SU1738758A1 - Ion-exchange method of cleaning sewage from nickel - Google Patents

Ion-exchange method of cleaning sewage from nickel Download PDF

Info

Publication number
SU1738758A1
SU1738758A1 SU904861695A SU4861695A SU1738758A1 SU 1738758 A1 SU1738758 A1 SU 1738758A1 SU 904861695 A SU904861695 A SU 904861695A SU 4861695 A SU4861695 A SU 4861695A SU 1738758 A1 SU1738758 A1 SU 1738758A1
Authority
SU
USSR - Soviet Union
Prior art keywords
nickel
ion
cation exchanger
exchanger
exchange
Prior art date
Application number
SU904861695A
Other languages
Russian (ru)
Inventor
Галина Михайловна Колосова
Николай Георгиевич Скворцов
Original Assignee
Институт геохимии и аналитической химии им.В.И.Вернадского
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Институт геохимии и аналитической химии им.В.И.Вернадского filed Critical Институт геохимии и аналитической химии им.В.И.Вернадского
Priority to SU904861695A priority Critical patent/SU1738758A1/en
Application granted granted Critical
Publication of SU1738758A1 publication Critical patent/SU1738758A1/en

Links

Abstract

The invention relates to a method of ion-exchange wastewater treatment from nickel, in particular, cleaning the washing waters of the nickel-plating process, in engineering, metallurgical, electrical, electronic and other enterprises of the industry with the return of purified water and for creating local systems of waste-free technology and allows reduce the cost and speed up the cleaning process, as well as reduce the number of ion-exchangers and reagents used. The method of ion-exchanging wastewater from nickel is carried out by passing water through ion-exchange sorbents with their subsequent regeneration, while a mixture of weakly acidic cation exchanger in hydrogen form and strongly basic anion exchanger in hydroxyl form with ratio 1: 1 is used as ion exchange sorbents. Before regeneration, the mixture of ion exchangers is separated by supplying water in countercurrent at a speed of 3.9 V 1.1 cm / s and is regenerated separately. 3 tab. (Ls

Description

The invention relates to a method for purifying wastewater from nickel, in particular, to ion-exchange methods for purifying wastewater from the process of nickel plating and recycling water supply, can be used for engineering, metallurgical, electrical, electronic and other industries with the return of treated water for creation of local systems of waste-free technology.
There are several methods for treating nickel-containing wastewater: reagent, biological, sorption, and others. It is most expedient to use an ion exchange method for cleaning waste water and extracting nickel in order to return it to the production process.
The essence of the known methods of cleaning wastewater from nickel using ion exchangers consists in passing them through a layer of cation exchanger followed by desorption of nickel with an acid solution.
The closest to the proposed technical essence and the achieved result is a method for extracting nickel from wastewater, including the sequential passage of water through two columns: the first with a weakly acidic cationic KB-4 in sodium form; the second — a mixed action filter — is loaded with a mixture of a strongly acidic cation exchanger KU-2 in
vj GO 00 SL
00
hydrogen form and strongly basic anionite AB-17 in hydroxyl form.
The disadvantage of this method is the use of weak acid cation in sodium form, which is associated with the additional treatment of the sorbent with sodium hydroxide after its regeneration with acid in order to extract nickel. This increases the cost of the process due to the additional technological operation on the first column (conversion of the ion exchanger into the salt form after acid regeneration) and the additional consumption of expensive sodium hydroxide reagent. In addition, with such a scheme, an equivalent amount of sodium is extracted from the first column of the cation exchanger in the purified water during extraction of nickel, which, in addition to the anion exchanger, must additionally provide for the addition of a strongly acidic cation exchanger or filter of mixed action (FSD).
The aim of the invention is to reduce the cost of the process by eliminating the stage of converting a weakly acidic cation exchanger to the sodium form, reducing the number of ion exchangers and reagents used, reducing the number of filters (ion exchange columns) and cleaning time.
In the process of sewage treatment, nickel extraction and recycling water supply, a mixture of weak acid cation exchanger in the hydrogen form and a strongly basic anion exchanger in the hydroxyl form are used as the sorbent material. Before regeneration, the mixture of ion exchangers is separated by supplying water in countercurrent at a rate of 3.9 - V 1.1 cm / s and is regenerated separately. The proposed method makes it possible to refuse the transfer of the hydrogen form of a weakly acidic cation exchanger to a salt form and to eliminate the column with a strongly acidic cation exchanger for sorption of the released sodium and other monovalent cations. The use of the known method only allows the extraction of nickel from wastewater, in which sodium ion in equivalent quality enters, the accumulation of which makes it difficult to reuse nickel-free wastewater.
about
Example. A column with a cross section of 1.0 cm is loaded with a mixture of cation exchanger KB-4 in hydrogen form and anion exchanger AB-17 in hydroxyl form at a ratio of 1: 1 over the exchange capacity with a uniform distribution of both ionites across the height of the layer (3 cm). 1000 ml is passed through the column.
a solution containing 100 mg Ni / l at a rate of 0.3 bpm./min. Sorbents are separated from the bottom with a linear velocity of 5–10 cm / s, the AB-17 anion exchange resin floats up, and the KB-4 cation exchanger spent on nickel remains at the bottom of the column. The KB-4 cation exchanger is regenerated with a 0.5N solution of sulfuric (or hydrochloric) acid, and the separated anion exchanger is regenerated with a 0.5N solution of sodium hydroxide. After regeneration, the sorbents are mixed and reused for water purification,
In tab. Figure 1 shows the results of purification of wash water from nickel at different degrees of purification (one and two orders) on weak acid cation exchanger used in various variants, at a solution passing rate of 60 ml / h, nickel concentration 100 mg / l, sorbent bed height 3.0 cm, column diameter 1.0 cm
From tab. 1 it follows that when using a mixture of weak acid cation exchanger in the hydrogen form and a strongly basic anion exchanger in the hydroxyl form, the volume of purified water increases by 100 times compared to using only the hydrogen form of the cation exchanger and more than doubled when using the sodium form of the cation exchanger under other equal conditions x experiment.
From tab. 1 that the effect is achieved by reducing the smearing of the equilibrium nickel front as it moves along the mixed layer of sorbents.
In tab. Figure 2 shows data on the degree of nickel extraction at different ratios of a weakly acid cation exchanger and a strongly basic anion exchanger in the mixture.
From tab. 2 it follows that the ratio of ion exchangers in exchange capacity 1: 1 is optimal, since it ensures the equivalence of exchange. With less than 1: 1, the amount taken in the mixture of anion exchange resin, nickel ion slip into the filtrate is observed: at a ratio of 1: 0.5 C / Co 0.16, at a ratio of 1: 0.75 C / Co 0.03 due to that the capacity of a weak acid cation exchanger is not fully utilized.
At more than 1: 1 amount taken in a mixture of an anion in the column, precipitation of nickel hydroxide is observed. At the same time, the volume of water purified from nickel increases, but the hydrodynamics of the process deteriorates significantly, the ion exchanger layer becomes clogged with nickel hydroxide, and the filtration rate slows down.
After processing the mixed layer of sorbents, they are separated by supplying water
countercurrent with a linear velocity of 3.9 to 1.1 cm / s.
In tab. 3, the rationale for the water supply rate for separation of a mixture of ion exchangers before regeneration is provided.
Separated ion exchangers are regenerated separately: cation exchanger - 0.5 N. sulfuric or hydrochloric acid solutions; anion exchanger — 0.5N sodium hydroxide solution (this method of regeneration is used in ion exchange processes).
Thus, the proposed method by using a mixture of a weak acid cation exchanger in hydrogen form and a strongly basic anion exchanger in hydroxyl form and a special technique for separating the spent ion exchanger mixture before regeneration allows the wastewater to be cleaned of nickel to the required concentration and returned to the wash bath, as well as nickel recovery in the form of a concentrated solution and using it to adjust the nickel baths.
The method makes it possible to exclude the transfer of a weakly acid cation exchanger to the sodium form after acid regeneration; use additionally strong acid
cation exchanger for sodium extraction, thus reducing the cost of wastewater treatment and speeding it up by reducing the number of operations.
Techno-economic advantage of the proposed method is to reduce technological operations and obtaining a larger volume of purified to the necessary degree of water.

Claims (1)

  1. Invention Formula
    The method of ion exchange wastewater treatment from nickel by passing water through ion exchange sorbents with their subsequent regeneration, characterized in that, in order to reduce the cost and speed up cleaning, reduce the amount of ion exchangers and reagents, a mixture of weakly acidic cation exchanger in hydrogen form is used as ion exchange sorbents and strong base anion exchanger in hydroxyl form at a ratio of 1: 1 for exchange capacity, while before regeneration
    5, the ionite mixture is separated by feeding water in countercurrent at a speed of 3.9 - V 1.1 cm / s and is regenerated separately.
    Table 1
    Form of weak acid cation exchanger
    The volume of water purified from nickel, ml. with C / Co
    0.1
    0.01
    Hydrogen cation exchanger 1.2 ml mixed with inert styrene copolymer and DVB 1.8 ml
    1.2 ml cation exchanger in sodium form mixed with inert copolymer of styrene and DVB 1.8 ml
    Cationite 1/2 ml in the hydrogen form in a mixture with strongly basic anioiite in the hydroxyl form 1.8 ml; ratio of exchange capacity 1: 1
    0.1
    0.01
    11.0
    3.6
    270.0
    160.0
    410.0
    360,0
    Water flow rate, cm / s
    , one,,
    3, 1
    1, 4, 4
    table 2
    Table 3
    Behavior of ionites
    Layer is motionless
    separation of components The separation of a layer of ionites to cation exchanger in nickel form (at the bottom of the column) and anion exchanger in
    sulphate form (top of column)
    Anion exchange ash is observed with a stream of water.
    Ablation of anion exchanger and cation exchanger
SU904861695A 1990-08-22 1990-08-22 Ion-exchange method of cleaning sewage from nickel SU1738758A1 (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
SU904861695A SU1738758A1 (en) 1990-08-22 1990-08-22 Ion-exchange method of cleaning sewage from nickel

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
SU904861695A SU1738758A1 (en) 1990-08-22 1990-08-22 Ion-exchange method of cleaning sewage from nickel

Publications (1)

Publication Number Publication Date
SU1738758A1 true SU1738758A1 (en) 1992-06-07

Family

ID=21533478

Family Applications (1)

Application Number Title Priority Date Filing Date
SU904861695A SU1738758A1 (en) 1990-08-22 1990-08-22 Ion-exchange method of cleaning sewage from nickel

Country Status (1)

Country Link
SU (1) SU1738758A1 (en)

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
RU2470877C1 (en) * 2011-06-16 2012-12-27 Государственное образовательное учреждение высшего профессионального образования Волгоградский государственный технический университет (ВолгГТУ) Method for ion-exchange purification of waste water from metal ions

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
Скворцов Н. Г. Колосова Г. М., Кумина Д. М. Ионообменна установка дл очистки промывных вод ванн никелировани . - Хими и технологи воды, 1989, 11, № 6, с. 536-538 *

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
RU2470877C1 (en) * 2011-06-16 2012-12-27 Государственное образовательное учреждение высшего профессионального образования Волгоградский государственный технический университет (ВолгГТУ) Method for ion-exchange purification of waste water from metal ions

Similar Documents

Publication Publication Date Title
US4519917A (en) Counter-current adsorption filters for the treatment of liquids and a method of operating the filter
EP0429183A1 (en) Regeneration of acidic cationic exchange resin used in the reactivation of spent alkanolamine
US4036751A (en) Method of treating water containing chromate
DD143212A5 (en) Method for removing ions from a waessress solution
CA2051016A1 (en) Nickel recovery process
Gregory et al. Wastewater treatment by ion exchange
SU1738758A1 (en) Ion-exchange method of cleaning sewage from nickel
US3580842A (en) Downflow ion exchange
US4049772A (en) Process for the recovery of chromic acid solution from waste water containing chromate ions
Calmon Recent developments in water treatment by ion exchange
US3803030A (en) Waste treatment
JP2004136231A (en) Method for washing ion-exchange resin after regeneration
RU2125105C1 (en) Method of nickel recovery from sheet solutions of electroplating
JP3913939B2 (en) Boron recovery method
US3607739A (en) Desalting and purifying water by continuous ion exchange
US4126548A (en) Ion exchange process
CN110643818B (en) Method for recovering nickel from electroplating wastewater
RU2049073C1 (en) Process for ion-exchange purification of sewage and industrial solutions from copper and nickel ions
JP4733807B2 (en) Method for purifying boron eluent and method for producing boron raw material
FI69444C (en) Release foer rening av vatten med laog fastmaterialhalt meelst jonbyte
JP4918197B2 (en) Method for recovering mineral acid from mixed acid of boric acid and mineral acid
Calmon et al. New directions in ion exchange
SU638549A1 (en) Method of purifying electrolytic production waste liquids
SU1608133A1 (en) Method of cleaning waste water from aliphatic amines
SU1386579A1 (en) Method and apparatus for regenerating ion exchange in countercurrent flow filter