EP1483204A1

EP1483204A1 - Preparation of waste water containing sodium chloride for use in chlor-alkali electrolysis

Info

Publication number: EP1483204A1
Application number: EP03702616A
Authority: EP
Inventors: Jürgen HEUSER; Werner Verhoeven; Domien Sluyts
Original assignee: Bayer MaterialScience AG
Current assignee: Covestro Deutschland AG
Priority date: 2002-02-22
Filing date: 2003-02-10
Publication date: 2004-12-08
Also published as: JP2005517624A; WO2003070639A1; DE10207442A1; TW200306952A; US20050115901A1; CN1646429A; AU2003205750A1

Abstract

The invention relates to a method for preparing waste water containing sodium chloride. Said method is characterized in that an aqueous sodium chloride solution is obtained by a specific sequence of acidulation, extraction, alkalization and stripping steps. The sodium chloride solution can then be used immediately for chlor-alkali electrolysis.

Description

Treatment of waste water containing table salt for use in chlor-alkali electrolysis

The present invention relates to a process for the treatment of saline wastewater, characterized in that an aqueous saline solution is obtained by a certain sequence of acidification, extraction, alkalization and stripping steps, which can be used directly in chlor-alkali electrolysis ,

Saline wastewater is produced in many chemical processes. For example, in the phase interface process for the production of polycarbonate, or the production of diphenyl carbonate also in the phase interface process and many other chemical reactions in which sodium chloride is formed directly or indirectly (see, for example, Schnell, “Chemistry and Physics of Polycarbonates”, polymer

Reviews, Volume 9, hrterscience Publishers, New York, London, Sydney 1964, pp. 33 ff.)

Many methods are already known for cleaning such waste water, e.g. Activated carbon adsorption, distillation, extraction or ozonolysis. The cleaned wastewater is then freed of most impurities, but the wastewater is not suitable for being discharged into the environment due to the remaining common salt. For example, it is particularly problematic if it is discharged into freshwater areas that may still be used for drinking water supply.

The question therefore arises as to how such waste water could be better disposed of. A possible option would be the use of such waste water in chlor-alkali electrolysis. Firstly, this would not pollute the environment with salt, secondly, resources would be saved and raw material costs would be saved. For use in chlor-alkali electrolysis, however, only waste water is considered which contains chlorides as anions practically exclusively. Therefore, wastewater, which still contains other anions and organic impurities, must be treated accordingly beforehand.

For example, wastewater generated in the production of polycarbonate or diaryl carbonate contains carbonate from phosgene hydrolysis in addition to saline concentrations of 2 to 20%. In addition to these inorganic salts, organic contaminants are also present. So there are still residues of phenols or bisphenols, catalyst and solvent. All these

Impurities would have to be reduced to a minimum to enable use in chlor-alkali electrolysis.

From EP AI 0 396 790 it is known that resulting, dilute solutions can be worked up by reactive extraction steps in such a way that a usable concentrate of certain constituents is obtained. However, no closed solution for all solution flows is disclosed. Nothing is said about a possible purification of a saline wastewater stream for use in chlor-alkali electrolysis.

Similar work-up methods using physical extraction steps are also known to the person skilled in the art (see, for example, Ulimann's Enyclopedia of industrial chemistry Volume B3, pages 6.3 to 6.6.) Here, however, only dilute wastewater streams are cleaned by extraction methods in such a way that the contaminants are converted into more concentrated solutions, which are then converted have it disposed of much more easily and cost-effectively.

From DE-A 195 10 063 it is known that reaction salts containing saline, such as are obtained, for example, from the interfacial processes for polycarbonate or diphenyl carbonate synthesis, can be worked up by means of reactive extraction after acidification in such a way that a solution suitable for introduction into the environment is obtained becomes. It is also pointed out that this solution can be used in chlor-alkali electrolysis after appropriate concentration. However, the process described there is not suitable for directly delivering a solution suitable for use in chlor-alkali electrolysis. The residual organic load still present according to this process would also be concentrated if it was concentrated, making the solution unsuitable for chlor-alkali electrolysis. Even in the solution that can be obtained by this method without concentration, the residual organic load would still be too high to use the solution in the membrane method preferred today for chlor-alkali electrolysis. For example, DE-A 195 10 063 only discloses waste water with a COD value of preferred

<100 ppm, in the examples at least 34 ppm. This waste water would not be suitable for use in chlor-alkali electrolysis.

These known processes for the treatment of process wastewater accordingly do not lead directly to a saline-containing solution suitable for use in chlor-alkali electrolysis, in particular according to the membrane process. There is also no indication that it could be possible to achieve this using the techniques available to date.

Based on the prior art, it was therefore the task of making an improved treatment process for saline wastewater available, which leads to saline solutions which are suitable for direct use in chlor-alkali electrolysis, and to a use which is as closed as possible of the partial streams while receiving the smallest possible amount of waste.

It has now surprisingly been found that saline process wastewater can be treated in such a way that the remaining saline solution can be used directly in the chlor-alkali electrolysis by using the process wastewater acidified with HCI and then degassed with an organic solvent, the aqueous phase alkalized and stripped with steam.

The method according to the invention achieves the following surprising advantages over the known methods of the prior art:

1. The salt solution obtained can be used directly in the electrolysis, a concentration is not necessary. In the case of membrane electrolysis, salt cleaning is no longer necessary and the water can be recycled.

2. The amount of salt and water is reduced.

3. In the case of diphenyl carbonate production, the diphenyl carbonate residues present as impurities in the wastewater become during the extraction

Phenol implemented.

4. The extracted phenols can be used again as raw materials in the synthesis.

5. Only small amounts of waste water remain, which benefits the environment. 6. The method can also be used without the use of components

Reactive extraction are operated. 7. The COD value achieved in the treated wastewater is below 30 ppm and thus below the application limit of the COD process. The value is therefore not exactly determinable but very low. 8. Content of phenolic impurities <1 ppm, phenol of <0.3 ppm, bisphenol below the detection limit, catalyst residues <1 ppm and organic solvent <1 ppm.

In the process according to the invention, the wastewater from the reaction is first with HCl, preferably with commercially available 37% aqueous acid, up to a pH of 1-5, preferably from 3 to 4, very particularly preferably 3 acidified. The carbonates are thus converted into carbonic acid, which escapes as a gas. The carbonic acid can possibly be recovered in order to convert it to CO in a reformer. Furthermore, phenolic anions are converted into the corresponding free phenolic compounds.

The acidic solution is then brought into contact with an extractant. Apolar organic solvents such as e.g. Methylene chloride, chlorobenzene or a mixture of these two, MIBK (methyl isobutyl ketone) or ether, preferably methylene chloride, chlorobenzene or a mixture of these two, can be used. Alternatively, you can use a non-soluble one

Base, preferably long chain tertiary amines such as e.g. Use alamin or tri-iso-octyl-amine, especially tri-iso-octyl-amine, as the reactive extractant, dissolved in inert apolar organic solvents such as petroleum fractions, e.g. Shell-Sol AB. However, physical extraction with inert organic solvents is preferred. This removes the phenolic compounds and other organic compounds from the aqueous solution. This extraction takes place in several, preferably 4-10 stages. Mixer-settlers or extraction columns, preferably extraction columns, particularly preferably pulsed filling or sieve plate columns, can be used for this purpose, see FIG. z. B. Perry's Chemical Engineering Handbook, Mc Graw Hill, New York,

1999, 15-44 to 15-46. A ratio of organic phase to aqueous phase of 5: 1 to 1: 5, preferably from 3: 1 to 1: 3, very particularly preferably from 1: 2 is aimed for.

The organic extraction phase obtained is then with an aqueous

Sodium hydroxide solution, in a concentration of 1-30%, preferably 5 to 20% NaOH, re-extracted. Here, the alkaline aqueous phase is used in a significant deficit as an extractant in order to achieve the highest possible phenolate concentrations in the alkaline aqueous phase. For the extraction with aqueous sodium hydroxide solution, a ratio of aqueous sodium hydroxide solution to organic phase of about 1:50 to 1: 1000, preferably 1: 400 to 1: 1000, would suffice. The exact However, ratios depend on the concentration of phenol in the organic phase to be worked up, since it is a reactive extraction in which approx. 1.1-1.5, preferably 1.2-1.3, particularly preferably 1.25 mol NaOH per mol phenol must be used. Accordingly, the amounts must be adjusted to the concentration of phenol in the organic phase. However, in order to obtain a miscible ratio, which is not the case at ratios of 1:50 to 1: 1000, sodium hydroxide solution is circulated, whereby an actual ratio of sodium hydroxide solution circulated to organic phase of approximately 1:10 is achieved. A partial stream is taken from each of the circulated sodium hydroxide solution, which is replaced by fresh alkali. The ratio taken

Partial flow to mass flow of the extracted organic phase now corresponds to the above-mentioned ratio. The aqueous extract obtained in this way can be treated further in order to recover phenols.

A preferred procedure is that the re-extraction with sodium hydroxide solution is carried out in two stages. In the first extraction step, extralation is carried out with an aqueous sodium hydroxide solution / phenolate solution, which is formed from the partial stream removed in the second extraction stage with the addition of additional NaOH to restore the concentration of 1-30%, preferably 5 to 20%, as described above. The partial stream obtained in this stage is fed directly to the phenol recovery and a corresponding amount of lye from the second stage as fresh lye, with the addition of additional NaOH to restore the concentration of 1-30%, preferably 5 to 20% NaOH, again. In the second extraction step, a concentration of 1-30%, preferably 5 to 20% NaOH, is extracted with NaOH, as described above, the partial stream removed being replaced by fresh liquor and this partial stream, with the addition of additional NaOH, to restore the concentration of 1-30 %, preferably 5 to 20% NaOH, is added as a fresh extractant to the first stage. As the partial stream taken from the first stage, a concentrated aqueous-alkaline solution of the phenolates is obtained, from which simply by neutralizing with

HCI two phases arise, which are separated in a simple separation container can. In this way you get an upper phase, which contains about 90% of the phenane amount, and which can either be used again in a synthesis (eg DPC) or otherwise eliminated. The other phase consists of an aqueous saline solution slightly contaminated with phenol and is returned to the reaction wastewater to be processed.

The content of phenolic compounds in the organic phase is reduced to below 1 ppm by this re-extraction. The organic phase thus freed from phenolic compounds is returned to the extraction of the reaction waste water as the extraction agent. The two-stage re-extraction can be designed, for example, in the form of a countercurrent extraction. These re-extractions are preferably carried out in a mixer-settler, e.g. as described in Perry's Chemical Engineering Handbook, Mc Graw Hill, New York, 1999, 15-22 to 15-29.

The extracted saline process wastewater, largely freed from phenolic and other organic compounds, is now alkalized with aqueous sodium hydroxide solution of any concentration, for example 1-50% NaOH, to a pH of 7-13, preferably 8-12, and with steam at 1- 4, preferably 2-3, particularly preferably 2.5 bar in a stripping column, see. e.g. "Azeotropic Distillation" in Perry's Chemical

Engineering Handbook, Mc Graw Hill, New York, 1999, 13-68 to 13-75, stripped. The amount of water vapor is related to the amount of solution to be stripped, such as 1-5, preferably 2-4, particularly preferably 3-3.5 to 100. In this step, both the catalyst and the residual solvent are removed. The top gases of the column therefore contain the catalyst and residual solvent, are condensed and can be returned to the synthesis reaction. The bottom product is a pure saline solution, which can now be used directly in chlor-alkali electrolysis. The content of residual organics in the saline solution thus prepared is <0.3, preferably <0.1 ppm, bisphenols and catalyst residues are no longer detectable and the residual content of organic solvents is <lppm, preferably <0.1 ppm.

Unless expressly stated otherwise, all steps of the process according to the invention are carried out at temperatures below the lowest boiling point of the solvents used in each case and at atmospheric pressure. If necessary, however, the steps can also be carried out at temperatures above these temperatures with a correspondingly adapted pressure.

The following diagrams are intended to illustrate the method according to the invention and explicitly the re-extraction without, however, restricting the subject matter of the present invention.

Examples:

The following examples are intended to illustrate the present invention without restricting it:

example 1

Wastewater from diphenyl carbonate production contains 200 ppm phenol, 30 ppm ethyl piperidine (EPP), 2 ppm diphenyl carbonate and 0.25% sodium carbonate.

98 kg of this wastewater are brought to pH 4 with 2 kg of 37% hydrochloric acid and degassed. The residual concentration of carbonate ions is less than 200 ppm.

This solution is then in an extraction column with a length of 5 meters,

0.05 meter diameter and 50 sieve trays extracted with half the amount (weight ratio) of methylene chloride.

The phenol concentration in the wastewater after the extraction column is <200 ppb. The ratio of wastewater to extractant (methylene chloride) is 2: 1.

The resulting 50 kg of solvent, which contains 400 ppm phenol and 4-5 ppm diphenyl carbonate, are re-extracted in 2 mixer settlers in a countercurrent process with 250 g 20% sodium hydroxide solution. The re-extract is neutralized with 241 g 37% HCI. This solution separates and gives 19 g of organic

Phase (95% phenol) and 493 g water phase (1% phenol) at pH 4. These 493 g aqueous phase are returned to the fresh waste water in the start of extraction. 50 kg of cleaned, water-containing solvent is returned to the extraction. 100 kg of extracted reaction wastewater from the extraction is then stripped in a stripper with 3.15 kg of water vapor at 2.5 bar. The top distillate left is 1.03 kg of water containing EPP and methylene chloride, which can be fed back into the synthesis. 102.3 kg of an aqueous saline solution with 15-18% sodium chloride and <1 ppm EPP and <1 ppm methylene chloride remain at the bottom.

The COD is 28 ppm and can therefore no longer be measured reproducibly because the sensitivity of the method is insufficient. The high NaCl content of the solution also leads to increased measured values so that the actual COD is still significantly lower.

Claims

claims

1. A process for the purification of chloride-containing wastewater, which contains acids, bases and solvent residues, characterized in that the wastewater is worked up by acidification, subsequent extraction, alkalizing and stripping.

2. The method according to claim 1, characterized in that the waste water originates from the phase boundary process for polycarbonate or diphenyl carbonate production.

3. The method according to claim 1, characterized in that first carbonates are removed by acidification and degassing.

4. The method according to claim 1, characterized in that the phenolic and other organic compounds are removed by extraction with solvent.

5. The method according to claim 1, characterized in that the acids are removed by extraction with bases in a reactive extraction.

6. The method according to claim 1, characterized in that the extraction is carried out in a column.

7. The method according to claim 1, characterized in that the phenolic compounds are recovered by re-extraction of the organic extractant with aqueous alkaline solution and subsequent neutralization of the aqueous re-extract.

8. The method according to claim 7, characterized in that the re-extraction is carried out in mixer settlers.

9. The method according to claim 7, characterized in that the re-extractions are carried out according to the countercurrent principle.

10. The method according to claim 7, characterized in that the re-extraction is carried out in two stages.