CN107311330B

CN107311330B - Method for decoloring alcohol biochemical tail water

Info

Publication number: CN107311330B
Application number: CN201710711464.7A
Authority: CN
Inventors: 蔡建国; 石洪雁; 龚向东
Original assignee: Jiangsu Helper Functional Materials Co ltd
Current assignee: Jiangsu Helper Functional Materials Co ltd
Priority date: 2017-08-18
Filing date: 2017-08-18
Publication date: 2021-02-26
Anticipated expiration: 2037-08-18
Also published as: CN107311330A

Abstract

The invention relates to a method for decoloring alcohol biochemical tail water, which comprises the following steps: pretreatment: filtering alcohol biochemical tail water; adsorption: adsorbing the pretreated alcohol biochemical tail water by using a fixed bed filled with an adsorbing material, wherein the adsorption temperature is 10-35 ℃, and the flow rate of the alcohol biochemical tail water is 0.1-6 BV/h; desorption: desorbing and regenerating the adsorbing material with desorbing agent at flow rate of 0.6-3 BV/hr and desorption temperature of 40-60 deg.c to obtain regenerated liquid. The method for treating the alcohol biochemical tail water has good treatment effect and strong operability, and effectively solves the problem of upgrading the alcohol biochemical tail water.

Description

Method for decoloring alcohol biochemical tail water

Technical Field

The invention relates to the field of environmental protection, in particular to a method for decoloring alcohol biochemical tail water.

Background

The alcohol production adopts starch crops such as cassava, corn, sugarcane and the like as raw materials, the blocky or granular raw materials are ground into powder, water is added to mix into slurry, then the slurry is steamed and saccharified, yeast is added to ferment, and finally the finished product of the alcohol is obtained by distillation. After fermenting cassava, corn and sugarcane to extract ethanol, raw lees liquid discharged from an alcohol distillation section enters a pollution-control anaerobic tank for fermentation, then is cooled and pumped into an inclined screen for filtration, part of solid matters are removed, the lees liquid enters a primary sedimentation tank, supernatant liquid of the primary sedimentation tank after sedimentation enters a secondary UASB (upflow anaerobic sludge Blanket) for further anaerobic fermentation, secondary anaerobic effluent enters a secondary sedimentation tank for secondary sedimentation, supernatant liquid is subjected to air floatation treatment, the supernatant liquid enters an aerobic biochemical system (activated sludge process) for treatment (aerobic tank or SBR), the biochemical treatment is discharged into a tertiary sedimentation tank, the secondary air floatation is performed after the sedimentation in the tertiary sedimentation tank, organic wastewater mainly formed in ethanol production and biochemical treatment of sewage is contained in the sewage, and therefore, the pollutants are preferably removed by adopting an adsorption method after the original biochemical treatment of the sewage.

The resin adsorption method is a currently recognized and relatively effective wastewater treatment and resource technology, the Fenton method is mostly applied to the upgrading of the alcohol tail water at present, but the Fenton method can generate a large amount of sludge, and the sludge belongs to dangerous waste, so the operation cost is quite high.

Disclosure of Invention

In order to solve the technical problems, the invention aims to provide a method for decoloring alcohol biochemical tail water.

The invention provides a method for decoloring alcohol biochemical tail water, which comprises the following steps:

(1) pretreatment: filtering alcohol biochemical tail water;

(2) downstream adsorption: adsorbing the pretreated alcohol biochemical tail water by using a fixed bed filled with an adsorbing material, wherein the adsorption temperature is 10-35 ℃, and the flow rate of the alcohol biochemical tail water is 0.1-6 BV/h;

(3) desorption: and (3) desorbing and regenerating the adsorption material treated in the step (2) by using a desorption agent to obtain regenerated liquid, wherein the flow rate of the desorption agent is 0.6-3BV/h, and the desorption temperature is 40-60 ℃.

Further, the method also comprises the step of oxidizing the regeneration liquid by using an oxidizing agent, mixing the regeneration liquid with the adsorbed effluent obtained in the step (2), and discharging the mixture.

Further, the oxidant is hydrogen peroxide and ferrous sulfate.

Further, in the step (1), the alcohol is one or more of cassava alcohol, cane alcohol and corn alcohol.

Further, in the step (2), the adsorbent is a pyrrolidone group-containing adsorbent resin. The pyrrolidone-containing adsorption resin is an ion exchange resin disclosed in Chinese patent with the application number of 201410064555.2.

Further, in the step (3), the desorption agent is an aqueous solution of sodium hydroxide or an aqueous solution of potassium hydroxide.

Further, the mass fraction of the desorption agent is 10-20%.

By the scheme, the invention at least has the following advantages:

by adopting the method, the chroma of the downstream adsorption effluent can be reduced to below 60 times from the original 800 times, the COD can be reduced to below 50mg/L from the original 200 times and 500mg/L, and the ammonia nitrogen can be reduced to below 20mg/L from the original 50-200 mg/L. The adsorption material can be regenerated by aqueous solution of alkali after adsorption, and the regenerated liquid can reach the standard after being mixed with the adsorption effluent after being oxidized. The method for treating the alcohol biochemical tail water has good treatment effect and strong operability, and effectively solves the problem of the standard improvement of the cassava alcohol biochemical tail water.

The foregoing is a summary of the present invention, and in order to provide a clear understanding of the technical means of the present invention and to be implemented in accordance with the present specification, the following is a preferred embodiment of the present invention and is described in detail below.

Detailed Description

The following examples are given to further illustrate the embodiments of the present invention. The following examples are intended to illustrate the invention but are not intended to limit the scope of the invention.

The pyrrolidone-based adsorption resin (HP-308) used in examples 1 to 3 was the resin disclosed in Chinese patent application No. 201410064555.2.

Example 1

20ml of an adsorption resin (. phi.35X 250mm) containing a pyrrolidone group (HP-308) was packed in an adsorption column (. phi.35X 250mm) having a jacket for holding temperature. Filtering cassava alcohol biochemical tail water with the chromaticity of 500 times, the COD of 300mg/L and the ammonia nitrogen of 150mg/L to obtain upper column liquid, passing through an adsorption column at the temperature of 30 ℃ at the flow rate of 5BV/h, and performing adsorption treatment on 100BV wastewater, wherein the chromaticity of the adsorbed water is 45 times, the COD of 30mg/L and the ammonia nitrogen of 11 mg/L. After the adsorption of the adsorption resin is saturated, 10 percent sodium hydroxide aqueous solution is adopted for desorption, the temperature is 50 ℃, and the flow is 1BV/h, so as to obtain regeneration liquid. The regenerated liquid is oxidized by 2 percent hydrogen peroxide and ferrous sulfate and then mixed with the absorbed effluent to reach the discharge standard.

Example 2

200ml of a pyrrolidone-based adsorbent resin (. phi.60X 600mm) was packed in an adsorption column (. phi.60X 600mm) having a heat-retaining jacket. Collecting corn alcohol biochemical tail water with the chroma of 600 times, the COD of 380mg/L and the ammonia nitrogen of 160mg/L, filtering the corn alcohol biochemical tail water to be used as upper column liquid, passing through an adsorption column at the temperature of 20 ℃ at the flow rate of 4BV/h, and performing adsorption treatment on 120BV wastewater, wherein the chroma of the adsorbed effluent is 42 times, the COD is 45mg/L and the ammonia nitrogen is 17 mg/L. After the adsorption of the adsorption resin is saturated, desorption is carried out by adopting a 20 percent sodium hydroxide aqueous solution at the temperature of 55 ℃ and the flow rate of 1.5BV/h, and a regeneration liquid is obtained. The regenerated liquid is oxidized by 3 percent hydrogen peroxide and ferrous sulfate and then mixed with the absorbed effluent to reach the discharge standard.

Example 3

800ml of an adsorption column (. phi.100X 1000mm) equipped with a heat-retaining jacket was packed with pyrrolidone-based adsorption resin (HP-308). Taking cane alcohol biochemical tail water with the chromaticity of 700 times, the COD of 500mg/L and the ammonia nitrogen of 135mg/L, filtering the cane alcohol biochemical tail water to be used as upper column liquid, passing through an adsorption column at the temperature of 22 ℃ and the flow of 4.5BV/h, and performing adsorption treatment on 120BV wastewater, wherein the chromaticity of the adsorbed water is 38 times, the COD of 35mg/L and the ammonia nitrogen of 16 mg/L. After the adsorption of the adsorption resin is saturated, desorption is carried out by adopting 15 percent sodium hydroxide aqueous solution at the temperature of 60 ℃ and the flow rate of 2BV/h, and regeneration liquid is obtained. The regenerated liquid is oxidized by 2.6 percent hydrogen peroxide and ferrous sulfate and then mixed with the absorbed effluent to reach the standard and be discharged.

Commercial resins were used for comparison, see examples 4-7.

Example 4

The pyrrolidone-group-containing adsorption resin in example 1 was replaced with a strongly acidic ion exchange resin 001 under the same conditions as those in the above example, and the throughput was 20 BV.

Example 5

The pyrrolidone-group-containing adsorbent resin of example 1 was replaced with the weakly acidic ion exchange resin 111 under the same conditions as the other operations, and the throughput was 36 BV.

Example 6

The pyrrolidone-based adsorption resin in example 2 was replaced with the strongly basic ion exchange resin 201, and the treatment amount was 18BV without changing the other operation conditions.

Example 7

The pyrrolidone-based adsorption resin in example 3 was replaced with a weakly basic ion exchange resin 301, and the treatment amount was 40BV without changing the other operation conditions.

Comparing examples 4-7 with examples 1-3, it can be seen that the treatment effect of the other resins is significantly worse than that of the pyrrolidone-based adsorption resin (HP-308), and the treatment amount is much lower than that of the resins of examples 1-3.

The above description is only a preferred embodiment of the present invention and is not intended to limit the present invention, it should be noted that, for those skilled in the art, many modifications and variations can be made without departing from the technical principle of the present invention, and these modifications and variations should also be regarded as the protection scope of the present invention.

Claims

1. The method for decoloring the alcohol biochemical tail water is characterized by comprising the following steps of:

(1) pretreatment: filtering the alcohol biochemical tail water;

(2) adsorption: adsorbing the pretreated alcohol biochemical tail water by using a fixed bed filled with an adsorbing material, wherein the adsorption temperature is 10-35 ℃, and the flow rate of the alcohol biochemical tail water is 4-5 BV/h; the adsorbing material is pyrrolidone group-containing adsorbing resin;

(3) desorption: and (3) desorbing and regenerating the adsorption material treated in the step (2) by using a desorption agent to obtain regenerated liquid, wherein the flow rate of the desorption agent is 0.6-3BV/h, the desorption temperature is 40-60 ℃, the desorption agent is an aqueous solution of sodium hydroxide or an aqueous solution of potassium hydroxide, and the mass fraction of the desorption agent is 10-20%.

2. The method of claim 1, wherein: and (3) oxidizing the regeneration liquid by using an oxidant, mixing the regeneration liquid with the adsorbed effluent obtained in the step (2), and discharging.

3. The method of claim 2, wherein: the oxidant is hydrogen peroxide and ferrous sulfate.

4. The method of claim 1, wherein: in the step (1), the alcohol is one or more of cassava alcohol, cane alcohol and corn alcohol.