, with a removal rate of 90-98%; the rectified oil phase can obtain ≥90% phenol by-product, ≥97% cumene by-product, and extractant; the extractant can be reused after recycling. Cr As a result, the present application can effectively reduce the cost of wastewater treatment, and the extractant does not contain harmful substances such as benzene / xylene to the human body, which has significant environmental and economic benefits, and can be applied to large-scale industrial production devices.

[0026] 3. The present application has high extraction efficiency, short treatment time, and effectively reduces the cost of wastewater treatment. The extractant does not contain harmful substances such as benzene / xylene to the human body, which has significant environmental and economic benefits, and can be applied to large-scale industrial production devices. BRIEF DESCRIPTION OF DRAWINGS

[0027] Figure 1 The present application is a process flow diagram for treating cumene hydroperoxide condensation wastewater. DETAILED DESCRIPTION

[0028] The present application is further described below by examples, but is not limited to the examples. The raw materials used in the following examples are commercially available.

[0029] Example 1, see Figure 1 The present example provides a device for treating cumene hydroperoxide condensation wastewater, which includes a wastewater tank 1, a delivery pump A 21, an oil-soluble surfactant storage tank 5, a delivery pump B 22, a CLA preparation tank 6, a peristaltic pump A 71, a CGA preparation tank 9, a peristaltic pump B 72, an extraction tower 10, and a liquid separation tank 12. In the present example, the height of the extraction tower 10 is 10 m, and the inner diameter is 1.6 m; in other examples, the height-to-diameter ratio of the extraction tower 10 can also be selected within the range of 6.25-10, and the top of the extraction tower 10 is provided with a first feed port, the bottom is provided with a second feed port, a third feed port, and a discharge port.

[0030] Wastewater tank 1 is connected to the first inlet of extraction tower 10 via transfer pump A 21. A flow meter A31 and a shut-off valve A41 for measuring the wastewater flow are installed on the outlet pipe of pump A21.

[0031] The oil-soluble surfactant storage tank 5 is connected to the CLA preparation tank 6 via a transfer pump B 22. The CLA preparation tank 6 is equipped with a mechanical stirrer. The CLA preparation tank 6 is connected to the second inlet of the extraction tower 10 via a peristaltic pump A71. The outlet pipe of the peristaltic pump A71 is equipped with a flow meter B32 for measuring the CLA flow rate and a one-way valve A81.

[0032] CGA preparation tank 9 is connected to the third feed port of extraction tower 10 via peristaltic pump B72. A flow meter C33 and a one-way valve B82 for measuring the CGA flow rate are installed on the outlet pipe of peristaltic pump B72.

[0033] The bottom outlet of the extraction tower 10 is connected to the separatory tank 12 via a discharge pipe. The discharge pipe is equipped with a shut-off valve B42 and a sight glass 11. The upper part of the separatory tank 12 has an oil phase outlet, which is connected to an oil discharge pipe. The oil discharge pipe is equipped with a flow meter D34 for measuring the oil phase flow rate. The oil discharge pipe is also connected to a distillation unit (not shown in the figure) for separating phenol, cumene, and the extractant. The bottom of the separatory tank 12 has an aqueous phase outlet, which is connected to a drainage pipe. The drainage pipe is equipped with a flow meter E35 for measuring the flow rate of the treated wastewater. The drainage pipe is connected to an intermediate water tank (not shown in the figure).

[0034] Examples 2-5 use the apparatus shown in Example 1 to treat dicumyl peroxide condensation wastewater. The COD of the dicumyl peroxide condensation wastewater is... Cr The concentration is 600,000-900,000 mg / L, with 2-8 wt% phenol, 1.5-3 wt% cumene, and 1-5 wt% α,α-dimethylbenzyl alcohol; the specific method is as follows:

[0035] Example 2:

[0036] (1) Add COD to condensation wastewater tank 1 Cr 9m³ of condensation wastewater with a concentration of 635249 mg / L, containing 2.7 wt% phenol, 1.6 wt% cumene, and 2.4 wt% α,α-dimethylbenzyl alcohol. 3 After adjusting the pH of the wastewater to 4.9 with 25% hydrochloric acid, it is then fed into the extraction tower 10 via pump A21.

[0037] (2) In the CLA preparation tank 6, 50 L of an aqueous solution containing 4000 mg / L of cetyltrimethylammonium bromide was added, and stirred at a speed of 500 rpm until stable foam was generated. Then, 550 L of kerosene containing 6200 mg / L of Tergitol 15-s-30 was added into the above aqueous solution at a rate of 20 L / min by the delivery pump B 22 under continuous stirring, to obtain 600 L of stable CLA;

[0038] (3) In the CGA tank 9, 800 L of an aqueous solution containing 2500 mg / L of cetyltrimethylammonium bromide was added, and stirred at a high speed of 3500 rpm until stable foam was generated, to obtain CGA;

[0039] (4) The CLA obtained in step (2) was diluted with water to 6.5 m 3 L, and the diluted CLA was introduced into the extraction column 10 from the bottom at a rate of 150 L / min by the peristaltic pump A 71. After the CLA was completely introduced into the extraction column 10, the CGA in the CGA tank 9 was introduced into the extraction column 10 from the bottom at a rate of 30 L / min by the peristaltic pump A 72. After standing for 30 min, the stop valve B 42 was opened, and the oil and water phases were separated by the phase separation tank 12. The separated oil phase was transported to a rectification device through an oil discharge pipeline, and the phenol, cumene and extractant were recovered by rectification. The separated water phase was stored in an intermediate water tank.

[0040] The water in the intermediate water tank was taken, and the COD Cr concentration in the treated water phase was detected to be 3851 mg / L, the mass fraction of phenol was 0.08%, the mass fraction of cumene was 0.06%, and the mass fraction of α,α-dimethylbenzyl alcohol was 0.06%.

[0041] Example 3:

[0042] (1) In the condensation wastewater tank 1, 9 m Cr L of condensation wastewater with a COD 3 concentration of 869544 mg / L, containing 6.5 wt% of phenol, 1.9 wt% of cumene and 3.7 wt% of α,α-dimethylbenzyl alcohol was added, and the pH of the wastewater was adjusted to 6.3 by 25% hydrochloric acid, and then the wastewater was introduced into the extraction column 10 by the delivery pump A 21;

[0043] (2) In the CLA preparation tank 6, 50 L of an aqueous solution containing 4000 mg / L of cetyltrimethylammonium bromide was added, and stirred at a speed of 500 rpm until stable foam was generated. Then, 550 L of kerosene containing 6200 mg / L of Tergitol 15-s-30 was added into the above aqueous solution at a rate of 20 L / min by the delivery pump B 22 under continuous stirring, to obtain 600 L of stable CLA;

[0044] (3) Add 900 L of an aqueous solution containing 4000 mg / L of sodium dodecyl benzene sulfonate into CGA tank 9, and stir at a speed of 4000 rpm until stable foam is generated to obtain CGA;

[0045] (4) Dilute the CLA obtained in step (2) to 8 m 3 and pass the diluted CLA through peristaltic pump A71 at a rate of 180 L / min from the bottom into extraction column 10; after the CLA is completely passed into extraction column 10, pass the CGA in CGA tank 9 through peristaltic pump A72 at a rate of 30 L / min from the bottom into extraction column 10, and after standing for 30 min, open stop valve B42 to separate the oil and water phases through phase separation tank 12; the separated oil phase is transported to a rectification device through an oil discharge pipeline, and phenol, cumene and extractant are recovered through rectification, and the separated water phase is stored in an intermediate water tank.

[0046] Take the water in the intermediate water tank to detect the COD Cr concentration of the treated water phase is 4860 mg / L, the mass fraction of phenol is 0.13%, the mass fraction of cumene is 0.07%, and the mass fraction of α,α-dimethyl benzyl alcohol is 0.08%.

[0047] Example 4:

[0048] (1) Add 9 m Cr of condensation wastewater with a COD 3 concentration of 675336 mg / L containing 2.6 wt% of phenol, 1.6 wt% of cumene and 2.7 wt% of α,α-dimethyl benzyl alcohol into condensation wastewater tank 1, and pass the wastewater into extraction column 10 through delivery pump A21 after adjusting the pH of the wastewater to 5.7 with 25% hydrochloric acid;

[0049] (2) Add 50 L of an aqueous solution containing 5300 mg / L of sodium dodecyl benzene sulfonate into CLA preparation tank 6, and stir at a speed of 500 rpm until stable foam is generated, then add 600 L of N,N-bis(1-methylheptyl)acetamide containing 7600 mg / L of Tween 80 into the above aqueous solution from surfactant-extractant storage tank 5 at a rate of 20 L / min under continuous stirring to obtain 650 L of stable CLA;

[0050] (3) Add 670 L of an aqueous solution containing 3700 mg / L of sodium dodecyl benzene sulfonate into CGA tank 9, and stir at a speed of 4000 rpm until stable foam is generated to obtain CGA;

[0051] (4) Dilute the CLA obtained in step (2) to 7.3 m 3The diluted CLA is passed through the bottom of the extraction column 10 at a rate of 150 L / min by means of a peristaltic pump A71. When the CLA has been completely passed into the extraction column 10, the CGA in the CGA tank 9 is passed through the bottom of the extraction column 10 at a rate of 30 L / min by means of a peristaltic pump A72. After standing for 30 min, the stop valve B42 is opened, and the oil and water phases are separated through the liquid separation tank 12. The separated oil phase is transported to a rectification device through an oil discharge pipeline, and the phenol, cumene and extractant are recovered by rectification. The separated water phase is stored in an intermediate water tank.

[0052] The water in the intermediate water tank is taken, and the COD in the treated water phase is detected Cr The concentration is 4027 mg / L, the mass fraction of phenol is 0.07%, the mass fraction of cumene is 0.06%, and the mass fraction of α,α-dimethylbenzyl alcohol is 0.07%.

[0053] Example 5:

[0054] (1) The COD Cr The concentration is 732581 mg / L, and the condensation wastewater 9m contains 3.4 wt% of phenol, 1.9 wt% of cumene and 3.1 wt% of α,α-dimethylbenzyl alcohol 3 After the pH of the wastewater is adjusted to 7.2 by 60% sulfuric acid, the wastewater is passed into the extraction column 10 by means of a delivery pump A21;

[0055] (2) 50 L of an aqueous solution containing 5500 mg / L of sodium dodecylbenzenesulfonate is added to the CLA preparation tank 6, and is stirred at a speed of 500 rpm until stable foam is generated. Then, 650 L of kerosene-phosphoric acid tributyl ester containing 7300 mg / L of Tergitol 15-s-30 is added to the above aqueous solution at a rate of 20 L / min by means of a delivery pump B22 under continuous stirring, and kerosene: phosphoric acid tributyl ester = 7:3, to obtain 700 L of stable CLA;

[0056] (3) 560 L of an aqueous solution containing 2100 mg / L of cetyltrimethylammonium bromide is added to the CGA tank 9, and is stirred at a high speed of 4500 rpm until stable foam is generated, to obtain CGA;

[0057] (4) The CLA obtained in step (2) is diluted with water to 4.6 m 3The diluted CLA is passed through the bottom of the extraction column 10 at a rate of 120 L / min by using a peristaltic pump A71. When the CLA is completely passed into the extraction column 10, the CGA in the CGA tank 9 is passed through the bottom of the extraction column 10 at a rate of 30 L / min by using a peristaltic pump A72. After standing for 30 min, the stop valve B42 is opened, and the oil and water phases are separated through the liquid separation tank 12. The separated oil phase is transported to a rectification device through an oil discharge pipeline, and the phenol, cumene and extractant are recovered by rectification. The separated water phase is stored in an intermediate water tank.

[0058] The COD in the treated water phase is detected by using the water in the intermediate water tank. Cr The concentration is 4236 mg / L, the mass fraction of phenol is 0.1%, the mass fraction of cumene is 0.06%, and the mass fraction of α,α-dimethylbenzyl alcohol is 0.08%.

[0059] Example 6:

[0060] (1) The COD Cr The concentration is 698533 mg / L, and the condensation wastewater 9m contains 3.0 wt% of phenol, 1.8 wt% of cumene and 2.8 wt% of α,α-dimethylbenzyl alcohol. 3 After the pH of the wastewater is adjusted to 5.5 by using 25% hydrochloric acid, the wastewater is passed into the extraction column 10 by using a delivery pump A21.

[0061] (2) 50 L of an aqueous solution containing 4500 mg / L of cetyltrimethylammonium bromide is added to the CLA preparation tank 6, and the aqueous solution is stirred at a speed of 500 rpm until stable foam is generated. Then, 650 L of fresh kerosene containing 5100 mg / L of Softanol 120 and the recovered kerosene recovered in Example 1 are added to the aqueous solution from the surfactant-extractant storage tank 5 at a rate of 20 L / min under continuous stirring, and the fresh kerosene:recovered kerosene = 5:5, to obtain 700 L of stable CLA.

[0062] (3) 750 L of an aqueous solution containing 2500 mg / L of cetyltrimethylammonium chloride is added to the CGA tank 9, and the aqueous solution is stirred at a high speed of 4500 rpm until stable foam is generated, to obtain CGA.

[0063] (4) The CLA obtained in step (2) is diluted with water to 7m 3The diluted CLA is passed through the bottom of the extraction column 10 at a rate of 150 L / min by means of a peristaltic pump A71. When the CLA is completely passed through the extraction column 10, the CGA in the CGA tank 9 is passed through the bottom of the extraction column 10 at a rate of 30 L / min by means of a peristaltic pump A72. After 30 min, the stop valve B42 is opened, and the oil and water phases are separated through the liquid separation tank 12. The separated oil phase is transported to the rectification device through the oil discharge pipeline, and the phenol, cumene and extractant are recovered by rectification. The separated water phase is stored in the intermediate water tank.

[0064] The water in the intermediate water tank is used to detect the COD in the treated water phase Cr The concentration is 3893 mg / L, the mass fraction of phenol is 0.07%, the mass fraction of cumene is 0.07%, and the mass fraction of α,α-dimethylbenzyl alcohol is 0.08%.

[0065] Example 7:

[0066] (1) The COD Cr The concentration is 786395 mg / L, and the condensation wastewater 9m contains 5.9wt% phenol, 2.2wt% cumene and 3.2wt% α,α-dimethylbenzyl alcohol 3 After the pH of the wastewater is adjusted to 4.9 by 25% hydrochloric acid, the wastewater is passed into the extraction column 10 by means of a delivery pump A21;

[0067] (2) 50 L of an aqueous solution containing 5700 mg / L of sodium dodecylbenzenesulfonate is added to the CLA preparation tank 6, and stirred at a speed of 500 rpm until stable foam is generated. Then, 700 L of the recovered kerosene of Example 1 containing 5000 mg / L of Softanol 30 is added to the above aqueous solution at a rate of 20 L / min by means of a delivery pump B22 under continuous stirring to obtain 750 L of stable CLA;

[0068] (3) 800 L of an aqueous solution containing 2500 mg / L of cetyltrimethylammonium bromide is added to the CGA tank 9, and high-speed stirring is carried out at a speed of 4000 rpm until stable foam is generated to obtain CGA;

[0069] (4) The CLA obtained in step (2) is diluted with water to 8m 3After the dilution, the CLA is pumped into the extraction column 10 from the bottom at a rate of 180 L / min by using the peristaltic pump A71. After the CLA is completely pumped into the extraction column 10, the CGA in the CGA tank 9 is pumped into the extraction column 10 from the bottom at a rate of 30 L / min by using the peristaltic pump A72. After 30 min, the stop valve B42 is opened, and the oil and water phases are separated by using the liquid separation tank 12. The separated oil phase is transported to a rectification device by using an oil discharge pipeline, and the phenol, cumene and extractant are recovered by rectification. The separated water phase is stored in an intermediate water tank.

[0070] The COD in the water phase after treatment is detected by using the water in the intermediate water tank. Cr The concentration is 4510 mg / L, the mass fraction of phenol is 0.11%, the mass fraction of cumene is 0.08%, and the mass fraction of α, α-dimethylbenzyl alcohol is 0.08%.

[0071] Table 1 COD in the DCP condensation wastewater before and after treatment cr and the content change of each component

[0072]

[0073] As shown in Table 1, the COD in the DCP condensation wastewater can be reduced to less than 5000 mg / L by using the method of the present application. Cr The removal rate is 91.7-94.4%. The concentration of phenol is reduced from 2-7% to less than 0.15%, and the removal rate is 92.5-98.1%. The concentration of cumene is reduced from 1.5-3% to less than 0.1%, and the removal rate is 93.3-96.7%. The concentration of α, α-dimethylbenzyl alcohol is reduced from 2-4% to less than 0.1%, and the removal rate is 90-98%. In addition, the same effect can be achieved by using the recovered solvent.

[0074] The above description is only the preferred embodiment of the present application, and the protection scope of the present application is not limited to this. Any person skilled in the art can make equivalent substitution or change according to the technical solution and the inventive concept of the present application within the technical range disclosed by the present application, and all of them should be covered in the protection scope of the present application.

Claims

1. A process for treating cumene hydroperoxide condensation wastewater, characterized by, The method comprises the following steps: (1) adjusting the pH of the condensate wastewater of cumene hydroperoxide to 4.9-8 with an acid, and transferring the wastewater to an extraction column; (2) preparing a gummy liquid foam: adding an oil phase containing an oil-soluble surfactant to an aqueous phase A containing a water-soluble surfactant A, and mechanically stirring until a foam is generated to obtain CLA; (3) preparing a gummy gas foam: using mechanical stirring to stir an aqueous phase B containing a surfactant B until a sustained volume of foam is generated to obtain CGA; (4) diluting the CLA prepared in step (2) with water, and then introducing the diluted CLA from the bottom of the extraction column; After standing for a period of time, the CGA prepared in step (3) is introduced from the bottom of the extraction column, and after the introduction is completed, the wastewater is separated from the extraction layer; The oil-soluble surfactant is at least one of Softanol 120, Softanol 30 and Tergitol 15-s-30; the oil phase is at least one of kerosene, N,N-bis(1-methylheptyl)acetamide and tributyl phosphate; The water-soluble surfactant A is at least one of sodium dodecylbenzenesulfonate and cetyltrimethylammonium bromide; The water-soluble surfactant B is at least one of sodium dodecylbenzenesulfonate and cetyltrimethylammonium chloride.

2. The cumene hydroperoxide condensate wastewater treatment process according to claim 1, characterized in that: In step (1), the acid is 20-30wt% hydrochloric acid or 50-70wt% sulfuric acid.

3. The cumene hydroperoxide condensate wastewater treatment process of claim 1, wherein: In step (1), the height-diameter ratio of the extraction column is 6.25-10.

4. The cumene hydroperoxide condensate wastewater extraction process of claim 1, wherein: In step (2), the content of the oil-soluble surfactant in the oil phase is 0.05-1.2wt%, the content of the water-soluble surfactant A in the aqueous phase A is 0.1-0.8wt%, and the mass ratio of the oil phase to the aqueous phase is (10-25):

1.

5. The cumene hydroperoxide condensate wastewater treatment process of claim 1, wherein: In step (3), the content of the water-soluble surfactant B in the aqueous phase B is 0.05-0.4wt%.

6. The cumene hydroperoxide condensate wastewater treatment process of claim 1, wherein: In step (4), the dilution ratio of the CLA is 1:(10-20), and after dilution, the mass ratio of the CLA to the wastewater is (0.4-1):1; the mass ratio of the CGA to the wastewater is (0.05-0.11):

1.

7. The cumene hydroperoxide condensate wastewater treatment process of claim 1, wherein: The speed of mechanical stirring during the preparation of CLA is 1000-1500rpm, and the stirring time is 30-60min; the speed of mechanical stirring during the preparation of CGA is 3000-5000rpm, and the stirring time is 10-30min.

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