CA1222156A - Reactor to perform chemical reactions with dimensional reduction of solid materials - Google Patents
Reactor to perform chemical reactions with dimensional reduction of solid materialsInfo
- Publication number
- CA1222156A CA1222156A CA000429614A CA429614A CA1222156A CA 1222156 A CA1222156 A CA 1222156A CA 000429614 A CA000429614 A CA 000429614A CA 429614 A CA429614 A CA 429614A CA 1222156 A CA1222156 A CA 1222156A
- Authority
- CA
- Canada
- Prior art keywords
- reactor vessel
- reactor
- disintegrating
- rotor
- pulp material
- Prior art date
- Legal status (The legal status 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 status listed.)
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Abstract
ABSTRACT OF THE DISCLOSURE
The present invention provides a reactor adapted to simultaneously accomplish chemical reactions and operations of size reduction of the solid materials in suspension and parti-cularly for treatment in the cellulose and/or paper pulp in-dustry. The reactor provides an essentially closed working environment and is provided in the lower part with a rotor which creates turbulence with flows over essentially the whole volume of the closed environment and is adapted to realize said condi-tions of the size reduction of solid materials with intimate mixing of same with the suspending liquid.
The present invention provides a reactor adapted to simultaneously accomplish chemical reactions and operations of size reduction of the solid materials in suspension and parti-cularly for treatment in the cellulose and/or paper pulp in-dustry. The reactor provides an essentially closed working environment and is provided in the lower part with a rotor which creates turbulence with flows over essentially the whole volume of the closed environment and is adapted to realize said condi-tions of the size reduction of solid materials with intimate mixing of same with the suspending liquid.
Description
~2221~6 The present invention relates to a reactor which per-mits simultaneous chemical reactions and operations of size reduction of the solid materials in suspension. Particularly, the invention relates to a reactor suited for the mentioned operations and named "TURBOPULPER" adapted particularly for treatment in the cellulose and/or paper pulp industries. This reactor has an axial admission rotor with a radial delivery such as to create turbulence inside the reactor. This reactor is preferably adapted to operate under pressure and has a sperical shape and may be heated.
The present invention relates to a reactor for effecting chemical reactions simultaneously with operations of size reduction of solid materials in suspension. Such a reactor is particularly usable, but not exclusively, for example in the alkali-oxygen process for delignification.
As known, generally the chemical reactions are acti-vated by a good mixing and by adequate temperatures. The re-action is still more active when conditions are created for a good "exchange of materials". Amongst these last conditions, there is the maximum possible exchange surface and interchange of the substances which must react along this surface. The general conditions summarized above are particularly difficult to attain in cases when the solid materials in suspension, for the reaction, are at high consistency in water or other liquid vehicles.
Particularly, these conditions must be reached in two separate apparatuses operating in the pulp industry and called pulper and digester. The apparatus of this lnvention provides for both these operations previously carried out in this industry by the aforesaid separate apparatuses. These appara-tuses generally are not capable in the conditions to completely satisfy all the requirements of the particular applications and "` ~ZZZ156 to have at the same time the necessary flexibility to reach the optimum or nearest to optimum working conditions with treated materials of different characteristics.
Therefore the present invention provides a reactor for the aforesaid uses, permitting, under the aforesaid condi-tions, activation and speeding up of the chemical reactions, assuring that their effec~ is distributed extremely homoge-neously throughout the reaction mass.
Particularly, the present invention provides a reac-tor, which simultaneously has the following advantages: (a)capability to reduce the size of the particles of the solids in suspension to the desired level; (b) homogeneous distribu-tion of chemical throughout the mass, simultaneously with the size reduction of the solid materials in suspension; (c) com-plete recycling of the contents of the reactor inside its spherical interior so that the material passes at every cycle at least one lnlet zone of the chemicals fed in continuously;
and (d) possibility of indirect heating i.e. the heating medium is not mixed with the suspension to be heated, and without the well known inconveniences deriving from the forma-tion of deposits of the suspended materials on the hot surface and thus maintaining a high constant coefficient of heat exchange independently from the type of suspension.
According to the present invention there is provided an apparatus for reacting a solution of cellulosic pulp mate-rial under intimate and turbulent contact with a chemical com-position while simultaneously subjecting the pulp material to a disintegrating treatment, said apparatus comprising: a) a stationary pressure-sealed substantially spherical reactor vessel in which the pulp~material is received and treated under conditions of elevated pressure and temperature, said reactor vessel having a top portion and a bottom portion for
The present invention relates to a reactor for effecting chemical reactions simultaneously with operations of size reduction of solid materials in suspension. Such a reactor is particularly usable, but not exclusively, for example in the alkali-oxygen process for delignification.
As known, generally the chemical reactions are acti-vated by a good mixing and by adequate temperatures. The re-action is still more active when conditions are created for a good "exchange of materials". Amongst these last conditions, there is the maximum possible exchange surface and interchange of the substances which must react along this surface. The general conditions summarized above are particularly difficult to attain in cases when the solid materials in suspension, for the reaction, are at high consistency in water or other liquid vehicles.
Particularly, these conditions must be reached in two separate apparatuses operating in the pulp industry and called pulper and digester. The apparatus of this lnvention provides for both these operations previously carried out in this industry by the aforesaid separate apparatuses. These appara-tuses generally are not capable in the conditions to completely satisfy all the requirements of the particular applications and "` ~ZZZ156 to have at the same time the necessary flexibility to reach the optimum or nearest to optimum working conditions with treated materials of different characteristics.
Therefore the present invention provides a reactor for the aforesaid uses, permitting, under the aforesaid condi-tions, activation and speeding up of the chemical reactions, assuring that their effec~ is distributed extremely homoge-neously throughout the reaction mass.
Particularly, the present invention provides a reac-tor, which simultaneously has the following advantages: (a)capability to reduce the size of the particles of the solids in suspension to the desired level; (b) homogeneous distribu-tion of chemical throughout the mass, simultaneously with the size reduction of the solid materials in suspension; (c) com-plete recycling of the contents of the reactor inside its spherical interior so that the material passes at every cycle at least one lnlet zone of the chemicals fed in continuously;
and (d) possibility of indirect heating i.e. the heating medium is not mixed with the suspension to be heated, and without the well known inconveniences deriving from the forma-tion of deposits of the suspended materials on the hot surface and thus maintaining a high constant coefficient of heat exchange independently from the type of suspension.
According to the present invention there is provided an apparatus for reacting a solution of cellulosic pulp mate-rial under intimate and turbulent contact with a chemical com-position while simultaneously subjecting the pulp material to a disintegrating treatment, said apparatus comprising: a) a stationary pressure-sealed substantially spherical reactor vessel in which the pulp~material is received and treated under conditions of elevated pressure and temperature, said reactor vessel having a top portion and a bottom portion for
- 2 ~
~22Z156 admitting the material to be treated and for discharging the treated material respectively; b) a rotor member mounted to rotate within said reactor vessel adjacent said bottom por-tion, about a substantially vertical axis; c) a stator member in said bottom portion spaced from and facing said rotor mem-ber to define a disintegrating zone therebetween; d) a helico-centrifugal pump connected with said rotor member for conduct-ing said pulp material axially into said disintegrating area by the aspirational effect generated by the rotation of said rotor and simultaneously generating an impeller action effec-tive to eject the pulp material radially outwards from said disintegrating area and thence in a generally upward direction in turbulent flow within the confines of the walls of said spherical reactor vessel with consequent enhancement of the disintegrating action; e) means for injecting said chemical composition into said disintegrating area and f) baffle ele-; ments extending along the walls of said reactor vessel for indirectly heating said pulp material while it is being treated in said reactor vessel.
: ::
.~
~12ZZlS6 The preser,ce of the rotor, operating as aforesaidcreates a turbulent motion depending on the choice of the structure and working characteristics of the rotor, to obtain the desired size reduc-tion of the solid particles in suspen-sion, optimizing the reaction condi~ions. The turbulence furthermore cooperates to distribute homogeneously the chemi-cals, which are fed near the rotor, 'chroughout the mass.
For some treatments, the best operative conditions are realized when the reactor is put under a super-atmospheric pressure and is of an essentially spherical shape. This con-figuration is of particular importance inasmuch as simul-taneously the following objectives are achieved: (a) to obtain the minimum possible ratio between the reactor's surface and its useful volume, reducing the overall dimensions; (b) to reduce to the utmost the thickness of the walls of the reactor specially in the case when operating under pressure and consequent reduc-tion of the weight and cost of the equipment; (c) to realize, downstreams of the turbulent motion phase, created near the rotor, guided uniform flows on the whole are of 360 and on the different levels where the flows are developing; and (d) to provide indirect heating of the reactor for example by means of steam, without any danger of scaling by solid matter on the - heated surfaces and hence maintaining a good heat exchange coefficient, due to the turbulence and to the flows formed.
The present invention will be further described by way of the accompanying drawings, in which:-Fig. 1 is a lateral view of a reactor according to one . 30 embodiment of the invention;
Fig. 2 is a par\tial sectional view following to a plane passing through the vertical shaft of the reactor and .. ~
., lZZZ~S6 llustrating the parts of the rotor;
Fig. 3 is a sectional view substantially along the line III-III of Fig. 2;
Fig. 4 is a plan view of an alternative shape of the impeller of the rotor;
! Fig. 5 represents schematically the curren-~s inside the reactor; and Fig.s 6, 7 and 8 are schematic illustrations of use of the reactor.
Referring initially to Fig. 1, the reactor comprises a spherical reactor container 10 which may have, for example, a diameter up to 10 m. (500 cu.m of useful volume) supported by vertical legs 11.
A shaft 12 is disposed in the lower part of the con-tainer 10 and extends outside through a stuffing box 21 con-trolling the rotation of the rotor. The shaft 12 is driven through a control group 13 by means of a belt transmission, gear reducer or gearmotor. A gearmotor is preferred when a strong mechanical action is required for the size reduction of the suspended material requiring high power absorbtion with a power , requirement up to 1000 kw.
; The material to be treated is charged into the con-tainer 10 through the charging opening 14 on the upper part, whilst the discharge is made through the outlet 15 in the bot-tom of the container. This procedure of feeding and discharg-ing the material is used when the equipment operates in batch or is the first one of a series for continuous operation.
However, in case of continuous operation or for ' special applications, the flow may be inverted by feeding
~22Z156 admitting the material to be treated and for discharging the treated material respectively; b) a rotor member mounted to rotate within said reactor vessel adjacent said bottom por-tion, about a substantially vertical axis; c) a stator member in said bottom portion spaced from and facing said rotor mem-ber to define a disintegrating zone therebetween; d) a helico-centrifugal pump connected with said rotor member for conduct-ing said pulp material axially into said disintegrating area by the aspirational effect generated by the rotation of said rotor and simultaneously generating an impeller action effec-tive to eject the pulp material radially outwards from said disintegrating area and thence in a generally upward direction in turbulent flow within the confines of the walls of said spherical reactor vessel with consequent enhancement of the disintegrating action; e) means for injecting said chemical composition into said disintegrating area and f) baffle ele-; ments extending along the walls of said reactor vessel for indirectly heating said pulp material while it is being treated in said reactor vessel.
: ::
.~
~12ZZlS6 The preser,ce of the rotor, operating as aforesaidcreates a turbulent motion depending on the choice of the structure and working characteristics of the rotor, to obtain the desired size reduc-tion of the solid particles in suspen-sion, optimizing the reaction condi~ions. The turbulence furthermore cooperates to distribute homogeneously the chemi-cals, which are fed near the rotor, 'chroughout the mass.
For some treatments, the best operative conditions are realized when the reactor is put under a super-atmospheric pressure and is of an essentially spherical shape. This con-figuration is of particular importance inasmuch as simul-taneously the following objectives are achieved: (a) to obtain the minimum possible ratio between the reactor's surface and its useful volume, reducing the overall dimensions; (b) to reduce to the utmost the thickness of the walls of the reactor specially in the case when operating under pressure and consequent reduc-tion of the weight and cost of the equipment; (c) to realize, downstreams of the turbulent motion phase, created near the rotor, guided uniform flows on the whole are of 360 and on the different levels where the flows are developing; and (d) to provide indirect heating of the reactor for example by means of steam, without any danger of scaling by solid matter on the - heated surfaces and hence maintaining a good heat exchange coefficient, due to the turbulence and to the flows formed.
The present invention will be further described by way of the accompanying drawings, in which:-Fig. 1 is a lateral view of a reactor according to one . 30 embodiment of the invention;
Fig. 2 is a par\tial sectional view following to a plane passing through the vertical shaft of the reactor and .. ~
., lZZZ~S6 llustrating the parts of the rotor;
Fig. 3 is a sectional view substantially along the line III-III of Fig. 2;
Fig. 4 is a plan view of an alternative shape of the impeller of the rotor;
! Fig. 5 represents schematically the curren-~s inside the reactor; and Fig.s 6, 7 and 8 are schematic illustrations of use of the reactor.
Referring initially to Fig. 1, the reactor comprises a spherical reactor container 10 which may have, for example, a diameter up to 10 m. (500 cu.m of useful volume) supported by vertical legs 11.
A shaft 12 is disposed in the lower part of the con-tainer 10 and extends outside through a stuffing box 21 con-trolling the rotation of the rotor. The shaft 12 is driven through a control group 13 by means of a belt transmission, gear reducer or gearmotor. A gearmotor is preferred when a strong mechanical action is required for the size reduction of the suspended material requiring high power absorbtion with a power , requirement up to 1000 kw.
; The material to be treated is charged into the con-tainer 10 through the charging opening 14 on the upper part, whilst the discharge is made through the outlet 15 in the bot-tom of the container. This procedure of feeding and discharg-ing the material is used when the equipment operates in batch or is the first one of a series for continuous operation.
However, in case of continuous operation or for ' special applications, the flow may be inverted by feeding
3 30 through the outlet 15 and discharging through the inlet 14.
The reactor is preferentially heated indirectly by means of a heating fluid, generally steam, which enters at 16 ,.
lZZZ156 and exits preferably as condensate, at 17, after having been in contact with heat exchanging surfaces or elements as can be seen better hereafter. Liquid or gaseous chemicals are passed in through the corresponding connection 18, whilst the gases produced by the reaction are discharged at 19, preferably under the control of a pressure regulator and analysis of samples of the discharged gases. Safety and control devices, normally required for pressurized vessels, as for example, manometers and safety valves are installed at the offtake 20.
The internal portion of the reactor container 10 in the zone of the turbulence formation is illustrated in detail in Figures 2, 3 and 4. The shaft 12 entering the reactor through the stuffing box 21, carries the rotor 22 and the rotating disc or ring 23 fixed thereto which cooperates with the lower stationary disc 24 with a perforated zone 25 through which the material to be treated or the treated material leave or enter via the connection 15. The disc 24 and the defibrating discs fixed thereto are crossed by the duct 26 connected to the inlet 18 for passage of liquid and/or gaseous reagents into the mixing and laminating zone 27 between the discs 24 and 23. The gap of this zone 27 or interspace between the static disc 24 and the rotating disc 23 can be varied with the machine working to better adjust it to the desired mechanical treatment to be performed. For the same reasons and depending on the material treated, the surfaces of the discs 23 and 24 may assume different structure characteristics as for example, blades, stakes and abrasive surfaces.
The rotor 22 and the defibrating disc 23 are structured as an impeller of a helico-centrufugal pump with axial admission and rad;al delivery. Indeed in the central part, the spokes 28 which~bring the disc into rotation are profiled as a section of a screw, for suspensions at higher con-A
1~22156 sistencies and low speed of rotation (10-200 r.p.m.), or a proper propeller in case of suspensions at lower consistencies and higher speed of rotation (200-1500 r.p.m.).
The centrifugal part of the pump is formed by the surfaces of the rota~ing disc 23 and the corresponding channels between the aforesaid blades, stakes or abrasive surfaces.
The rotor 22 with disc 23 may be replaced by an open agitator of the type shown at 29 in Fig. 4 specially when the treatment does not require an energy consuming action of de-fibration or disintegration.
The action of the impeller or helico-centrifugal pump, causes, in cooperation with proper baffles 30, circulation of the treated mass of the type shown in Fig. 25, where it may clearly be seen, that the suspension guided by the baffles 30 radially leaves the pump and moves towards the top following the shape of the spherical wall and then concentrates at the top from where it falls down forming a central column 31 sucked from the central part of the rotor.
It has thus been shown that the apparatus is of particular efficiency. Furthermore, it was possible to heat indirectly the suspension during the treatment by letting the heating fluid through connections 32 (Fig.s 1 and 3) into the space defined by the baffles 30 between their surface and the wall of the reactor's shell; space which consequently is not in contact with the suspension during the treatment. The steam circulating inside the baffles 30 is discharged through con-nections 33 (Fig. 1) and heats to the desired temperature the external surface 34 (Fig. 3) of said baffles, the number and shape of which may vary depending upon the quanity of heat to be transmitted to the suspension. On the outside, the baffles are contacted at high speed by the suspension pushed by the helico-centrifugal rotor, creating the conditions for a good heat ~xchange which is maintained during the operation because scaling and deposits on the surface 34 are avoided. The heat-ing fluid or steam condensate are recovered through a distribu-tion ring 35 (Fig. 1) and then passed through a heat source and again sent back in a closed cycle to the upper distribution ring 36.
The reactor having the name "TURBOPULPER" can be used ; ~J for batch operations as shown schematically in Fig. 6 or in continuous operations by putting in series two or more reactors of the same type (Fig. 7). The turbopulper could also be used for continuous operations, where a homogeneous distribution of reagents and 2 is achieved, size reduction of the suspended ; material and heating to the reaction temperature is obtained, whilst the necessary retention time for the complete develop-ment of the reaction is obtained in another static container 37 of an essentially conventional type, also this pressurized and i of suitable shape, in series with the turbopulper.
'I When the apparatus is used, as in the preferred case, to achieve optimum conditions for a delignification treatment, (cooking) following the alkali-oxygen process, it overcomes the mentioned difficulties of the known treatments, represented particularly by the indirect heating of a cellulose-fibres (from wood or short cycle vegetables, straw, etc.) suspension in a liquid, achieving a progressive size reduction of chips or fibre bundles from wood or annual plants with an increase of the total contact surface.
The apparatus also effects a perfect distribution and intimate mixing of the reagents with the fibres in suspension.
Moreover, in the case of the mentioned treatment, yields and activates the quantity of the oxygen required for the delig-nification of the fibrous material, overcoming the problem of the low solubility of oxygen in water and particularly at the ~. ~
:12221S6 temperatures required to obtain the delignification (100-180C).
The capacity of the apparatus to distribute gas in liquid, creates a solution within the permitted limi~s of the equilibriuim conditions and at the same time produces an emulsion of gas in the liquid medium, thus giving rise to a continuous contact and replace;nent of 2 on the surface of the single fibres or bundles, which must be delignified.
As aforesaid, the reaction is eased by a simultaneous mechanical defibration of the fibres. The reactions are speeded up by the simultaneous indirect heating.
The turbopulper operates at consistencies of the fibre suspensions between 3 and 15% depending on the type of material in suspension and on the quantity of liquid necessary to contain the required quantity of 2 as a solution-emulsion for the delignification.
The quantity of active 2' in a liquid solution-emulsion, may reach 10% of the dry cellulosic fibres contained in the reactor. The volume of the apparatus or of each one in the case of operating in series, is chosen so as to achieve reaction times which may vary between 30 minutes and 3 hours.
j The heating medium (generally steam) has characteris-tics which permit the heating up to temperatures which may vary between 60 and 180C. The turbopulper is tested for working pressures up to 20 bars. The pressure naturally depends from the performance required by the apparatus and is the equivalent of the partial gas (2) pressure plus that of the vapor at the ~, corresponding working temperatures.
~ ~' ~ 30 : ~
~ ~ - 8 -
The reactor is preferentially heated indirectly by means of a heating fluid, generally steam, which enters at 16 ,.
lZZZ156 and exits preferably as condensate, at 17, after having been in contact with heat exchanging surfaces or elements as can be seen better hereafter. Liquid or gaseous chemicals are passed in through the corresponding connection 18, whilst the gases produced by the reaction are discharged at 19, preferably under the control of a pressure regulator and analysis of samples of the discharged gases. Safety and control devices, normally required for pressurized vessels, as for example, manometers and safety valves are installed at the offtake 20.
The internal portion of the reactor container 10 in the zone of the turbulence formation is illustrated in detail in Figures 2, 3 and 4. The shaft 12 entering the reactor through the stuffing box 21, carries the rotor 22 and the rotating disc or ring 23 fixed thereto which cooperates with the lower stationary disc 24 with a perforated zone 25 through which the material to be treated or the treated material leave or enter via the connection 15. The disc 24 and the defibrating discs fixed thereto are crossed by the duct 26 connected to the inlet 18 for passage of liquid and/or gaseous reagents into the mixing and laminating zone 27 between the discs 24 and 23. The gap of this zone 27 or interspace between the static disc 24 and the rotating disc 23 can be varied with the machine working to better adjust it to the desired mechanical treatment to be performed. For the same reasons and depending on the material treated, the surfaces of the discs 23 and 24 may assume different structure characteristics as for example, blades, stakes and abrasive surfaces.
The rotor 22 and the defibrating disc 23 are structured as an impeller of a helico-centrufugal pump with axial admission and rad;al delivery. Indeed in the central part, the spokes 28 which~bring the disc into rotation are profiled as a section of a screw, for suspensions at higher con-A
1~22156 sistencies and low speed of rotation (10-200 r.p.m.), or a proper propeller in case of suspensions at lower consistencies and higher speed of rotation (200-1500 r.p.m.).
The centrifugal part of the pump is formed by the surfaces of the rota~ing disc 23 and the corresponding channels between the aforesaid blades, stakes or abrasive surfaces.
The rotor 22 with disc 23 may be replaced by an open agitator of the type shown at 29 in Fig. 4 specially when the treatment does not require an energy consuming action of de-fibration or disintegration.
The action of the impeller or helico-centrifugal pump, causes, in cooperation with proper baffles 30, circulation of the treated mass of the type shown in Fig. 25, where it may clearly be seen, that the suspension guided by the baffles 30 radially leaves the pump and moves towards the top following the shape of the spherical wall and then concentrates at the top from where it falls down forming a central column 31 sucked from the central part of the rotor.
It has thus been shown that the apparatus is of particular efficiency. Furthermore, it was possible to heat indirectly the suspension during the treatment by letting the heating fluid through connections 32 (Fig.s 1 and 3) into the space defined by the baffles 30 between their surface and the wall of the reactor's shell; space which consequently is not in contact with the suspension during the treatment. The steam circulating inside the baffles 30 is discharged through con-nections 33 (Fig. 1) and heats to the desired temperature the external surface 34 (Fig. 3) of said baffles, the number and shape of which may vary depending upon the quanity of heat to be transmitted to the suspension. On the outside, the baffles are contacted at high speed by the suspension pushed by the helico-centrifugal rotor, creating the conditions for a good heat ~xchange which is maintained during the operation because scaling and deposits on the surface 34 are avoided. The heat-ing fluid or steam condensate are recovered through a distribu-tion ring 35 (Fig. 1) and then passed through a heat source and again sent back in a closed cycle to the upper distribution ring 36.
The reactor having the name "TURBOPULPER" can be used ; ~J for batch operations as shown schematically in Fig. 6 or in continuous operations by putting in series two or more reactors of the same type (Fig. 7). The turbopulper could also be used for continuous operations, where a homogeneous distribution of reagents and 2 is achieved, size reduction of the suspended ; material and heating to the reaction temperature is obtained, whilst the necessary retention time for the complete develop-ment of the reaction is obtained in another static container 37 of an essentially conventional type, also this pressurized and i of suitable shape, in series with the turbopulper.
'I When the apparatus is used, as in the preferred case, to achieve optimum conditions for a delignification treatment, (cooking) following the alkali-oxygen process, it overcomes the mentioned difficulties of the known treatments, represented particularly by the indirect heating of a cellulose-fibres (from wood or short cycle vegetables, straw, etc.) suspension in a liquid, achieving a progressive size reduction of chips or fibre bundles from wood or annual plants with an increase of the total contact surface.
The apparatus also effects a perfect distribution and intimate mixing of the reagents with the fibres in suspension.
Moreover, in the case of the mentioned treatment, yields and activates the quantity of the oxygen required for the delig-nification of the fibrous material, overcoming the problem of the low solubility of oxygen in water and particularly at the ~. ~
:12221S6 temperatures required to obtain the delignification (100-180C).
The capacity of the apparatus to distribute gas in liquid, creates a solution within the permitted limi~s of the equilibriuim conditions and at the same time produces an emulsion of gas in the liquid medium, thus giving rise to a continuous contact and replace;nent of 2 on the surface of the single fibres or bundles, which must be delignified.
As aforesaid, the reaction is eased by a simultaneous mechanical defibration of the fibres. The reactions are speeded up by the simultaneous indirect heating.
The turbopulper operates at consistencies of the fibre suspensions between 3 and 15% depending on the type of material in suspension and on the quantity of liquid necessary to contain the required quantity of 2 as a solution-emulsion for the delignification.
The quantity of active 2' in a liquid solution-emulsion, may reach 10% of the dry cellulosic fibres contained in the reactor. The volume of the apparatus or of each one in the case of operating in series, is chosen so as to achieve reaction times which may vary between 30 minutes and 3 hours.
j The heating medium (generally steam) has characteris-tics which permit the heating up to temperatures which may vary between 60 and 180C. The turbopulper is tested for working pressures up to 20 bars. The pressure naturally depends from the performance required by the apparatus and is the equivalent of the partial gas (2) pressure plus that of the vapor at the ~, corresponding working temperatures.
~ ~' ~ 30 : ~
~ ~ - 8 -
Claims (5)
PROPERTY OR PRIVILEGE IS CLAIMED ARE DEFINED AS FOLLOWS:
1. Apparatus for reacting a solution of cellulosic pulp material under intimate and turbulent contact with a chemical composition while simultaneously subjecting the pulp material to a disintegrating treatment, said apparatus com-prising: a) a stationary pressure-sealed substantially spher-ical reactor vessel in which the pulp material is received and treated under conditions of elevated pressure and temperature, said reactor vessel having a top portion and a bottom portion for admitting the material to be treated and for discharging the treated material respectively; b) a rotor member mounted to rotate within said reactor vessel adjacent said bottom por-tion, about a substantially vertical axis; c) a stator member in said bottom portion spaced from and facing said rotor mem-ber to define a disintegrating zone therebetween; d) a helico-centrifugal pump connected with said rotor member for conduct-ing said pulp material axially into said disintegrating area by the aspirational effect generated by the rotation of said rotor and simultaneously generating an impeller action effec-tive to eject the pulp material radially outwards from said disintegrating area and thence in a generally upward direction in turbulent flow within the confines of the walls of said spherical reactor vessel with consequent enhancement of the disintegrating action; e) means for injecting said chemical composition into said disintegrating area and f) baffle ele-ments extending along the walls of said reactor vessel for indirectly heating said pulp material while it is being treated in said reactor vessel.
2. Apparatus according to Claim 1 in which said heat exchange means comprise baffle elements extending along the walls of said reactor vessel.
3. Apparatus according to Claim 1 or 2, in which said rotor member and said stator member are provided with cooperating shearing elements for enhancing the disintegrating action.
4. Apparatus according to Claim 1 in which said rotor member and said stator member are relatively adjustable to vary the width of said disintegrating zone.
5. Apparatus according to Claim 2 in which said reactor vessel is constructed to withstand an internal abso-lute pressure of 20 bars and a temperature of 180°C.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CA000429614A CA1222156A (en) | 1983-06-03 | 1983-06-03 | Reactor to perform chemical reactions with dimensional reduction of solid materials |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CA000429614A CA1222156A (en) | 1983-06-03 | 1983-06-03 | Reactor to perform chemical reactions with dimensional reduction of solid materials |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CA1222156A true CA1222156A (en) | 1987-05-26 |
Family
ID=4125395
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA000429614A Expired CA1222156A (en) | 1983-06-03 | 1983-06-03 | Reactor to perform chemical reactions with dimensional reduction of solid materials |
Country Status (1)
| Country | Link |
|---|---|
| CA (1) | CA1222156A (en) |
-
1983
- 1983-06-03 CA CA000429614A patent/CA1222156A/en not_active Expired
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