WO1996027046A1

WO1996027046A1 - Method and apparatus for making paper pulp using basic processing effluents from a hydrogen peroxide production plant

Info

Publication number: WO1996027046A1
Application number: PCT/FR1996/000302
Authority: WO
Inventors: Henry Ledon
Original assignee: Chemoxal S.A.
Priority date: 1995-02-28
Filing date: 1996-02-27
Publication date: 1996-09-06
Also published as: FR2731021B1; FR2731021A1

Abstract

A plant for making paper pulp and particularly chemical pulp, including at least one impregnation station (25) for impregnating a material produced by crushing wood, a cooking station (20), and a paper pulp bleaching station (28), each of said stations being supplied with a basic processing solution from a source. Said basic solution source (24) is the outlet for a basic processing effluent from the working solution of a plant (I) for producing hydrogen peroxide in situ in a paper pulp manufacturing plant (II).

Description

Process and installation for the production of pulp using the basic treatment effluents of a hydrogen peroxide production installation.

The present invention relates to installations for manufacturing pulp and relates more particularly to such installations using as bleaching agent hydrogen peroxide produced by an installation on the site of the installation for manufacturing pulp paper.

Installations for the production of oxygen peroxide generally use a process comprising the following steps: a) reduction in a hydrogenator of an organic solution of an anthraquinone derivative, with hydrogen, in the presence of a catalyst; b) oxidation after filtration of the catalyst, of the reduced solution with a gas or a mixture of gases containing oxygen; c) treatment of the solution with water to extract the hydrogen peroxide formed; d) recycling to the hydrogenator of the organic solution extracted with water, after treatment in whole or in part, with a basic aqueous solution.

In conventional hydrogen peroxide production installations, the basic solution used for the treatment retains a substantial basicity and must therefore be neutralized in order to be able to be rejected while it could still be used in an industrial operation which would be implemented. at the site of the hydrogen peroxide production facility.

Furthermore, the neutralization treatment which requires additional operations does not, however, allow the effluents to be free from any danger to the environment.

In a paper manufacturing plant, basic solutions are used at many points in the pulp processing process. The invention therefore aims to remedy the drawbacks caused by the discharge of effluents from an installation for producing hydrogen peroxide.

It therefore relates to a process for manufacturing paper pulp, comprising treatment phases using a basic solution, characterized in that the basic solution consists of the effluent from the basic treatment of the solution. of work used in a process for the production of hydrogen peroxide implemented on the site of the manufacture of paper pulp.

The invention also relates to an installation for manufacturing paper pulp, in particular chemical pulp intended for the implementation of the process defined above and comprising at least one station for impregnating the material resulting from grinding. wood, a cooking station, and a station for bleaching paper pulp, these stations being each supplied by a source of basic treatment solution, characterized in that the source of basic solution is the outlet of the effluent from the basic treatment of the working solution of a hydrogen peroxide production installation on the site of the pulp manufacturing installation.

The invention will be better understood on reading the description which follows, given solely by way of example and made with reference to the appended drawing, in which:

The single figure is a schematic view of an installation for producing hydrogen peroxide associated with an installation for manufacturing paper pulp on a common site according to the invention.

The installation shown in the figure includes installed on the same site, an installation I for the production of hydrogen peroxide and an installation II for the production of paper pulp. Installation I for the production of hydrogen peroxide comprises three main devices in the form of columns: a catalytic hydrogenator 1, a counter-current oxidizer 2, and a water extractor 3. It also includes numerous associated equipment. to these three devices, only some of which have been shown: a booster-condenser assembly 4 for recirculating the gaseous mixture containing hydrogen, associated with the ydrogé¬ nator, a filter 6, a pump 7, a heat exchanger 8, a water cooler 9, an overhead condenser 10 and an air compressor 11 associated with the oxidizer, a pipe 12, as short as possible, connecting the base of the oxidizer 2 to that of the extractor 3 and a coalescer 14 and a pump 15 for recycling the working solution. FIG. 1 also shows a line 16 for supplying the hydrogenator with make-up hydrogen, a line 17 for supplying air to the compressor 11, a line 18 for supplying the ex¬ tractor 3 in demineralized water, a pipe 19 for the production of hydrogen peroxide, which leaves from the base of the extractor 3 and ends at the installation II for the production of paper pulp consuming hydrogen peroxide at the same concentration , and a pipe 21 for recycling the working solution. Installation II is located on the same site as installation I for the production of hydrogen peroxide.

The installation for producing hydrogen peroxide further comprises a device 22 for treating a fraction of the working solution with a basic solution, placed on a branch 23 of the recycling loop for the working solution, for example immediately downstream of coalescer 14.

The treatment device 22 is intended to remove from the portion derived from the working solution of the compounds coming from degradation, essentially by oxidation, solvents and anthraquinone derivatives to maintain the acidity of the working solution at an appropriate level.

In the present example, the treatment device 22 is supplied with a sodium hydroxide solution which, after treatment of the portion derived from the working solution, leaves the installation via a pipe 24 for supplying the installation with basic solution. II for the production of paper pulp. Installation II very schematically shown is a Kraft type chemical pulp installation.

It includes among others, a station 25 for impregnating the products resulting from slicing or sawing or crushing wood, a cooking station 26, a delignification station 27 and a station for bleaching the pulp to which it is connected. the pipe 19 for supplying hydrogen peroxide from the installation I. As is well known in the art, the treatment stations 25 are each supplied by a source of basic treatment solution.

According to the invention, the source of basic solution for the treatment stations 25 to 28 of the installation II for manufacturing paper pulp is constituted by the outlet of the device 22 for treatment with basic solution of the solution of work of the installation I of peroxide production.

This output is constituted by the line 24 connected to the stations 25 to 28 by branches 29.30, - 31.32 respectively.

In the bleaching station 28, several successive bleaching processes use the action of sodium hydroxide on the paper pulp in known manner. However, bleach station 28 has been shown in the drawing as comprising only one line 31 for supplying basic solution.

In operation, the working solution, consisting of at least one anthraquinone derivative and at least one organic solvent, is introduced at the base of the hydrogenator 1 via the recycling line 21 connected to the discharge of the pump 15, and a stream of hydrogen-containing gas is also introduced at the base of the hydrogenator. This gas stream consists on the one hand of the gas stream drawn off at the top of the hydrogenator, recirculated by the booster-condenser assembly 4, and on the other hand, of additional hydrogen arriving via line 16.

The anthraquinone derivative constituting the working solution is preferably chosen from the 2 alkyl 9.10 anthraquinones in which the alkyl substituent comprises from 1 to 5 carbon atoms, such as the ethyl, ethyl, sec-butyl, tert-butyl radicals , tertio-a yl, iso-amyl, as well as the corresponding tetrahydro-5,6,7,8 derivatives, or among the dialkyl 9,10 anthra¬ quinones in which the alkyl substituents, identical or different, comprise from 1 with 5 carbon atoms, such as methyl, ethyl, tert-butyl radicals, for example 1.3 dimethyl, 1.4 dimethyl, 2.3 dimethyl, 2.7 dimethyl, 1.3 diethyl, 2.7 ditertio-butyl, 2 ethyl 6 tert-butyl and the corresponding tetrahydro-5,6,7,8 derivatives. The organic solvent constituting the working solution is preferably a mixture of a non-polar compound and a polar compound. The non-polar compound is preferably chosen from petroleum fractions with a boiling point above 140 ° C. containing predominantly aromatic hydrocarbons containing at least 9 carbon atoms, such as the isomers of trimethylbenzene, the isomers of tetramethylbenzene , tert-butylbenzene, isomers of methylnaphthalene, isomers of diethylnaphthalene. The polar compound is preferably chosen from saturated alcohols preferably containing from 7 to 11 carbon atoms, such as diisobutylcarbinol, trimethyl-3,5,5 hexanol, isoheptanol, acid esters carboxylic acids such as cyclohexyl methyl acetate sold under the name of "Sextate", heptyl acetate, butyl benzoate, ethyl heptanoate, esters of phosphoric acid such as tributyl phosphate , tri (2 ethyl butyl) phosphate, tri phosphate (2 ethyl hexyl), tri (n-octyl) phosphate, tetrasubstituted ureas such as tetra (n-butyl urea).

The working solution is thus partially reduced. The reduced solution, drawn off from the base of the hydrogenator by the pump 7 via the filter 6, therefore contains hydroquinone derivatives (for example 80% tetrahydroanthrahydroquinone and 20% anthrahydroquinone). The quantity of hydrogen peroxide, expressed in grams, that a liter of working solution is capable of supplying at the end of the oxidation step if the rendering of this step in 1Oxider 2 is 100% , is designated by "hydrogen peroxide equivalent". This potential mass concentration of peroxide corresponds to a molar concentration which is equal to the molar concentration of all the reoxidizable anthrahydroquinone forms in the working solution.

In the present case, the hydrogenation is carried out at a temperature between 50 and 70 ° C., with a pressure in the gaseous sky of the hydrogenator (pressure which regulates the flow of hydrogen) from 0.8 to 1.5 approximately bar, and the hydrogen peroxide equivalent is adjusted to a value between approximately 7 and 9 g / l, by adjusting the residence time in the hydrogenator, for a given concentration of anthraquinone forms. The reduced working solution withdrawn from the hydrogenator is filtered at 6 to remove all traces of catalyst, then cooled at 8 and then at 9 to a temperature of the order of 35 to 40 °. The pressure of the gaseous overhead of the oxidizer is maintained at a value between 2 and 4 bars. The reduced working solution is thus oxidized in 2, the head fluid of the oxidizer being partially condensed in 10.

The hydrogen peroxide formed by the oxidation reaction is withdrawn from the base of the oxidizer, in an amount equal to the product of the hydrogen peroxide equivalent mentioned above by the yield of the oxidizer, mixed with the working solution. oxidized again. This liquid is sent directly via line 12, thanks to the difference in driving pressure, to the base of the extractor 3, which operates a little above atmospheric pressure. In the extractor is carried out a liquid-liquid extraction by means of demineralized water introduced at the top of the extractor. A water-hydrogen peroxide solution is drawn from the base of the latter, the hydrogen peroxide concentration is adjusted to the value necessary for its direct use in installation II for making paper pulp. The hydrogen peroxide concentration is chosen to be less than 15% by weight, for example between 5 to 12% by weight.

The working solution separated from the hydrogen peroxide is drawn off from the top of the extractor 3, freed from the droplets of aqueous phase which it has entrained in the coalescer 14, then sent by the pump 15 to the heat exchanger 8, in which it heats up, and from there is recycled to the base of the hydrogenator 1.

The degraded compounds contained in the working solution circulating in the recycling line which are essentially formed by oxidation of solvents and anthraquinone derivatives must be eliminated from the working solution because they increase the acidity of the organic phase and modify the surface tension of the liquid, which is likely to create problems on the stage of extraction, and reduce both the activity and the selectivity of the hydrogenation catalyst.

A fraction of the working solution is therefore derived from the main stream at the outlet of the coalescer 14 and treated using the sodium hydroxide solution in the treatment device 22, to maintain the acidity of the working solution below of a reasonable level.

Then, the organic phase is washed with an aqueous solution of mineral acid, then carefully with water in equipment not shown before being recycled.

The basic solution from the treatment device 22 is sent via line 24 to the installation II for manufacturing paper pulp and distributed in the branches 29 to 32 to be introduced into successive stations 25 to 28, for impregnation , cooking, delignification and blanching.

In the paper pulp cooking operation carried out at cooking station 26, the soda solution from the hydrogen peroxide production installation is used in the form of a mixture of soda and sodium sulfide received by a pipe 34.

In the delignification step, the abovementioned basic treatment effluent is used at the delignification station 27 as a source of alkali using oxygen received via a pipe 35.

In the bleaching station, the basic treatment effluent is used as an alkali source, in a step "E" of alkaline extraction or in a step "Eo" of alkaline extraction reinforced with oxygen from paper pulp.

Still in the bleaching station, the effluent of the basic treatment of the working solution of the hydrogen peroxide production installation is mixed with part of the aqueous hydrogen peroxide solution.

A hydrogen peroxide stabilizer is added to the basic solution of hydrogen peroxide. This stabilizing agent is chosen from carboxylic, aminomethylenecarboxylic, phosphonic and aminomethylenephosphonic compounds.

In particular, this stabilizing agent is chosen from ethylenediamine tetraacetic acid ("EDTA") or its salts, diethylenetriaminepentaacetic acid ("DTPA") or its salts, polyacrylic acids, ethylenediaminetetramethylenephosphonic acid or its salts, diethylenetriaminepentamethylenephosphonic acid or its salts, 1,2-diamino acid NNN'N 'tetramethylenephosphonic acid or its salts, hydroxyethylbismethylenephosphonic acid or its salts.

The basic solution of hydrogen peroxide can also be used in a reinforced alkaline extraction stage with oxygen and with hydrogen peroxide "Eop". The basic solution of hydrogen peroxide can also be used in a bleaching stage of the paper pulp, leads to a temperature above 100 ° C. and to a pressure above atmospheric pressure, in the presence of a gas. or a mixture of gases containing oxygen.

The basic solution used corresponds to the basic solution for treating the working solution of the installation for the production of hydrogen peroxide. It can be a sodium hydroxide solution at a concentration of between 0.01 and 10 M and preferably between 1 and 3 M.

It should also be mentioned that the basic solution is not necessarily the only source of alkali but can be used in addition to another source of alkali.

Thanks to the arrangement which has just been described, advantage is taken in the pulp production installation of the basic solution source that constitutes the basic effluents of the installation for producing hydrogen peroxide located on the site of the pulp manufacturing facility, while in an independent hydrogen peroxide production facility, these basic effluents could not be used and should therefore be rejected.

Claims

1. A method of manufacturing paper pulp, comprising treatment phases using a basic solution, characterized in that the basic solution consists of the basic treatment effluent of the working solution used in a process for the production of hydrogen peroxide implemented on the site of the manufacture of paper pulp.

2. Method according to claim 1, comprising a phase of cooking Kraft type chemical pulp, characterized in that the residual basic solution from the treatment of the working solution used in the process for producing hydrogen peroxide is a soda solution which is mixed with sodium sulfide.

3. Method according to one of claims 1 and

2, comprising a delignification step using oxygen and in which the basic treatment effluent is used as a source of alkali.

4. Method according to one of claims 1 to

3, comprising a bleaching phase of the paper pulp in which the effluent from the basic treatment is used in an alkaline extraction step "E" or an oxygen-reinforced alkaline extraction step "Eo" from the pulp paper.

5. The method of claim 4, wherein the effluent from the basic treatment is mixed with part of the aqueous solution of hydrogen peroxide produced at the site of the manufacture of the pulp.

6. The method of claim 5, wherein a stabilizing agent of hydrogen peroxide is added to the basic solution of hydrogen peroxide.

7. The method of claim 6, wherein the hydrogen peroxide stabilizing agent is chosen from carboxylic, aminomethylene-carboxylic, phosphonic, aminomethylene-phosphonic compounds.

8. The method of claim 7, wherein the stabilizing agent of hydrogen peroxide is selected from ethylenediamine tetraacetic acid ("EDTA") or its salts, diethylenetriaminepentaacetic acid ("DTPA") or its salts, polyacrylic acids, ethylenediaminetetramethylenephosphonic acid or its salts, acidediethylenetriaminepentamethylenephosphonic acid or its salts, diamino-1,2 NNN'N 'tetramethylene-phosphonic acid or its salts, hydroxyethylbismethylenophosphonic acid or its salts .

9. Method according to one of claims 5 to 8, in which the basic solution of hydrogen peroxide is used in an alkaline extraction stage reinforced with oxygen and with hydrogen peroxide "Eop".

10. Method according to one of claims 4 to 9, wherein the pulp bleaching stage is carried out at a temperature above 100 ° C and at a pressure above atmospheric pressure, in the presence of a gas or d 'a mixture of gases containing oxygen.

11. Method according to one of claims 1 and 3 to 10, wherein the base used in the basic solution for treating the working solution of the process for producing hydrogen peroxide is sodium hydroxide.

12. The method of claim 11, wherein the concentration of sodium hydroxide is between 0.01 and 10 M and preferably between 1 and 3 M.

13. Installation for manufacturing paper pulp, in particular chemical pulp intended for the implementation of the method according to any one of claims 1 to 12 and ^t comprenan _{AT LEAST} s station _₍₂₅₎ impregnation of the material resulting from the grinding timber, a station (26) for cooking, and a station (28) for paper pulp bleaching, these stations being each fed by a source of basic treatment solution, characterized in that the source of basic solution is the outlet (24) of the effluent from the basic treatment of the working solution of an installation (I) production of hydrogen peroxide on the site of the plant (II) for manufacturing paper pulp.

14. Installation according to claim 13, further comprising a delignification station (27) and in which the source of basic solution (24) is connected to the delignification station (27) to which is also connected an oxygen source.