The method of obtaining crystalline sodium acetate from waste products chemical products

 

(57) Abstract:

Usage: salts of lower carboxylic acids, sodium acetate, processing effluents and gaseous emissions from the production of triacetin. The inventive liquid effluents and gaseous emissions mixed with acetic acid in the production of triacetin neutralized with alkali, the resulting aqueous solutions with a content of 5-28% sodium acetate evaporated at 80-95°C. and a residual pressure of 0.5-0.8 kg/cm2. One stripped off the solution is cooled, crystallized, salt is filtered off and dried the resulting sodium acetate.

The invention relates to waste disposal and the simultaneous achievement of commercial products and can be used in other industries where liquid wastes with a content of acetic acid.

The prior art method of obtaining sodium acetate crystal presents known how to obtain it.

A method of obtaining acetic acid (acetate) sodium from methylacetanilide liquid saponification their aqueous alkali at 60-70aboutWith subsequent evaporation of the reaction mixture prior to crystallization, as a result of the crystalline monoliths salt the Oia methanol and sodium acetate by distillation of the methanol-methylacetate waste polyvinyl alcohol or polyvinylacetate emitting cubic product aqueous methanol and distillate - azeotropic methylacetophenone mixture with impurities such as acetaldehyde and dimethylacetal using aqueous-alkaline treatment and distillation of acetaldehyde and other products of fractions from an aqueous solution of sodium acetate using a cation exchanger.

The disadvantage of this method is the complexity of its process.

Closest to the proposed method is a method of obtaining sodium acetate, which take the waste polyvinyl alcohol containing 15% acetate, 50% methanol and 35% water, and rectificatum emitting azeotropic mixture comprising about 70% of acetate and 30% methanol.

This mixture is loaded into the reactor-malitel and amyraut equimolecular amount of alkali, which is injected in aqueous solution. After saponification of the reaction mixture is distilled methanol to the salt content in the solution is about 60%, which is then purified by known methods. The obtained salt is solvated acetate sodium - CH3The N 3H2O. the product Analysis, % : sodium Acetate 60 Water 39,9834 Chlorides 0,007 Iron 0,0006 Insoluble part 0,009

The disadvantage of this method is that its implementation requires large expenditures on cleaning mutilator> The essence of the proposed sooba is to use the waste products of triacetin (liquid waste, gas emissions) to obtain acetic acid sodium neutralization.

The advantage of the proposed method is to obtain a product of higher quality, reduced complexity, reduced environmental pollution.

The possibility of carrying out the invention is confirmed by the description of the method.

P R I m e R 1. Liquid fraction from the production of triacetin content,% : Acetic acid 2,25 Insoluble residue 0,00031 Water 97,74969

served in the reactor-Converter continuous action in the amount of 4500 kg/h and neutralized equimolecular amount of alkali (67,55 kg/h), which imposed a 20% aqueous solution (337,75 kg/h) at a temperature of 30-65aboutC and pH 7-9 aqueous solution of sodium acetate, with continuous removal of the neutralized solution. The obtained neutralized aqueous solution of sodium acetate in the amount of 4837,75 kg/h with content, %: sodium Acetate 2,86 Water 97,1359 Insoluble residue 0,0041

direct evaporator apparatus continuous action in the amount of 6000 kg/h, where 80-85aboutWith a vacuum of at least 0.5 kgf/cm2is evaporation. The upar is Arat-mould, where it is cooled to a temperature not above 35aboutC.

Bicrystalline salt is filtered and dried on the vacuum filter.

The obtained salt is solvated sodium acetate CH2The Na 3H2About content of about 40% moisture.

The product analysis, %:

The appearance of a Homogeneous crystal

"powder light - lo-yellow sodium Acetate 60,1 Water 39,8925 Insoluble residue 0,0071

the pH of a 25% aqueous solution of sodium acetate 8,0

The filtrate, after filtering and drying in vacuum filters, content, %:

Sodium acetate 27,5

Water 72,4937

The insoluble residue 0,0063

at 10% (29 kg/h) from one stripped off solution sent for re-evaporation neutralized with a sodium acetate solution.

The condensate water in the amount of 94% (4547,49 kg/h) from the initial solution of sodium acetate content, %: Water 99,9945 non-volatile residue 0,0055

drained into the sewer.

The yield of sodium acetate monohydrate from theoretical 93,73% (130 kg/h).

Loss 5,77% (7,98 kg/h) with the filtrate sodium acetate.

0,5% (0,69 kg/h) for filtering and packaging.

Considering the return of the filtrate to re-evaporation

the output of the AC shall/P> P R I m m e R 2.

Liquid fraction from the production of triacetin content, %: Acetic acid 11,21 Water 88,78969 Insoluble residue 0,00031

served in the reactor-Converter continuous action in the amount of 4500 kg/h and neutralized equimolecular amount of alkali (336,33 kg/h), which imposed a 20% aqueous solution (1681,75 kg/h) at 30-65aboutC and pH 7-9 aqueous solution of sodium acetate with continuous removal of the neutralized solution.

The obtained neutralized aqueous solution of sodium acetate (6181,75 kg/h) content, %: sodium Acetate of 11.15 Water 88,8451 Insoluble residue 0,0041

direct evaporator apparatus with continuous action and next, as in example 1.

The filtrate in an amount of 10% (136 kg/h) from one stripped off solution sent for re-evaporation.

The condensate water in the amount of 78% (4821,77 kg/h) from the initial solution of sodium acetate content, %: Water 99,9945 non-volatile residue 0,0055

drained into the sewer.

The yield of sodium acetate from theoretical 94,02%.

Loss 5,42% (37,4 kg/h) with the filtrate sodium acetate, 0.5% of (3,45 kg/h) for filtering and packaging.

Considering the return of the filtrate to re-evaporation of the output of sodium acetate O3. Liquid fraction from the production of triacetin content, %:

Acetic acid was 6.73

The insoluble residue 0,00031

Water 93,26969

served in the reactor-Converter continuous action in the amount of 4500 kg/h and neutralized equimolecular amount of alkali (reach 201.9 kg/h), which imposed a 20% aqueous solution (1009,5 kg/h) at 30-65aboutC and pH 7-9 aqueous solution of sodium acetate, with continuous removal of the neutralized solution. The obtained neutralized aqueous solution of sodium acetate in the amount of 5509,5 kg/h with content, %: sodium Acetate 7,51 Water 92,4859 Insoluble residue 0,0041

Direct evaporator apparatus with continuous action and next, as in example 1.

The filtrate in an amount of 10% (74,16 kg/h) from one stripped off solution sent for re-evaporation.

The condensate water in the amount of 86,58% (4767,92 kg/h) from the initial solution of sodium acetate content, %:

Water 99,9945

Non-volatile residue 0,0055

drained into the sewer.

The yield of sodium acetate from theoretical monohydrate 94,58%.

Loss to 4.92% (20,39 kg/h) with the filtrate sodium acetate, 0.5% of (2,07 kg/h) for filtering and packaging.

Considering the return of the filtrate to re-evaporation output acetate is aretina in the amount of 12,000 m3/h containing 2 lhs/l acetic acid, treated in the column of chemisorber 16% aqueous alkali solution with a flow rate of 30000-40000 kg/h

The absorbent solution circulating in the system to achieve a pH of 7-9, which corresponds to the following content of the solution, %:

Sodium acetate 24,7

Water 75,2952

Insoluble in water balance 0,0048

The feeding capacity of chemisorber (3000 kg) is 41 PM

The resulting solution in the amount 3894 kg sent to an evaporation apparatus, and then, as in example 1.

P R I m e R 5. Gas emissions from the production of triacetin in the amount of 12,000 m3/h containing 5 lhs/l acetic acid, treated in the column of chemisorber 16% aqueous alkali solution with a flow rate of 30000-40000 kg/h

The solution absorber circulates in the system to achieve a pH of 7-9, which corresponds to the following contents dissolve RA,%: sodium Acetate 24,7 Water 75,2952

Insoluble in water balance 0,0048

The feeding capacity of chemisorber (3000 kg) 16.4 h

The resulting solution in the amount 3894 kg sent to an evaporation apparatus, and then, as in example 1.

P R I m e R 6. Gas emissions from the production of triacetin in the amount of 12,000 m3/h, content the course 30000-40000 kg/H. The absorbent solution circulating in the system to achieve a pH of 7-9, which corresponds to the following solution composition, % : sodium Acetate 24,7 Water 75,2952 Insoluble residue 0,0048

The feeding capacity of chemisorber (3000 kg) is 21,28 PM

The resulting solution in the amount 3894 kg sent to an evaporation apparatus, and then, as in example 1.

A comparative analysis of the obtained product with the prototype shows that it has higher qualities on the base material, the content of insoluble impurities, it does not contain chlorides, iron.

The METHOD of OBTAINING CRYSTALLINE SODIUM ACETATE FROM WASTE products CHEMICAL PRODUCTS processing flows in an aqueous solution of sodium hydroxide, followed by evaporation of the resulting solution of sodium acetate, cooling, crystallization of salts, separating and drying the crystalline product, characterized in that as a waste use of waste water or gas emissions to the process of getting triacetin with the content of acetic acid in water flows 2 - 11.5 wt. % and in gas emissions - 2 - 5 mg/l, and a solution of sodium acetate evaporated at 80 - 85oWith a residual pressure of not less than 0.5 kg/

 

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