WO1993004979A1

WO1993004979A1 - Acidity control in chlorine dioxide manufacture

Info

Publication number: WO1993004979A1
Application number: PCT/SE1991/000605
Authority: WO
Inventors: Rolf Carl August BRÄNNLAND; Sture Erik Olof NORÉUS
Original assignee: Eka Nobel Ab
Priority date: 1991-09-12
Filing date: 1991-09-12
Publication date: 1993-03-18

Abstract

The continuous generation of chlorine dioxide by reduction of sodium chlorate with sulphur dioxide, sodium chloride, methanol or some other suitable reductant requires acid reaction conditions. According to the invention, the acidity is maintained, completely or partially, with acid produced by the electrolysis of a solution of sodium sulphate (Na2SO4 or Na3H[SO4]2). This sulphate is obtained by crystallization and redissolution of sodium sulphate formed in the chlorine dioxide generating process. The electrolysis of the sodium sulphate is limited for reasons of efficiency, such that only a part of the sulphate is decomposed to acid, whereas the remainder is recycled together with the acid to the reactor, where chlorine dioxide is generated. Sodium hydroxide, oxygen gas and hydrogen gas are also formed during the process of electrolysis and are utilized within the pulp manufacturing process.

Description

Acidity control in chlorine dioxide manufacture

Technical field

The present invention relates to a method for technically producing chlorine dioxide intented for bleaching cellulose pulp produced, for instance, chemically, such as sulphate pulp or sulphite pulp, and involving a more effective use of the chemicals used by combining the manufacturing process with an electrolysis process for the purpose of controlling acidity in the generation of chlorine dioxide.

Background art Chlorine dioxide is manufactured on a technical scale, by reacting sodium chlorate in aqueous solution with a suitable reductant. Conventional reductants are sulphur dioxide, sodium chloride, hydrogen chloride and methanol, although other inorganic substances are also mentioned in the litera¬ ture, such as nitrogen dioxide and sulphur, or organic sub¬ stances such as ethanol and oxalic acid. Experience and scientific research have shown that the reduction of the chlorate shall be carried out in a strongly acid solution. Sulphuric acid or hydrochloric acid (hydrogen chloride) are the substances most commonly used to effect such acidifica¬ tion. Subsequent to the chlorate having been consumed, there remains a strongly acid solution of sulphuric acid and sodium sulphate, or hydrochloric acid and sodium chloride, so-called spent acid. Sulphur containing spent acid has hitherto been used as a make-up chemical in the pulp mills, wherein the acid has been utilized to cleave or split tall oil soap for the production of tall oil, and the sodium sulphate is used to make up alkali losses and sulphur losses in the cooking chemical system of the pulp mills. A modern variant of the chlorine dioxide process is based on reacting a mixture of sodium chloride and sodium chlorate in a solution which is acidified with sulphuric acid. The reaction takes place under vacuum conditions, 10-57 kPa, at a temperature of 45-85°C. A mixture of water vapour (steam), chlorine dioxide and chlorine departs during this reaction. The reaction is represented by the formula:

NaC10₃+NaCl+H₂S0₄ = C10₂+l/2 Cl₂+Na₂S0₄+H₂0

In view of present-day requirements on the limited use of chlorine and hypochlorlte in pulp bleaching processes, it is desirable to limit the amount of molecular chlorine formed.

This can be achieved by also using sulphur dioxide as a reductant, in accordance with the formula:

NaCl0d+l/2S0 A = C102.,+l/2Na2.-SO4_J,

Sulphur dioxide can also be used to absorb in an aqueous solution chlorine gas which has not dissolved in the water washing tower used to produce chlorine dioxide water. This results in a mixed acid according to the formula:

2HC1+H2-S04. This mixed acid can be returned to the chlorine dioxide reactor. Flows of sodium chlorate, sodium chloride and sulphuric acid are delivered to the reactor. The reaction products chlorine dioxide and chlorine are absorbed in a tower to which pure water is delivered and which produces a liquid which contains chlorine dioxide and chlorine. The residual gas from the absorption tower is passed to a reac¬ tion vessel, to which sulphur dioxide and water are supplied. The resultant mixed acid is passed back to the reactor. Crystals of sodium sulphate (Na_SO.) formed in the chlorine dioxide reactor are pumped to a filter and ejected, whereas the mother liquor is returned to the reactor.

According to one alternative embodiment, methanol is used as a reductant, which is supplied to the reactor along with sodium chlorate and sulphuric acid. The chlorine dioxide gas formed is passed to a tower in which the gas is absorbed in water, and the resultant bleaching liquid is passed to the bleaching department. Crystals of sodium sesquisulphate (Na₃H[SO.]₂) formed in the chlorine dioxide reactor are pumped to a filter and ejected, whereas the mother liquor is returned to the reactor. The following reaction formulas are representative of this embodiment:

6NaCl0₃+CH₃OH+4H₂S0₄ = 6C10₂+C0₂+2Na₃H(S0₄)₂+5H₂0 respectively

12NaCl0₃+3CH₃OH+8H₂S0₄ = 12ClO₂+3HCOOH+4Na₃H(SO₄)₂+9H₂0

Disclosure of the Invention

The technical problem in recent times, the chemical systems of pulp mills have been closed very effectively and the need for make- p chemi¬ cals has therewith decreased. At the same time, the use of chlorine dioxide has increased very considerably, in that chlorine has been replaced, inter alia, with chlorine dioxide to a great extent, for environmental reasons.

This has resulted in an imbalance which, in turn, has resulted in an excess of spent acid. The situation has been alleviated to some extent by the introduction of methods in which the sulphate formed, in some cases sesquisulphate (Na₃H[S0₄]₂) and in other cases neutral sulphate Na₂S0₄) has been removed from the generating liquid in the form of solid crystals. This enables a certain amount of acid to be saved and also limits loading the pulp mill with undesirable sulphur.

A further complication with this decrease in the consump¬ tion of chlorine consumption is that sodium hydroxide, which is formed in equivalent quantities with chlorine in the electrolysis of sodium chloride (table salt) has become scarce. It is therefore necessary to look for alternative methods of producing sodium hydroxide.

The solution The present invention solves these problems and relates to a method for generating chlorine dioxide, by reducing a chlorate solution in the presence of hydrogen ions at a pH- value below 7 with the use of one or more reductants and a sulphur-containing compound in the form of a reductant and/or an acid, characterized by maintaining the hydrogen ion con¬ centration (the acidity) in the chlorine dioxide generating process, completely or partially, with the aid of acid ob¬ tained by the electrolysis of a solution of sodium sulphate (Na₂S0₄ or Na₃H[S0₄]₂). produced by crystallization and redissolution of sodium sulphate formed during the chlorine dioxide generating process, the electrolysis being restricted so that part of the sodium sulphate is recycled to the chlorine dioxide generating process together with the acid formed. The crystals of sodium sulphate formed in the chlorine dioxide generating process are separated on a filter and re- dissolved and passed to the anode chamber and there subjected to electrolysis in, for instance, a membrane cell provided with a unipolar cation-selective membrane. Part of the sodium ions in the sodium sulphate solution is caused to pass the membrane and forms sodium hydroxide in the cathode chamber, this sodium hydroxide being removed from said chamber and used, preferably in the alkaline bleaching stage of the pulp mill. The remaining acid sulphate/sulphuric acid solution is tapped off. Part of this acid solution is removed from the system and used, for instance, for the production of tall oil in the sulphate mill, and its corresponding sodium content is used, for instance, to make-up alkali losses in the cooking chemical system of the mill.

The remainder of this acid solution is preferably sub¬ jected to evaporation, so as to maintain the water balance in the system. After the evaporation, the acid solution is re¬ turned to the chlorine dioxide generator and there used to control the acidity in the process.

In order to utilize the vapourized water, it is suitable to pass this water vapour to the crystal dissolving vessel, furthermore, the water can be vapourized at a pressure level such that the vapour formed can be used to heat the solution in the chlorine dioxide generator.

In order to further save chemicals, the mixed acid formed by reduction of chlorine gas with sulphur dioxide can be used to acidify the pulp prior to the first bleaching stage, in those instances when chlorine has been replaced to a great extent with chlorine dioxide and the initial acidity in the bleaching process is too low. The mixed acid used for this purpose can be replaced in the chlorine dioxide generating process with chlorine-free acid generated in the electrolysis cell. By adapting the outtake of sodium sulphate, acid and alkali in relation to the chlorine dioxide generation, tall oil cooking and chemical losses in the pulp mill, it is possible, in each individual case, to minimize the total amount of chemicals used and to control the acidity in the chlorine dioxide generating process in a satisfactory manner. Part of the acid required to control acidity can be taken from an external source, in order to further increase flexi¬ bility. Practical tests have been carried out with a simple mem¬ brane cell provided with an iron cathode, platinated titanium anode and a unipolar cation-selective membrane of perfluoro- sulphonic acid or perfluorocarboxyllc acid. i.e. the type that has long been used in the production of chlorine and alkali by electrolytic decomposition of sodium chloride. These tests have shown that the sodium sulphate obtained in crystal form in the chlorine dioxide generating process can be worked-up surprisingly easily. The salt is dissolved in pure water, such as to obtain a concentration of about 400 g/1 Na₂S0₄. this solution being delivered continuous¬ ly to the electrolysis plant.

In principle, it is possible to decompose completely the sodium sulphate to sulphuric acid and sodium hydroxide, although practical tests have shown that it is suitable to limit the degree of decomposition (the degree of conversion) to 40-80%. since the current yield falls with higher contents of acid and alkali in the anode and cathode chambers respec¬ tively. The hydrogen ion concentration of the liquid tapped from the anode chamber is then 2-5 val/1. For similar reasons, it is suitable to add water in an amount such as to limit the sodium hydroxide concentration to 100-200 g/1 NaOH.

According to one preferred embodiment cf the invention, the electrolysis vessel is divided by means of a membrane into a chamber for the cathode and a chamber for the anode. Sodium sulphate solution is supplied through a conduit and converted solution containing sulphuric acid, possibly with residual non-converted sodium sulphate, is removed through another conduit. Oxygen gas is generated at the anode. Sodium ions diffuse through the cation-selective membrane, where they form sodium hydroxide at the cathode and hydrogen gas is generated at the same time. Pure water is delivered through a conduit and the sodium hydroxide formed is removed through another conduit. It is also possible to use other types of electrolysis cells, although the effectiveness of these cells is somewhat lower.

Advantages

The invention has enabled the consumption of acid and alkali in a pulp mill to be reduced considerably, by com- bining acid and alkali consuming processes with an electro¬ lytic process, wherein salts which are formed in the chlorine dioxide generating process are decomposed to their individual consituents and reused. At the same time, the biproducts oxygen gas and hydrogen gas are obtained, which can be utilized in the pulp manufacturing process for bleaching and for steam generation respectively.

Furthermore, the invention enables the quotient between acid requirements in the production of tall oil and the sulphate requirements for making-up losses in the cooking chemical cycle to be varied in accordance with the local con¬ ditions. Also of great value are the chemicals sodium hydroxide, oxygen gas and hydrogen gas formed in accordance with the invention and utilized within the pulp manufacturing process. This reuse of chemicals improves the economy of pulp manufacture and also reduces the load on the environment caused by the emission of non-consumed chemicals. Brief description of the drawings

Figure 1 is a flow sheet pertaining to a preferred embodiment of the invention. Figure 2 illustrates the con¬ struction of a suitable electrolysis cell in more detail.

Best mode of carrying out the invention

In the following, preferred embodiments of the invention are described with reference to the Figures, and an account of the results achieved in accordance with the invention is also given.

Example 1

Tests were carried out in accordance with the invention

- with the use of a chlorine dioxide generating plant which, in principle, operated in accordance with Figure 1 with the use of sodium chloride as a reductant for the chlorate in the reactor 1 and with sulphur dioxide as the reductant in the absorption tower 3.

The reactor 1 was operated under the following conditions:

Temperature 70°C

Pressure 30.7 kPa Acidity 4.4 val/1

Amount of chlorate supplied (4) 1300 kg/h (NaClOg)

Amount of chloride supplied (5) 585 kg/h (NaCl) Amount of chlorine dioxide produced(9) 800 kg/h CIC Amount of chlorine produced 361 kg/h (Cl ) Crystal concentration

(Na₂S0₄-crystals) 10%

Amount of crystals removed 2141 kg/h (Na„S0 )

Amount of steam supplied 6500 kg/h The generated mixture of chlorine dioxide and chlorine gas was transported to the absorption tower 2 with the aid of

3 steam, where 100 m /h cooled water (10°C) was delivered through the line 8. Practically all chlorine dioxide was dissolved in this water, although only 168 kg/h chlorine gas dissolved, and the water was pumped to the bleaching depart¬ ment of the mill, through the line 9. Remaining chlorine gas, 193 kg/h, was passed further to the reactor 3, where the chlorine gas was reacted with 170 kg/h sulphur dioxide supp- lied through the line 7, and 1100 1/h water supplied through the line 11. Of the mixed acid formed, 720 1/h were returned to the reactor 1 through the line 12, whereas 380 1/h was passed to acidification of unbleached pulp upstream of the first bleaching stage, through the line 13, The residual gas was removed through the line 10.

2141 kg/h crystals of sodium sulphate were taken out of the circulation circuit 16 over a filter 14 and were dissolv¬ ed in 5352 1/h water in the vessel 23, this water being de¬ livered mainly from the evaporator 29, through the line .28. The solution obtained was delivered to the electrolysis plant 27 which was operated so that 75% of the sulphate was con¬ verted to sulphuric acid and sodium hydroxide and the sulphuric acid being obtained in mixture with the sodium sulphate in the anode chamber and tapped-off through the line 24. The composition of the acid solution was then:

Na₂S0₄ 79 g per kg solution H₂S0₄ 163 g per kg solution

Pure water was supplied to the cathode chamber through the line 25. and 9000 1/h sodium hydroxide having a 10%-con- centration, corresponding to 904 kg/h NaOH, was tapped-off

3 through the line 26. In addition, 127 /h oxygen gas (181

3 kg/h) were generated in the anode chamber, and 253 m /h hydrogen gas (22.6 kg/h) were generated in the cathode chamber. The acid solution was pumped through the line 24 to the evaporation vessel 29, which was operated under vacuum condi¬ tions, 50 kPa and 82°C. 4614 kg/h water were evaporated and passed to the dissolving tank 23. The concentrated acid now had the composition:

Na₂S0. 225 g per kg solution H-SO. 465 g per kg solution

Of this solution, 5% was passed to the tall oil cooking department of the sulphate mill through the line 30, for de- composition of tall oil soap, and 95% to the chlorine dioxide generator, through the line 31.

As a result of this recirculation of acid, it was possib¬ le to maintain the acidity in the generation of chlorine dioxide, without needing to supply acid from an external source. The following savings were made possible in this example:

Sulphuric acid 1108 kg/h

Sodium hydroxide 904 kg/h

Oxygen gas 181 kg/h Hydrogen gas (fuel) 22.6 kg/h

Sodium sulphate 24 kg/h

The power consumed by the electrolysis process was 3460

2 kW at a current density of 30A/dm . 70°C and the recited concentrations of acid and alkali.

Example 2

According to another embodiment of the invention, sodium chloride was similarly used as the reductant for the chlorate in the reactor 1 and sulphur dioxide as the reductant in the absorption tower 3. although with the difference in relation to Example 1 that no solution was returned to the reactor 1 from the absorption tower 3. The reactor 1 worked under the following conditions:

Temperature 70°C

Pressure 30.7 kPa

Acidity 4.2 val/1 Amount of chlorate supplied (4) 1300 kg/h (NaClOg)

Amount of chloride supplied (5) 702 kg/h (NaCl) Amount of chlorine dioxide produced (9) 800 kg/h (C10₂)

Amount of chlorine produced 432 kg/h (C1-) Crystal concentration

(Na₂S0₄-crystals) 9%

Amount of crystals removed 3436 kg/h (Na^SO.)

Amount of steam delivered 7000 kg/h

The generated mixture of chlorine dioxide and chlorine gas was transported to the absorption tower 2 with the aid of

3 steam, where 90 m /h cooled water (10^βC) were supplied through the line 8. Practically all chlorine dioxide dis¬ solved in this water, but only 170 kg/h chlorine gas, and the water was pumped to the bleaching department of the mill, through the line 9. Remaining chlorine gas, 262 kg/h, was passed further to the reactor 3, where it was reacted with 236 kg/h sulphur dioxide supplied through the line 7 and 1500 1/h water supplied through the line 11. Of the mixed acid formed, 500 1/h were used to acidify unbleached pulp upstream of the first bleaching stage and were removed through the line 13, while the remainder was passed to a discharge outlet subsequent to neutralization with dust from the lime kiln filter.

3436 kg/h crystals of sodium sulphate were removed from the circulation circuit 16 over a filter 14 and dissolved in 8590 1/h water in the vessel 23, the majority of this water being delivered from the evaporator 29, through the line 28. The resultant solution was delivered to the electrolysis plant 27, which was operated so that 50% of the sulphate was converted to sulphuric acid and sodium hydroxide, of which the sulphuric acid was obtained in mixture with the sodium sulphate in the anode chamber and tapped-off through the line 24. The composition of the acid solution was then:

a₂S0₄ 152 g per kg solution H-SO. 105 g per kg solution

Pure water was delivered to the cathode chamber through the line 25. and 9600 kg/h sodium hydroxide having a concen¬ tration of 10%. corresponding to 968 kg/h NaOH were tapped-

3 off through the line 26. In addition, 135 m /h oxygen gas

(194 kg/h) were generated in the anode chamber, and 271 m /h hydrogen gas (24.2 kg/h) were generated in the cathode chambe .

The acid solution was pumped through the line 24 to the evaporation vessel 29, which was operated under vacuum condi¬ tions, 50 kPa and 82°C. 7071 kg/h water were evaporated and delivered to the dissolving tank 23. The concentrated acid now had the composition:

Na₂S0₄ 399 g per kg solution H₂S0₄ 275 g per kg solution

This solution was returned to the chlorine dioxide gene- rator through the line 31. This recycling of acid enabled the acidity of the chlorine dioxide generating process to be maintained without needing to supply acid from an external source. The example enabled the following savings to be made: Sulphuric acid 1186 kg/h Sodium hydroxide 968 kg/h

Oxygen gas 194 kg/h

Hydrogen gas (fuel) 24.2 kg/h The power consumed by the electrolysis process was 2880

2 kW aatt aa ccuurrrreenntt ddeennssiittyy ooff 3300 AA//dm , 70°C, and the recited concentrations of acid and alkali.

Example 3

According to a third embodiment of the invention, methanol was used as the reductant for the sodium chlorate in the aforesaid reactor 1, which operated under the following conditions:

Temperature 70°C

Pressure 30.7 kPa

Acidity 6.1 val/1

Amount of chlorate supplied (4) 1300 kg/h (NaC10₃)

Amount of methanol supplied (17) 98 kg/h (CH₃OH)

Amount of chlorine dioxide produced (9) 800 kg/h (C10₂) Crystal concentration

(Na₃H[S0₄]₂-crystals) 10% Amount of crystals removed 2133 kg/h (Na₃H[S0₄]₂) Amount of steam supplied 6000 kg/h

Similar to Example 1, the chlorine dioxide gas was tran¬ sported by steam to the absorption tower 2, although since the gas was practically free from chlorine, no reaction stage with SO_?-reduction was required and no mixed acid was pro¬ duced in this case.

2133 kg/h crystals were removed from the circulation cir¬ cuit 16 over a filter 14 and dissolved in the vessel 23 in 4335 1/h water, which was supplied mainly from the evaporator 29. The resultant solution was delivered to the electrolysis plant 27, which was operated so that 50% of the sodium con¬ tent of the sulphate was converted to sodium hydroxide. This was formed in the cathode chamber while adding 4800 1/h water and tapped-off at a concentration of 10% through the line 26, corresponding to an amount of 488 kg/h NaOH. In addition, 136

3 m /h hydrogen gas (12.2 kg/h) were generated in the cathode

3 chamber, and 68 m oxygen gas (98 kg/h) were generated in the anode chamber.

The composition of the acid solution after electrolysis was:

Na₂S0₄ 143 g per kg solution ^H2^S04 ^{164 g per kg} solution

This solution was pumped through the line 24 to the eva¬ poration vessel 29, which was operated under vacuum condi¬ tions, 50 Pa and 82°C. 3348 kg/h water were evaporated and delivered to the dissolving tank 23. The concentrated acid had the composition:

Na₂S0₄ 321 g per kg solution H₂SO 369 g per kg solution

This acid was supplied to the reactor 1 through the line 31. This recirculation of acid enabled the acidity to be maintained in the chlorine dioxide generating process without supplying acid from an external source. Acid from an external source, however, can be supplied through the line 6 if con¬ sidered suitable. The example has enabled the following savings to be made:

Sulphuric acid 598 kg/h

Sodium hydroxide 488 kg/h

Oxygen gas 98 kg/h

Hydrogen gas (fuel) 12.2 kg/h The electrolysis had a power consumption of 1650 kW at

2 the current density of 30 A/dm , 70°C, and the recited acid and alkali concentrations.

The invention is not limited to the cases described in Examples 1-3, but can also include chlorine dioxide generat¬ ing processes which are based on reductants other than those mentioned here, or on combinations of generating processes, for instance reduction with sulphur dioxide in a first stage followed by a second stage with chloride reduction, where- after sodium sulphate crystallizes out.

Figure 2 illustrates a preferred embodiment of the elec¬ trolysis cell 27, which is provided with an iron cathode 18, a platinated titanium electrode 19 and a unipolar cation selective membrane 20. Hydrogen gas 21 is generated at the cathode and oxygen gas 22 is generated at the anode. A solu¬ tion of sodium sulphate is delivered to the anode chamber through the line 23, and the acid formed is removed through the line 24. Pure water is supplied to the cathode chamber through the line 25, and the sodium hydroxide formed is re- moved through the line 26.

According to the invention, the chemical requirements of the sulphate mill can be covered by taking out flows from different points in the system, either separately or in com¬ bination. A crystal mass of sodium sulphate can be taken out through the line 15 in order to cover the sodium and sulphur requirement of the pulp mill. An acid, highly concentrated solution of sulphuric acid and sodium sulphate can be taken out through the line 30 for the production of tall oil. A dilute solution of corresponding composition appropriate in those instances when the evaporation capacity is found avail¬ able in another location in the mill can be taken out through the line 32.

Claims

1. A method for generating chlorine dioxide by reduction of a chlorate solution in the presence of hydrogen ions at a pH- value below 7, while using one or more reductants and a sulphur-containing compound in the form of a reductant and/or an acid, c h a r a c t e r i z e d by maintaining the hydro¬ gen ion concentration (the acidity) in the generation of chlorine dioxide, completely or partially, with the aid of acid obtained by the electrolysis of a solution of sodium sulphate (Na₂S0₄ or Na₃H[S0₄]₂) produced by crystallization and redissolution of sodium sulphate formed in the chlorine dioxide generation process, the electrolysis being restricted so that part of the sodium sulphate is recycled to the chlorine dioxide generating process together with the acid formed.

2. A method according to Claim 1, c h a r a c t e r i z e d by limiting the electrolytic decomposition of the sodium sulphate so that the hydrogen ion concentration in the solu¬ tion departing from the electrolysis cell is at most 5 val/1, preferably 2-4 val/1.

3. A method according to Claim 1 and 2, c h a r a c t e r i z e d by carrying out the electrolysis in a cell provided with a cation-selective membrane, wherein the sodium sulphate solution is supplied to the anode chamber, and wherein acid is formed and oxygen gas developed at the anode and hydrogen gas at the cathode, while supplying, at the same time, pure water to the cathode chamber so as there to form sodium hydroxide.

4. A method according to Claims 1-3, c h a r a c t e r i z e d by returning the acid solution formed in the anode chamber to the chlorine dioxide genera¬ tor, the water supplied by dissolution of the sodium sulphate being removed by evaporation of the water either from the acid solution or from the salt solution of the chlorine di¬ oxide generator, or from both of said solutions.

5. A method according to Claims 1-3, c h a r a c t e r i z e d by removing from the system an amount of sulphate corresponding to the amount of sulphur supplied to the system, this amount of sulphate comprising alternatively sodium sulphate removed prior to the electro¬ lysis stage, or acid sodium sulphate after the electrolysis stage.