CN203383092U - Causticizing technology device for preparing precipitated calcium carbonate by recovering alkali from papermaking - Google Patents
Causticizing technology device for preparing precipitated calcium carbonate by recovering alkali from papermaking Download PDFInfo
- Publication number
- CN203383092U CN203383092U CN201320405798.9U CN201320405798U CN203383092U CN 203383092 U CN203383092 U CN 203383092U CN 201320405798 U CN201320405798 U CN 201320405798U CN 203383092 U CN203383092 U CN 203383092U
- Authority
- CN
- China
- Prior art keywords
- tank
- causticizing
- causticization
- calcium carbonate
- utility
- 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.)
- Expired - Fee Related
Links
Landscapes
- Paper (AREA)
Abstract
The utility model provides a causticizing technology device for preparing precipitated calcium carbonate by recovering alkali from papermaking. The causticizing technology device comprises a digestor, a mixing tank, multiple causticizing tanks, a storing tank and a depositing tank, wherein the digestor is used for generating a Ca(OH)2 digestive liquid, the mixing tank is connected with the digestor and a container containing an NaOH solution, the multiple causticizing tanks are connected in sequence, the first causticizing tank is connected with the mixing tank and each causticizing tank is internally connected with a green liquid container, the storing tank is connected with the last causticizing tank, and the depositing tank is connected with the lower part of the storing tank and a container containing an Na2CO3 solution. Due to the adopted multistage reflux causticizing technology, the causticizing technology device not only achieves the aim of alkali recovery, but also obtains high-whiteness fine-granularity precipitated calcium carbonate with an aragonite crystal structure as main, without re-carbonization after causticization, and the high-whiteness fine-granularity precipitated calcium carbonate can be directly used for paper filling and substitute for commercial precipitated calcium carbonate; in addition, as for the existing alkali recovery technology, special reaction equipment is not required to be customized for the causticizing technology device, and the causticizing technology device is easy to implement.
Description
Technical field
The utility model relates to field of papermaking, and particularly a kind of alkali recovery prepares the causticization method of winnofil, and a kind of alkali recovery prepares the causticization process device of winnofil.
Background technology
Soda pulping process is the technique extensively adopted in current most of pulp and paper making (especially grass as raw material pulp and paper making).Can produce a large amount of winnofils (white clay) in the causticization process of soda pulping process papermaking.Causticization is the Na in the green liquor that soda pulping process papermaking is produced
2cO
3with Ca (OH)
2causticizing reaction occurs, and generates containing the white liquid of NaOH with containing precipitate C aCO
3the course of reaction of white clay.
Meanwhile, calcium carbonate is increasingly extensive as filler and the application of coating pigment in the industry such as papermaking.Along with paper lightweight development and the Modern Paper Machine speed of a motor vehicle improve, require calcium carbonate to there is higher opacity and the lower wearing and tearing to forming net.But the white clay of traditional causticization process production exists, whiteness is low, the problem of form lack of homogeneity, can not satisfy the demand.In existing paper technology, general commodity in use calcium carbonate is as filler, and to after causticization without carbonization, the technical scheme that directly causticization is produced winnofil rarely has report.
In view of the demand of paper industry to high-quality calcium carbonate constantly increases, therefore how to improve and improve the winnofil quality in the causticization process, making its main component is the aragonitic crystal structure, with the performance requirement that meets filler and coating pigment etc. and replace commodity calcium carbonate, be those skilled in the art's technical problems urgently to be resolved hurrily.
The utility model content
In view of this, the causticization process device that provides a kind of alkali recovery to prepare winnofil is provided the purpose of this utility model, and this causticization process device can promote the crystal growth of aragonitic structure, improves the quality of winnofil.
Alkali recovery of the present utility model prepares the causticization process device of winnofil, and this causticization process device comprises:
Form containing Ca (OH)
2the digester of digestive juice;
Blending tank, connect described digester and containing the container of NaOH solution;
A plurality of causticization tanks that connect successively, wherein first causticization tank connects described blending tank, in described each causticization tank, connects respectively the green liquor container;
Basin, described basin connects last causticization tank;
Settling tank, described settling tank connects the bottom of described basin and contains Na
2cO
3the container of solution.
Further, the upper and lower of described basin all is connected with described blending tank, and described basin is the described container containing NaOH solution.
Digestive juice of the present utility model and green liquor carry out causticizing reaction at a plurality of causticization tanks, by adopting multi-stage countercurrent causticization technology, have reached desirable causticization effect.Compared with prior art, the utility model has not only reached the purpose that alkali reclaims, and just can obtain having that whiteness is high, the high-quality calcium carbonate of fine size after causticization without carbonization, gained calcium carbonate be take the aragonitic crystal structure as main, can directly as filler, replace commodity calcium carbonate, there is significant economic benefit; The consersion unit that the utility model is special-purpose without customization carries out Optimizing Reconstruction on the basis of existing alkali recovery equipment, can realize the technical solution of the utility model, has advantages of easy to implement.
The accompanying drawing explanation
Fig. 1 is the causticization process installation drawing that the utility model one embodiment prepares winnofil.
The specific embodiment
Below the drawings and specific embodiments of the present utility model are described in further detail.For the person of ordinary skill in the field, to detailed description of the present utility model, above and other purpose of the present utility model, feature and advantage will be apparent.
For the ease of to understanding of the present utility model, first causticization method is described.The papermaking causticization method of the utility model one embodiment comprises step a, step b and step c.
In step a, the utility model will be containing Ca (OH)
2digestive juice, with the aragonite calcium carbonate crystal seed, mix containing NaOH solution, mixed liquor enters successively a plurality of causticization tanks and carries out causticizing reaction, in described each causticization tank, passes into containing Na
2cO
3green liquor;
Wherein, should be containing Ca (OH)
2digestive juice can be selected lime and clear water digestion afterproduct, also can select the white liquid digestion of one-level described later lime, and it can be the Ca (OH) that mass fraction is 10～50%
2suspension; Can be the special solution of making containing NaOH solution, be preferably the white liquid of one-level in conventional alkali paper-making technique.It can be also the white liquid of the utility model secondary described later, and the utility model is not limited to this.Preferably containing Ca (OH)
2digestive juice with containing after NaOH solution mixes, the molar concentration of NaOH wherein is 1～4mol/L.Containing Ca (OH)
2digestive juice can be 1:0.5～3 with the volume ratio containing NaOH solution.Further, in this mixed liquor, can also add the aragonite calcium carbonate crystal seed, this crystal seed can adopt the first clay wash of step b separation, also can adopt the aragonite calcium carbonate of special preparation.
The utility model passes into containing Na in each causticization tank
2cO
3green liquor, and by causticizing reaction, this green liquor is converted into to white liquid.This green liquor forms product after preferably adopting grass as raw material alkaline cooking, alkali to reclaim.In addition, in order to guarantee grass as raw material, the precipitation of causticizing reaction and calcium carbonate is not caused to " silicon interference ", can adopt and stay the silicon digesting technoloy that silicon is retained in straw pulp, with the silicone content by green liquor, be controlled at and be less than 1～8g/L (with SiO
2meter).
Should be understood that, in order to make high-quality aragonitic winnofil, the quality of green liquor is most important, and the utility model preferably adopts following steps to form green liquor:
Add grass as raw material and alkali lye and carry out cooking reaction in digester, form straw pulp and black liquor, comprise NaOH, Na in described alkali lye
2s, digesting assistant and stay silicea; Described green liquor is the lysigenous product of black-liquor combustion.Aforementioned cooking reaction can be that intermittence or continous mode are stayed the silicon boiling, and the utility model is not limited to this.
Owing in aforementioned alkali lye, having added and having stayed silicea, grass as raw material suppresses silicon in the boiling delignification to be shifted in black liquor, has reduced the content of silicon in the black liquor.The black liquor of this low silicon content can be burnt in the alkali stove, and alkali stove fused mass dissolves can form green liquor.What dissolve alkali stove fused mass can be both clear water, the white liquid of secondary, the second clay wash wash water described later or their mixing, and the utility model is not limited to this.
On the basis of technique scheme, resulting green liquor is comparatively muddy turbid green liquor.In order to improve causticization effect and winnofil quality, the utility model preferably in each causticization tank stream add containing Na
2cO
3clear green liquor, this pure and turbid liquid is pretreated green liquor.It has carried out preliminary treatment on aforementioned (turbid) green liquor basis, and preliminary treatment comprises green liquor is placed in to the preliminary treatment tank, adds green liquor quality 0～5% milk of lime (in CaO) and 0～1% polyacrylamide to stir and clarify.Pretreated green liquor can be sent into standby causticization in the green liquor storage tank and use.
As an embodiment of the present utility model, staying the silicea that stays in the alkali lye of silicon boiling is that the calcium base stays silicea, the described active component of silicea that stays at least comprises calcareous material, the mass fraction of described calcareous material is M, the described active component of silicea that stays also comprises the aluminium-containing substance that mass fraction is 0～0.8M, and mass fraction is 0～0.5M containing the magnesium material, wherein each mass fraction calculates with oxide, described calcareous material is the product after lime stone or dolomite calcination, wash aforementioned product with water, and add described aluminium-containing substance and/or stay silicea containing magnesium material formation emulsion.Preferably, described calcareous material is 1100～1200 ℃ of burnt lime stones.
Described aluminium-containing substance can be bauxite roasting afterproduct.Preferably, described aluminium-containing substance is that granularity is not less than baked bauxite, the wherein mass fraction of Fe<4% under 60 orders, 550～850 ℃.
Described can be dolomite or magnesite calcining afterproduct containing the magnesium material.Preferably, described is granularity for being not less than 60 orders, 800～1500 ℃ of burnt dolomites or magnesite containing the magnesium material.
In an embodiment of the present utility model, calcareous material, aluminium-containing substance and be respectively lime stone, bauxite and dolomite containing the magnesium material, its mass ratio is 1 ︰ 0.5 ︰ 0.2, preparation is containing NaOH, Na
2s, digesting assistant and stay the mass fraction of silicea to be respectively 5%, 0.5%, 0.03% and 1% boiling alkali lye, the 1:3 25m that simultaneously grass as raw material (as reed) and aforementioned alkali lye packed into by volume
3spherical digester in, 6 tons, the reed of packing into altogether.Boiling method routinely, after idle running 15min, 1.5h is warming up to 160 ℃, and insulation 2h carries out cooking reaction, spurts and obtains straw pulp.To the steaming prod testing result, black liquor desiliconization rate 75%.
It should be noted that, each component of alkali lye of the present utility model also can have other content, comprises the NaOH that mass fraction is 2～18% in preferred alkali lye described in the utility model, the Na that mass fraction is 0～2%
2s, the digesting assistant that mass fraction is 0～0.2%, mass fraction is 0.1～5% stays silicea.Cooking reaction also can have other process conditions, and the mass ratio of preferred described grass as raw material and alkali lye is 1 ︰ 1～5, and the reaction temperature of described cooking reaction is room temperature～190 ℃, and the reaction time of described cooking reaction is 35～180 min.The aforementioned techniques scheme all can reach higher desiliconization rate in black liquor, and the silicone content in the assurance green liquor is controlled at and is less than 1～8g/L (with SiO
2count), thus while making causticizing reaction, avoid silicon to disturb.
The utility model carries out causticizing reaction in various degree in each causticization tank, and preferred causticization tank of the present utility model comprises 3, the Na added in first causticization tank
2cO
3the Na added in 20～40%, the second causticization tank of amount for total theoretical amount
2cO
3the Na added in the 30～50%, three causticization tank of amount for total theoretical amount
2cO
3amount is 40～60% of total theoretical amount; Total theoretical amount is with the Ca in mixed liquor (OH)
2the amount of digestive juice is carried out stoichiometry.After the 3rd causticization tank causticizing reaction, Ca (OH)
2digestive juice should be excessive in addition, and preferably the amount of ash excessively of CaO is 0～20%.The utility model is not limited to this.
Aforementioned containing Ca (OH)
2temperature during digestive juice digestion is room temperature～90 ℃, and the causticization temperature of each causticization tank is room temperature～100 ℃, and the speed of agitator of each causticization tank reduces successively.Its speed of agitator can be respectively high as far as possible, moderate and maintain the product crystallization and not precipitate.
In step b, the utility model sinks the reactant liquor of last causticization tank clear, separates the white liquid of the first clay wash and one-level.As previously mentioned, in the end after causticization tank causticizing reaction, Ca (OH)
2digestive juice is excessive in addition, and wherein the main component of the white liquid of one-level is NaOH.The white liquid of one-level that step b separates can be used as described in step a containing NaOH solution.In addition, the white liquid of this one-level can also be for carrying out pulping by cooking.
In step c, the utility model is by described the first clay wash and containing Na
2cO
3solution reaction, by unreacted Ca (OH) completely
2react completely, separate the white liquid of the second clay wash and secondary.Should be containing Na
2cO
3solution can be the aforesaid green liquor of the utility model, can be also the special solution of making, and the utility model is not limited to this.In step c, Na
2cO
3solution is excessive, the Na added in the first clay wash in preferred steps c
2cO
3amount is 100～120% of theoretical amount, and this theoretical amount is with the Ca in clay wash (OH)
2the amount of digestive juice is carried out stoichiometry.Therefore, wherein the main component of the white liquid of secondary is NaOH.The main component of this second clay wash is CaCO
3, this second clay wash separates and can directly be used as the copy paper filler through (secondary) wash water, and filler can be 10～70% CaCO
3suspension.Wherein, the CaCO of aragonitic crystal structure
3account for 1～95%.
In the utility model one embodiment, mixed liquor adopts the Ca (OH) that mass fraction is 10～50%
2the white liquid of the one-level that suspension and molar concentration are 2mol/L NaOH, volume ratio is 1 ︰ 1, in green liquor, total alkali concn 100g/L(is in NaOH), silicone content 2g/L(is with SiO
2meter), the total residence time of controlling three causticization tanks is 2 hours, and it is 50 ℃ that three causticization tanks are controlled temperature, and speed of agitator is respectively 80 rev/mins, 50 rev/mins and 20 rev/mins.The products obtained therefrom feature is as follows:
The white liquid of one-level: effective alkali concentration 98g/L (in NaOH), carsticity 90.5%;
The white liquid of secondary: effective alkali concentration 80g/L (in NaOH);
White clay: the dry processing detected after filtration, whiteness 91%, 325 screen residue 0.25%, the CaCO of aragonitic crystal structure
3account for 78%.
In another embodiment of the utility model, the mixed liquor composition is the same, and the total alkali concn 110g/L(of green liquor is in NaOH), silicone content 1.5g/L is (with SiO
2meter), the total residence time of controlling three causticization tanks is 2 hours, and it is 85 ℃ that three causticization tanks are controlled temperature, and speed of agitator is respectively 100 rev/mins, 50 rev/mins and 10 rev/mins.The products obtained therefrom feature is as follows:
The white liquid of one-level: effective alkali concentration 105g/L(is in NaOH), carsticity 89%;
The white liquid of secondary: effective alkali concentration 82g/L(is in NaOH);
White clay: the dry processing detected after filtration, whiteness 90.2%, 325 screen residue 0.15%, aragonitic crystal CaCO
3account for 83%.
Shown in Fig. 1, be the causticization process installation drawing that the utility model one embodiment prepares winnofil, this causticization process device comprises digester 1, blending tank 2, a plurality of causticization tank 3, basin 4 and settling tank 5.Wherein, this digester 1 forms containing Ca (OH) for digesting CaO
2digestive juice can be put into selected lime and clear water in this digester 1.
A plurality of causticization tanks 3 connect successively, and wherein first causticization tank 3 connects described blending tank 2, in described each causticization tank 3 respectively stream add containing Na
2cO
3green liquor; Mixed liquor in blending tank 2 and green liquor can pump in causticization tank 3 by pumping mechanism.
Basin 4 connects last causticization tank 3, for separating of the first clay wash and the white liquid of one-level; In this basin 4, Ca (OH)
2digestive juice is excessive in addition, and wherein the main component of the white liquid of one-level is NaOH.Between basin 4 and causticization tank 3, can adopt pumping mechanism to connect.
Settling tank 5 connects the bottom of basin 4 and contains Na
2cO
3the container of solution, pass into described the first clay wash and contain Na
2cO
3solution, separate the white liquid of the second clay wash and secondary.Can adopt membrane pump that described the first clay wash is passed in settling tank 5, Na in settling tank 5
2cO
3solution is excessive, and wherein the main component of the white liquid of secondary is NaOH.The main component of this second clay wash is CaCO
3.
Further, the upper and lower of basin 4 of the present utility model all is connected with blending tank 2, and described basin 4 is the described container containing NaOH solution.The first clay wash of the bottom of basin 4 is as the aragonite calcium carbonate crystal seed, and the white liquid of the one-level on top is as containing NaOH solution.It should be noted that, the white liquid of this one-level also can pump in digester the alkali lye component that is used as pulping by cooking.In addition, the white liquid of this secondary also can be as the solvent that generates green liquor.The aragonite calcium carbonate crystal seed of sending into blending tank 2 can also be the special aragonite calcium carbonate crystal seed of making.Between aforementioned each parts, also can be connected by pumping mechanism.
Principle and the aforementioned causticization method of causticization process device for preparing winnofil due to the utility model is basic identical, and this paper is no longer repeated at this.In settling tank 5, the second clay wash of precipitation separates and can directly be used as the copy paper filler through (secondary) wash water, and filler can be 1～70% CaCO
3suspension.Wherein, the CaCO of aragonitic crystal structure
3account for 1～95%.
The utility model reclaims purpose simultaneously reaching alkali, after causticization, without carbonization, just can obtain that whiteness is high, the high-quality winnofil of fine size, can be directly used in paper and add and fill out, and has significant economic benefit; And the utility model carries out Optimizing Reconstruction and can realize on the basis of existing alkali recovery equipment, the special-purpose consersion unit without customization, easy to implement.Therefore the beneficial effects of the utility model are apparent.
It should also be understood that; although the utility model clearly demonstrates by above embodiment; yet in the situation that do not deviate from the utility model spirit and essence thereof; the person of ordinary skill in the field is when making various corresponding variations and correction according to the utility model, but these corresponding variations and correction all should belong to the protection model of claim of the present utility model.
Claims (2)
1. an alkali recovery prepares the causticization process device of winnofil, it is characterized in that, comprising:
Form containing Ca (OH)
2the digester of digestive juice (1);
Blending tank (2), connect described digester (1) and containing the container of NaOH solution;
A plurality of causticization tanks (3) that connect successively, wherein first causticization tank (3) connects described blending tank (2), in described each causticization tank (3), connects respectively the green liquor container;
Basin (4), described basin (4) connects last causticization tank (3);
Settling tank (5), described settling tank (5) connects the bottom of described basin (4) and contains Na
2cO
3the container of solution.
2. causticization process device according to claim 1, is characterized in that, the upper and lower of described basin (4) all is connected with described blending tank (2), and described basin (4) is the described container containing NaOH solution.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201320405798.9U CN203383092U (en) | 2012-09-28 | 2013-07-09 | Causticizing technology device for preparing precipitated calcium carbonate by recovering alkali from papermaking |
Applications Claiming Priority (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201220501335.8 | 2012-09-28 | ||
| CN201220501335 | 2012-09-28 | ||
| CN201320405798.9U CN203383092U (en) | 2012-09-28 | 2013-07-09 | Causticizing technology device for preparing precipitated calcium carbonate by recovering alkali from papermaking |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN203383092U true CN203383092U (en) | 2014-01-08 |
Family
ID=49871604
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201320405798.9U Expired - Fee Related CN203383092U (en) | 2012-09-28 | 2013-07-09 | Causticizing technology device for preparing precipitated calcium carbonate by recovering alkali from papermaking |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN203383092U (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103303956A (en) * | 2012-09-28 | 2013-09-18 | 湖南文理学院 | Causticizing method and process device for recycling papermaking alkali to prepare precipitated calcium carbonate |
-
2013
- 2013-07-09 CN CN201320405798.9U patent/CN203383092U/en not_active Expired - Fee Related
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103303956A (en) * | 2012-09-28 | 2013-09-18 | 湖南文理学院 | Causticizing method and process device for recycling papermaking alkali to prepare precipitated calcium carbonate |
| CN103303956B (en) * | 2012-09-28 | 2015-08-26 | 湖南文理学院 | A kind of alkali recovery prepares causticization method and the process unit of precipitated chalk |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN103303956B (en) | A kind of alkali recovery prepares causticization method and the process unit of precipitated chalk | |
| CN101327942A (en) | Method for preparing light magnesium carbonate and magnesium oxide from dolomite sea water bittern | |
| CN101684570A (en) | Method for preparing calcium carbonate crystal whisker with controllable shape | |
| CN103145160A (en) | Method for producing alumina by using high-alumina fly ash | |
| CN101343074B (en) | Bauxite dissolving out method for reducing caustic alkali combined in prepared red mud | |
| CN103332714B (en) | Reduce the method for low steaming carbonate in mother liquor content | |
| CN102561086B (en) | Method for preparing spindle crystal form alkali recovery white clay | |
| CN203383092U (en) | Causticizing technology device for preparing precipitated calcium carbonate by recovering alkali from papermaking | |
| CN103880058B (en) | A kind of precipitated chalk production technique of falling magnesium increasing calcium | |
| CN103068737A (en) | Lime causticization product brightness improvement via pre-slaking | |
| CN101279756A (en) | Preparation of polyaluminium sulfate | |
| CN100542963C (en) | A kind of preparing fiber lightweight calcium | |
| CN109336158A (en) | The method that high calcium witherite mineral produces barium chloride | |
| US4894217A (en) | Process for causticizing of an aqueous solution containing alkali carbonate | |
| CN101580250A (en) | Filtration method of sodium aluminate solution | |
| CN101734696B (en) | Method for removing organic matter by Bayer process | |
| CN110395748A (en) | The method that lithium carbonate causticizing process prepares lithium hydroxide | |
| CN105540624A (en) | Preparation method of high purity acicular magnesium hydroxide | |
| CN102079536B (en) | Method for producing caustic soda and papermaking filler calcium carbonate by using natural alkali liquor | |
| CN1198402A (en) | Telchnological process of sodium method producing bleaching powder extract | |
| CN108569716A (en) | A kind of method of crude liquor of sodium aluminate refining filtering | |
| CN101734697A (en) | Method for causticizing and eliminating organics by adding lime milk in aluminum hydroxide wash liquor | |
| CN105001933A (en) | Environmentally-friendly sulfur fixation coal binder prepared from causticized lime mud | |
| CN101591020A (en) | A kind of method and system thereof that utilizes aluminous fly-ash to produce white carbon black | |
| CN103991851A (en) | New process for green and cyclic production of hydrazine hydrate |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20140108 Termination date: 20140709 |
|
| EXPY | Termination of patent right or utility model |