JP4580321B2 - Continuous synthesis method of high-performance zeolite - Google Patents

Description

  The present invention relates to a method for synthesizing zeolite from a solid raw material containing silica and / or alumina, and reacts continuously by mixing, heating, dissolving, adjusting the temperature, adding a secondary raw material with an alkaline aqueous solution of the solid raw material, The present invention relates to a method for continuously synthesizing a desired type (A type, X type, Y type) zeolite from which heavy metals have been removed to a level satisfying the standard.

  Zeolite is a silicate mineral that belongs to an aluminosilicate that has a regular three-dimensional structure of silica and alumina and contains crystal water, contains ion-exchangeable cations, and is weakly retained water that is easily reversibly dehydrated. It has features such as being connected and having a three-dimensional network structure. Zeolite is used as a desiccant and deodorant because of its strong adsorptivity, and because it has cation exchange in aqueous solution, it is used for soil improvement materials, wastewater treatment, and purification of fish ponds. Moreover, since it also has a catalytic action as a solid acid, it may be used, for example, as a catalyst for gasoline production, and further used as a molecular sieve for purification of lubricating oil.

  Zeolite is roughly classified into natural zeolite and synthetic zeolite, and especially zeolite synthesized from coal ash is often called artificial zeolite. Natural zeolites are mainly produced in two or three types of zeolite as mineral resources, but they are inexpensive, but they contain many impurities and the content of impurities is indefinite. There is a problem in use that the function is low and the quality varies greatly depending on the content of impurities. Due to its low price, it has been used in some fields such as agricultural soil improvement and drainage water purification, and its demand has been increasing year by year.

  Synthetic zeolites are mainly produced from industrial raw materials, and conventionally, various types of single crystal zeolites with high purity are synthesized by a batch type apparatus using sodium aluminate, water glass and caustic soda as main raw materials. Since this synthetic zeolite is a single crystal having a high purity without impurities, it exhibits high functions, but there are problems that the raw material is an industrial raw material and that the production cost is high due to a small amount of production using a batch apparatus. Therefore, the application field is limited to a special field, and it is not used for large-scale consumption fields such as agricultural soil improvement, general soil improvement, and drainage water purification.

  Next, artificial zeolite is synthesized from coal ash by some manufacturers, and is manufactured and sold under the name of artificial zeolite. Such artificial zeolite is manufactured by a batch type or semi-batch type device as disclosed in Patent Documents 1 to 3, for example.

  The above artificial zeolite is mainly composed of P-type zeolites among many kinds of zeolites, and sometimes contains one to several kinds of zeolites and / or mixed crystal zeolites containing a small amount of non-zeolite sodalite. Yes, manufactured by batch-type equipment. In order to synthesize single-crystal zeolite from coal ash, which is a waste product, it is necessary to create specific narrow synthesis conditions that differ for each zeolite to be synthesized. However, in batch equipment, the synthesis conditions must be kept constant within a narrow range. Therefore, a mixed crystal zeolite composed mainly of P-type zeolite is produced. In general, P-type zeolite has the smallest pore size among 2.6 kinds of zeolites, and there is a problem that applications are limited even if the cation exchange capacity is equivalent to other zeolites. .

  Furthermore, since artificial zeolite is manufactured by a batch-type apparatus as described above, it has not led to synthesis of single-crystal high-performance zeolite of A type, X type or Y type until now, and mixed crystals are produced for each production batch. In addition, the purity of the main component P-type zeolite varies and the proportion of mixed crystals also varies, so there is a problem that the quality is not uniform. Due to these problems, the usage destinations are not so wide. In the above, the single crystal high-functional zeolite means that any one of the crystal types of A type, X type and Y type is contained alone. For example, in the case of A type, other X type, This means that Y-type and P-type materials are not contained, but it does not mean that anything other than zeolite crystals is not contained. This also applies to the following.

  Since there existed the above problems in a batch type apparatus, the continuous manufacturing method and apparatus of a zeolite are proposed by patent document 4 and patent document 5 recently, for example.

  The example of Patent Document 4 relates to a method for continuously producing artificial zeolite in a circulating fluidized tank and an apparatus therefor. According to this apparatus, stirring is performed relatively well, but reaction products and raw materials are circulated. Since mixed backmixing occurs, there is a problem that a mixed crystal zeolite mainly composed of P type is synthesized, and any single crystal high-functional zeolite of A type, X type or Y type cannot be selectively synthesized.

  The example of patent document 5 is proposed in order to solve the problem in the example of patent document 4, and the reaction process is divided into two processes, a tube contact reaction process and a rotating disk contact reaction process. Is a method in which a zeolite raw material is continuously passed through a catalytic reaction tube to produce a zeolite intermediate composition, and the intermediate composition is sequentially stirred by a multistage rotating disk in a rotating disk contacting reaction process to produce a desired zeolite. .

However, in the method of Patent Document 5, the reaction temperature for the initial reaction after dissolution is lower than the melting temperature of the coal ash and the auxiliary raw material in the tube contact reaction step of the first step. When an initial reaction occurs at a high melting temperature, a precursor of P-type zeolite can be made in addition to A-type, X-type or Y-type zeolite precursor , and single-crystal high-performance zeolite of A-type, X-type or Y-type can be synthesized. However, there is a problem that the P-type zeolite is mixed crystal.

  Further, in the invention of Patent Document 5, a variety of wastes are produced by adding one or more crystalline minerals having a specific Si / Al ratio to a zeolite raw material or a zeolite intermediate composition to cause a zeolitic reaction. Even when used as a raw material, since a specific type of zeolite corresponding to the added crystal mineral is derived, as a result, without adjusting the Si / Al ratio to a predetermined value in advance. However, it is said that waste having an arbitrary Si / Al ratio can be easily adopted as a zeolite raw material. This is a case where a mixed crystal zeolite is synthesized with P-type zeolite as a main component. Crystalline high-performance zeolite (A type, X type, Y type) cannot be selectively produced. In addition, since a circulation process is provided, back-mixing occurs, so that mixed crystal zeolite mainly composed of P-type is synthesized, and single-crystal high-performance zeolite of A-type, X-type or Y-type cannot be synthesized. There was a problem.

  Next, Patent Document 6 describes an invention relating to a method for producing A-type zeolite using coal ash as a main raw material, but the invention of Patent Document 6 includes any of A-type, X-type, and Y-type. There is no structure for selectively synthesizing such single-crystal high-functional zeolite, and Patent Document 6 does not disclose a method or apparatus for continuously producing these zeolites. In the invention of Patent Document 6, coal ash as a main raw material is stirred in an alkaline solution at a predetermined temperature and time, and then an aluminum source, a sodium source and water as auxiliary raw materials are added and heated to stir to react. However, since the reaction is carried out while heating, there is a problem that it is difficult to adjust the reaction temperature, and it is impossible to produce a desired type of zeolite efficiently, as well as to produce continuously.

Also, since heavy metals remain in the form of coal ash and sewage sludge incineration ash, etc., these are currently used as cement raw materials, or after taking measures to prevent unnecessary heavy metals from flowing out. In many cases, landfills are disposed of. Zeolite can be produced by hydrothermal synthesis using industrial waste containing SiO ₂ and Al ₂ O ₃ such as coal ash, sewage sludge incineration ash, municipal waste incineration ash, etc., but heavy metals are also included in the produced zeolite Has been confirmed to be partly included, limiting the use expansion. If the heavy metals concentrated in coal ash, etc. can be removed to a level that satisfies environmental standards as a pretreatment for resource recovery without eluting the components necessary for resource recovery, the product can be used in a wide variety of soil improvement materials, etc. Will open. However, in the inventions of Patent Documents 1 to 6, no study has been made on the removal of heavy metals and the technology therefor in the production of zeolite.

  In addition, as a general conventional heavy metal removal method, a method of dissolving and removing contained heavy metal using an acid is already well known. However, according to this method, heavy metals contained in industrial waste such as coal ash can be removed, but silica and alumina components required for zeolite synthesis contained in coal ash etc. are eluted. However, there is a problem that the conventional heavy metal removal method using an acid cannot be applied as it is.

Incinerated ash is composed of granular or amorphous particles. In the case of coal ash, fly ash is composed of particles of 1 μm to 200 μm. For example, when zeolite synthesis is performed using incinerated ash such as coal ash as the main raw material, silica and alumina, which are the raw materials for zeolite synthesis, are eluted from the surface of each particle of the incinerated ash, and zeolite synthesis is performed on the surface of each particle. Is called. Therefore, since the synthesized zeolite is added to the coal ash particles, the size of the synthesized zeolite is added, so there is a problem that the synthesized zeolite particle size is not less than the particle size of the incinerated ash of the main raw material. .
Incidentally, the zeolite synthesized from industrial raw materials such as caustic soda, sodium aluminate, water glass, etc. has a particle size of 10 μm or less. Although it has been confirmed that it can be reduced, since it is currently produced from industrial raw materials by a batch-type apparatus, the production cost of zeolite is increased, and its use is not widespread.
JP-A-6-321524 JP-A-6-321525 JP-A-6-321526 JP-A-10-324518 JP 2002-187715 A JP-A-6-100314

The proposed continuous production method and apparatus for artificial zeolite, which replaces the conventional batch-type production method, have the above-mentioned problems, and the method of reacting while stirring with heating continuously synthesizes the desired type of zeolite. In addition, there is a problem that the synthesized zeolite contains heavy metals exceeding the value determined by the environmental standards .

The present invention solves the above problems and can continuously synthesize a high-performance zeolite of a desired type (A, X, Y type) without lowering the synthesis rate. An object of the present invention is to provide a new method capable of synthesizing fine zeolite.

The constitution of the present invention made for the purpose of solving the above problems is a method of synthesizing zeolite from a solid raw material containing silica and / or alumina by an alkaline hydrothermal reaction, wherein the raw material is added before the zeolitization reaction. After mixing with an alkaline aqueous solution, heating to a temperature required to promote dissolution in the heating step, and proceeding with dissolution of the silica and / or alumina component in the dissolution step, the solution is converted into A-type, X-type, Y-type. cooled to any type temperature suitable for synthesis of the zeolite of, after the cooling, SiO ₂ source required to obtain a composition that is suitable for synthesis of the zeolite and / or Al ₂ O ₃ source and by adding a predetermined type of seed zeolites, in the method for synthesizing the zeolite side reactions with depressive example high synthesis rate, the acid before the solid material is mixed with an aqueous alkaline solution of water The mixture is stirred and mixed, and at least one removal component selected from cadmium, lead, hexavalent chromium, arsenic, mercury, selenium, fluorine, and boron contained in the solid raw material is an effective component in the solid raw material. After removing the silica and / or alumina components without losing them into an acid aqueous solution, a removal step for separating the removed component eluate is provided. In the preparation step, the solid raw material is mixed with an acid aqueous solution in a preparation tank. Elution of the removed component into the aqueous acid solution while mixing with stirring, continuously supplying to the filter to separate the removed component eluate, and determining the removed component elution concentration of the separated eluate In the case where the concentration is less than a predetermined concentration, the step of returning to the preparation tank and adding an acid to circulate is included.

  In the above-mentioned configuration, the present invention can also synthesize fine-grained zeolite by using the reaction recovery solution after synthesis of zeolite as part of the alkaline aqueous solution.

In the present invention, a SiO ₂ source, an Al ₂ O ₃ source and a Na ₂ O source may be added to the reaction recovery liquid.

  Further, the present invention is the above-described configuration, in the melting step, the mixed liquid of the solid raw material and the aqueous alkaline solution is continuously charged into a fluid disk type dissolver having a multistage rotating disk inside, and the multistage rotation in the dissolver is performed. It can be carried out while stirring sequentially with a disk.

  Note that the zeolite synthesis reaction can also be carried out while continuously stirring the solution in a fluidized rotary disk reactor equipped with a multistage rotating disk inside and sequentially stirring with the multistage rotating disk in the reactor.

  Here, the fine-grained zeolite refers to a synthetic zeolite having a maximum particle size of 20 μm or less measured with a laser diffraction / scattering particle size distribution measuring device (model LA-920 wet type) manufactured by Horiba, Ltd.

  The present invention is as described above. According to the present invention, the solid raw material is mixed with an alkaline aqueous solution and heated, and then the silica and / or alumina components contained in the raw material are sufficiently dissolved and then suitable for the reaction. Since the auxiliary material is added after adjusting the temperature, the synthesis efficiency of the zeolite is increased compared with the case where the auxiliary material is added in a state where the silica and / or alumina components in the raw material are not sufficiently dissolved in the alkaline aqueous solution. The effect that it can be obtained. Moreover, since a high-performance zeolite of a desired type (A type, X type, Y type) can be continuously synthesized from a solid raw material, the production cost is low and the performance is also synthesized from conventional industrial raw materials. It is comparable to and extremely useful.

  Furthermore, in the present invention, heavy metals are removed at the stage of raw materials before mixing with an alkaline aqueous solution, so that the field of use of zeolite products can be used in large quantities and safely in large-scale fields such as agricultural soil improvement and drainage water purification. It is possible to obtain an excellent effect that it can contribute to the achievement of a recycling-oriented environmental society.

  Furthermore, in the present invention, by adjusting the rotational speed of the rotating disk in the fluidized rotating disk reactor, stirring and mixing of the raw material component solution can be performed without back mixing, and sufficient catalytic reaction is performed. Therefore, there is an effect that a high-purity product can be obtained.

In addition, in the present invention, the reaction recovery solution recovered after the zeolite synthesis reaction is used again as a part of the alkaline aqueous solution, and the components which are insufficient due to the appropriate addition of SiO ₂ source, Al ₂ O ₃ source and Na ₂ O source A type, X type and Y type fine-grained zeolite can be synthesized continuously, so that these fine-grained zeolites can be mixed with concrete to improve fluidity and reduce the moisture content of the concrete. The effect that it can be used for the production of coating raw materials having the deodorizing effect in the house, the countermeasure against sick house, and the humidity control effect is obtained. Furthermore, it can also be used to manufacture raw materials having paper, cloth folding, deodorization and humidity control effects.

  Next, an embodiment of the present invention will be described with reference to the drawings. FIG. 1 is a flowchart of an example synthesis process of the present invention, FIG. 2 is a flowchart of an example of a heavy metal removal process from a solid material, and FIG. 3 is a block diagram of an example of an apparatus for carrying out the continuous synthesis method of the present invention. 4 is a cross-sectional view showing the internal structure of the flow rotating disk reactor in the apparatus shown in FIG. 3, FIG. 5 is an enlarged view of the rotating disk of the flow rotating disk reactor of FIG. 4, (a) is a bird's eye view, ( b) is a cross-sectional side view, FIG. 6 is an A-type single crystal synthesis X-ray analysis diagram from coal ash, FIG. 7 is an X-type single crystal synthesis X-ray analysis diagram from coal ash, and FIG. It is a Y-type single crystal synthetic | combination X-ray-analysis figure.

FIG. 1 is a flow chart showing an example of a synthesis process of the present invention, through a heavy metal removal process (part surrounded by a wavy line) from a solid raw material, a mixing process of a solid raw material from which heavy metals have been removed and an alkaline aqueous solution, and a heating process. After the silica and alumina components contained in the solid raw material are sufficiently dissolved in the alkaline aqueous solution in the dissolving step, the temperature is adjusted to a temperature suitable for the reaction temperature, and the SiO ₂ source and the Al ₂ O ₃ source as auxiliary materials are added. The zeolite synthesized through the continuous reaction step, the cooling step, and the solid-liquid separation step is recovered. By providing the above-described dissolution step, the synthesis rate of zeolite was able to be increased to 51%, which was about 21% in the case of Type A. The remaining reaction recovery liquid is reused as part of the alkaline aqueous solution, but the reaction recovery liquid can be returned to the reaction process, returned to the dissolution process, or returned to the raw material mixing process. Further, when returning the reaction recovery liquid, a deficient SiO ₂ source, Al ₂ O ₃ source and Na ₂ O source are appropriately added and replenished.

  Next, an example of the process of removing heavy metals from the solid raw material will be described with reference to FIG. In this heavy metal removal step, after mixing the solid raw material, here coal ash, with the aqueous acid solution in the mixing tank, it is supplied to the stirring dissolution tank by the pump P, and the heavy metal is eluted into the aqueous acid solution while stirring and mixing. Continuously supply to the filter to separate the heavy metal eluate, discriminate the heavy metal elution concentration of the separated eluate and discard the one with a predetermined concentration or higher, and return the one with the predetermined concentration or lower to the preparation tank. An acid is added for recycling. In addition, it can also be set as the structure which does not provide a circulation process. Moreover, one mixing stirring dissolution layer (not shown) which combines mixing and stirring dissolution can also be used.

  FIG. 3 shows an example of an apparatus for carrying out the continuous synthesis method of the present invention. FIG. 3 shows the main raw material, which is a solid raw material from which heavy metals have been removed in the heavy metal removal step shown in FIG. 2, wherein 1 is a raw material mixing tank for mixing the main raw material with an alkaline aqueous solution, 1a is this raw material mixing tank 1 is a motor for rotating the stirring blade 1a, 2 is a raw material mixed liquid mixed in the raw material preparation tank 1, heated by a heating device Q, and then silica and / or contained in the solid raw material Alternatively, it is a fluid rotary disk type dissolver for dissolving the alumina component. Reference numeral 2a denotes a rotating disk provided in multiple stages in the melter 2 at appropriate intervals in the vertical direction, and 2b is a rotating shaft that supports these rotating disks 2a at the center thereof, and is rotated by a motor 2c. The rotating disk 2a is rotated. The rotation speed of these rotary disks 2a can be adjusted to a predetermined speed by the motor 2c. In FIG. 3, symbol P indicates a pump for sending the mixed solution from the raw material preparation tank 1 to the heating device Q, a pump for sending the auxiliary raw material from the auxiliary raw material tanks S1 and S2, and other pumps. Moreover, in FIG. 3, the code | symbol M has shown the motor for rotating the stirring blade C when stirring a raw material, an auxiliary material, and a product in a tank. Further, as the dissolver, in addition to the fluidized rotary disk dissolver 2 described above, although not shown, a continuous contact tube dissolver or the like can also be used.

3, after adjusting the slurry-like raw material mixture in which the silica and / or alumina components are sufficiently dissolved in the fluid rotating disk type dissolver 2 to a temperature suitable for the reaction in the heat exchanger 4, the SiO ₂ source as a secondary raw material , A fluidized rotary disk reactor for continuously charging and reacting a raw material component solution added with an Al ₂ O ₃ source. The structure of the fluid rotary disk reactor 3 is substantially the same as that of the fluid rotary disk dissolver 2, and 3a is a rotary disk provided in multiple stages in the reactor 3 at appropriate intervals in the vertical direction. , 3b is a rotating shaft that supports these rotating disks 3a at the center thereof, and is rotated by a motor 3c to rotate the rotating disks 3a. The rotational speed of these rotary disks 3a can be adjusted to a predetermined speed by the motor 3c. Adjustment of the rotation speed of the rotating disk 3a, prevention of back mixing and control of reaction time by the dimensions, shape and number of stages of the rotating disk 3a and inner tray 3d, synthesis of zeolite corresponding to each type, and corresponding to each type The synthesis rate of zeolite can be changed. The internal structures of the fluid rotary disk type dissolver 2 and the fluid rotary disk type reactor 3 will be described in detail later.

The heat exchanger 4 for adjusting the reaction temperature provided between the fluidized rotary disc type dissolver 2 and the fluidized rotary disc type reactor 3 is prepared by using the raw material mixture from the fluidized rotary disc type dissolver 2 as follows: The temperature is lowered to a temperature suitable for the reaction. Here, the temperature is cooled in the cooler 5 connected to the synthesized zeolite outlet ZT of the fluidized rotary disk reactor 3 and separated in the solid-liquid separator 6. The temperature is lowered by exchanging heat with the recovered reaction solution. The temperature adjustment varies depending on the type of zeolite to be synthesized. Since heat is recovered by raising the temperature of the reaction recovery liquid in the heat exchanger 4, it is possible to effectively use heat resources. The type of zeolite to be synthesized is also related to the composition ratio of SiO ₂ / Al ₂ O ₃ in the raw material component solution, as will be described later. Incidentally, the temperature can be adjusted by adjusting the flow rate and flow rate of the raw material mixture when passing through the heat exchanger 4, and can also be performed by bypassing the raw material mixture by a bypass. it can. The zeolite mold to be synthesized is fixed by cooling in the cooler 5, for example, by cooling to room temperature.

  The cooler 5 described above is for cooling the zeolite synthesized by the reaction in the fluidized rotary disk reactor 3 to a temperature at which the synthesis does not proceed rapidly. Although not shown, a pressure control valve is provided to keep the pressure of the reaction system in the synthesis apparatus described above constant. By operating this pressure control valve, the pressure in the reaction system is kept constant, The liquid is prevented from evaporating due to boiling, and vapor lock (flow adhesion) due to evaporating.

Next, since the internal structures of the fluid rotary disk type dissolver 2 and the fluid rotary disk type reactor 3 are substantially the same, the internal structure of the fluid rotary disk type reactor 3 will be described with reference to FIG. In FIG. 4, the flow rotating disk reactor 3 includes a multi-stage rotating disk 3a, a rotating shaft 3b that horizontally supports these rotating disks 3a at appropriate intervals in the vertical direction, a motor 3c that rotates the rotating shaft 3b, It is composed of an inner tray 3d provided between each rotating disk 3a and projecting in a ring shape from the inner surface of the fluid rotating disk reactor 3, and is composed of a high-performance zeolite of A type, X type or Y type. Prevents back mixing and controls reaction time. In FIG. 4, RT is a continuous inlet for the zeolite raw material component solution, and ZT is an outlet for the synthesized zeolite. As shown in FIG. 5, the rotating disk 3a is preferably provided with a plurality of baffles j and protrusions t at arbitrary positions as required, and the inner tray 3d has a fluidized rotating disk reactor. It is preferable to make the attachment part to 3 into R shape. In FIG. 4, the upper and lower portions of the mounting portion of the inner tray 3d are formed in an R shape. However, as shown in FIG. 5, the R shape may be provided only in the upper portion or may be provided only in the lower portion. Moreover, it is preferable that the attachment part of the rotating disk 3a to the rotating shaft 3b is also R-shaped (see FIGS. 4 and 5). The b shape of the baffle plate j and the projection t of the rotating disk 3a and the R shape of the mounting portion of the inner tray 3d can further improve the back mixing preventing action. An inner tray 2d having an R-shaped mounting portion is also provided in the fluid rotating disk type dissolver 2 (see the inner tray 3d having an R-shaped mounting portion in the fluid rotating disk reactor 3 in FIGS. 4 and 5). The rotating disk 2a is provided with a baffle plate j and a protrusion t, which together promote the dissolution of the SiO ₂ and Al ₂ O ₃ components in the raw material in the alkaline aqueous solution. it can.

Thus, the zeolite has a dissolution process in which the SiO ₂ source and Al ₂ O ₃ source in the raw material are dissolved in an alkaline aqueous solution, a precursor generation prior to zeolite crystallization, and a crystallization / crystal growth process of the zeolite. Sequentially synthesized without mixing. By the way, when the above steps are mixed, backmixing occurs and synthesis of the zeolite stops, and a predetermined zeolite is not synthesized, so that P-type zeolite and finally sodalite or an analcyme crystal are synthesized. The present invention suitably prevents the occurrence of backmixing by the fluidized rotating disk type dissolver 2 and the fluidized rotating disk type reactor 3, and controls the reaction temperature, time, composition, and stirring speed that are adjusted in advance, A-type, X-type, and Y-type zeolites can be synthesized.

  The continuous synthesis method of the high-performance zeolite from the solid raw material of the present invention is carried out in the above-described example of the synthesis apparatus. At the start of operation of this apparatus, an alkaline aqueous solution is introduced and the inside of the apparatus system is circulated. Ensure that the temperature is necessary for the synthesis operation. When the inside of the apparatus system reaches a predetermined temperature, the raw material mixture is heated and then introduced into the dissolution step to start the zeolite synthesis operation.

Hereinafter, the flow of the synthesis process will be described in order. In the raw material blending tank 1, coal ash, which is industrial waste, is used as a solid raw material in the alkaline aqueous solution having a predetermined concentration, and is sufficiently stirred and mixed. At this time, a seed crystal of any of A type, X type, and Y type corresponding to the type of zeolite to be synthesized is added. Next, in the heating device Q, the raw material mixture is heated to 85 ° C. to 140 ° C., preferably 85 ° C. to 120 ° C., and then continuously charged into the fluidized rotary disk dissolver 2 while stirring with the rotary disk 2a. The SiO ₂ and Al ₂ O ₃ components contained in the coal ash are sufficiently dissolved in the alkaline aqueous solution.

  Then, after adjusting the raw material mixture from the fluid rotary disk type dissolver 2 to a temperature (80 ° C. to 120 ° C.) suitable for the reaction in the heat exchanger 4, the raw material mixture line immediately before the fluid disk type reactor 3 Together with the auxiliary material supplied from the auxiliary material supply line L from the connected auxiliary material tank S, it is continuously charged into the fluidized rotary disk reactor 3. The auxiliary material can also be added directly to the fluid disk reactor 3. In this case, water glass, sodium aluminate or drainage liquid containing aluminum and / or silica is put in the auxiliary material tank S as an auxiliary material.

  In the fluid disk reactor 3, the raw material component solution that has been continuously charged is moved from its central portion to the inner peripheral wall side of the reactor 3 by the rotating upper rotating disk 3 a and at the lower stage by the inner tray 3 d. Since this movement is repeated from the upper stage to the lower stage of the rotating disk 3a, it is moved to the center side of the rotating disk 3a, so the raw material component solution reacts sufficiently during the movement, and the zeolite precursor Formation and single crystal growth can be generated with high efficiency. In addition, by adjusting the rotation speed of the rotating disk 3a, the stirring and mixing of the zeolite raw material component solution can be performed without back mixing, and a sufficient contact reaction can be performed. And the reaction can be carried out continuously.

  The zeolite produced in the fluidized disk reactor 3 is taken out and sent to the cooler 5 where the desired type of zeolite is synthesized at a temperature below which synthesis does not proceed rapidly. In order to prevent solidification in the apparatus system when the synthesis apparatus is stopped, the soda is replaced at once.

  Next, the raw material components used in the present invention will be described. In the embodiment of the present invention, since coal ash is used as a solid raw material as described above, the synthesis rate of zeolite is further improved, and In order to further shorten the synthesis time, the coal ash is pretreated, specifically, pulverized or classified. In the pulverization, it is preferable that the coal ash has an average particle diameter of 10 μm or less, and 30 μm or more is 1% or less of the whole. Classification is preferably performed at 45 μm, preferably 25 μm, and the particles are synthesized with the smaller one.

Thus, for the synthesis of zeolite, four kinds of compounds of SiO ₂ , Al ₂ O ₃ , Na ₂ O, and H ₂ O are required. Coal ash contains SiO ₂ and Al ₂ O _3, but the amount of components does not match the proportions required for the synthesis of A-type, X-type, and Y-type zeolites, depending on the type of zeolite being synthesized. , SiO ₂ or Al ₂ O ₃ is insufficient, and one of them becomes surplus as an unreacted component. In order to use this unreacted portion for the synthesis of zeolite, the auxiliary raw material is added to supplement the shortage. The auxiliary material may be either solid or liquid. The components that are insufficient when producing each type of zeolite based on coal ash are Al ₂ O _{3 in} the case of Type A and Al ₂ O ₃ or SiO _{2 in} the case of Type X (in the coal ash). (Depending on the content of SiO ₂ ) becomes an insufficient component, and in the case of the Y type, SiO ₂ becomes an insufficient component.

As an auxiliary material to be used, as an SiO ₂ source, for example, industrial raw materials containing SiO ₂ such as water glass, natural raw materials containing SiO ₂ such as diatomaceous earth, papermaking sludge incineration ash, rice husk incineration ash, etc. Solid raw materials such as industrial waste containing SiO ₂ can be mentioned.

Further, as an Al ₂ O ₃ source, for example, industrial raw materials containing Al ₂ O ₃ such as sodium aluminate, aluminum hydroxide, aluminum dross, red mud, aluminum can, aluminum processing waste liquid, aluminum processing sludge, etc. And solid raw materials such as industrial waste containing Al ₂ O ₃ .

Zeolite is synthesized by mixing and reacting the above main raw materials and auxiliary raw materials in an aqueous alkali solution of a prescribed concentration, and the raw materials for the aqueous alkali solution include, for example, industrial raw materials containing Na ₂ O such as sodium hydroxide and sodium carbonate. And industrial waste containing Na ₂ O such as various types of waste soda. In the above apparatus, continuous synthesis of zeolite is started, and the reaction recovery liquid separated in the solid-liquid separation apparatus 6 after the synthesis can be reused as a part of the alkaline aqueous solution. Since the recovered liquid contains silica and alumina components, fine zeolite with fine particles can be synthesized by reacting the recovered liquid again. As shown in FIG. 1, when the reaction recovery liquid separated into solid and liquid is reused, it can be directly returned to the reaction process (fluid rotating disk reactor 3), and the dissolving process (fluid rotating disk dissolver). It is also possible to return to 2). Moreover, it can also return to the mixing process (raw material preparation tank 1) of the main raw material. Further, the fine zeolite is preferably recovered with a fine solid-liquid separator.

Next, in an example of an apparatus for performing the continuous synthesis method of the present invention, as shown in FIGS. There is a heavy metal removal process to separate heavy metal eluate after eluting heavy metal into acid aqueous solution without losing silica and / or alumina components which are active ingredients in the raw material. To explain again the significance of this, the zeolitic technology has already been established as a method for recycling coal ash and other resources. It is well known that aqueous solutions such as hydrochloric acid are effective for eluting heavy metals contained in solids. To produce zeolite using coal ash as a raw material, SiO, which is the active ingredient in coal ash, is used. It is important to keep the conditions such as ₂ and Al ₂ O ₃ in the solid and to elaborate heavy metals as much as possible to find the conditions for economical production of high quality zeolite. As described above, heavy metals have been removed by acid in the past, but the conventional method elutes the silica and alumina components required for zeolite synthesis contained in coal ash, etc. Concentration adjustment is extremely important.
In the present invention, coal ash or the like is added to 0.1 mol / l or more hydrochloric acid in a mixing tank to adjust the solid-liquid ratio to 3 to 30 w / v%, and the slurry is sent to a fluid rotating disk type dissolver, at room temperature or higher. The heavy metals are eluted in a temperature range of 0.5 to 3 hours. By using a fluidized rotating disk type dissolver, heavy metals can be effectively eluted while avoiding severe stirring and preventing extreme destruction of particles. The treated coal ash and the like can be drained with a filter, made into a cake state, recovered in the raw material preparation tank 1, and used as a zeolite raw material. The elution of heavy metals in zeolite synthesized from acid-treated coal ash, etc., has cleared the elution standards (= environmental standards) related to the Soil Contamination Countermeasures Law, and does not cause environmental pollution. It has the potential to open up a wide range of applications such as soil improvement in relations.

  Heavy metals to be removed in the present invention are cadmium, lead, hexavalent chromium, arsenic, mercury, selenium, fluorine, boron and the like. Table 1 below shows the results of heavy metal elution experiments in which coal ash was washed with a 1 mol hydrochloric acid aqueous solution.

  Next, the constituent ratios of the main raw material, auxiliary raw material, alkali component, and water are prepared in molar ratios as shown in the following Table 2 for each zeolite type. In order to shorten the synthesis time, it is preferable to age the prepared main raw material, auxiliary raw material and alkaline aqueous solution at 80 ° C. or lower for 6 hours or longer.

Further, in order to shorten the synthesis time, it is more preferable to add zeolite synthesized as seed crystals to the prepared main raw material, auxiliary raw material and alkaline aqueous solution in the ratio shown in Table 3 below. In addition, the zeolite used as a seed crystal can use the zeolite from a commercial industrial raw material, or the fine-grained zeolite synthesize | combined by this invention.
Further, it is more preferable to add the zeolite to be added after aging it at room temperature or 80 ° C. or less in an alkaline aqueous solution prepared in advance.

Next, the zeolite synthesis conditions in the synthesis apparatus for carrying out the present invention will be described.
(1) Flow velocity of the main raw material, auxiliary raw material, and aqueous alkaline solution prepared during synthesis in the apparatus Keep the flow speed at 0.3 m / sec or more so that coal ash does not settle in the piping in the apparatus. When coal ash is pulverized, the flow rate can be increased to 0.2 m / second or more.
(2) Heating temperature in the heating device In the case of a solid raw material containing both silica and alumina components, it is 70 ° C to 120 ° C, preferably 80 ° C to 105 ° C. If only one of silica and alumina is contained, the upper limit temperature is further increased to 150 ° C. It may be raised to about ° C. For solid raw materials that are easily dissolved in alkali, the temperature may be lowered from 50 ° C. to about 60 ° C.
(3) Dissolution time in a fluid rotating disk type dissolver When both the silica and alumina components are included, a short time is required when the temperature is high and a long time when the temperature is low in order to prevent the formation of stable low-grade zeolite. Dissolve with.
When the temperature is 80 ° C. to 105 ° C., the dissolution time is 105 ° C., preferably 20 minutes to 1 hour, and when 80 ° C., the dissolution time is preferably 1 hour to 5 hours.
(4) Number of revolutions of the rotating disk in the fluidized rotating disk reactor The rotating disk is adjusted so that the flow of the raw material prepared in the fluidized rotating disk reactor changes from 10 5 to 10 6 in Reynolds number. Rotate. Preferably, the rotational speed is such that the Reynolds number is 50,000 to 250,000.
Here, the equation of the modified Reynolds number (N _Re ) including the rotational speed is as follows.
N _Re = nDi ² ρ / μ
n: Number of revolutions (rps)
Di: Diameter of stirring blade (m)
ρ: Liquid density (kg / m3)
μ: Liquid viscosity (kg / m · sec)
In the case of a fluid rotary disk reactor, Di is the diameter of the rotary disk.
(5) Temperature suitable for synthesis (temperature control)
Zeolite type, 90 ° C to 105 ° C in the case of A type, preferably 98 ° C to 102 ° C, 85 ° C to 100 ° C in the case of X type, preferably 85 ° C to 98 ° C, 85% in the case of Y type ° C to 105 ° C.
(6) Synthesis time In the case of zeolite type A, it is 1 hour to 3 hours, preferably 2 hours to 3 hours, and in the case of form X, it is 2 hours to 6 hours, preferably 3 hours to 4 hours. In the case of Y type, it is 2 hours to 6 hours, preferably 3 hours to 4 hours.
(7) Cooling temperature The cooling temperature in the cooler 5 is 80 ° C. or lower in any of the A type, the X type, and the Y type, and the cooling is performed to fix the type of the produced zeolite.

  Next, examples of the present invention will be described. The blending ratio of each type of raw material for producing zeolite is shown in Table 4 below.

  Next, Table 5 shows the synthesis conditions for each type of zeolite synthesis raw material.

  As a result of X-ray analysis of the zeolite synthesized in the above examples, synthesis of A, X, and Y types was confirmed. These analysis results are shown in FIG. 6 as an A-type single crystal synthesis X-ray analysis diagram from coal ash, FIG. 7 as an X-type single crystal synthesis X-ray analysis diagram from coal ash, and FIG. Type single crystal synthetic X-ray analysis diagrams.

In the above embodiment, coal ash is used as the solid raw material. Among them, fly ash having a small particle size is preferable, and if the component contains silica and / or alumina, sewer sludge other than coal ash is used. Incineration ash, diatomaceous earth, rice husk ash, waste incineration ash, etc. can be used. Sludge incineration ash and the like are preferable because they contain a large amount of silica and alumina components. Diatomaceous earth, fir shell incineration ash, etc. contain a lot of silica components. Some of these solid materials are mixed and used in cement, etc., but most of them are disposed of as a solid material in a managed landfill, and industrially effective high-performance zeolite can be obtained from these solid materials. It is very preferable from the viewpoint of environmental problems. When used as a solid raw material other than coal ash, the ratio of the silica component and alumina component contained is different from that of coal ash, so the addition ratio of secondary raw materials (SiO ₂ source, Al ₂ O ₃ source) is also Depends on the solid raw material.

  The present invention can continuously and inexpensively produce high-performance zeolite (A type, X type, Y type) from which heavy metals have been removed to a level that satisfies environmental standards by using a solid raw material, and is also used in agriculture. It can be used in large-scale fields such as soil improvement and drainage water purification, contributing to the achievement of a recycling-oriented environmental society.

The flowchart of the synthetic | combination process of an example of this invention. The flowchart of an example of the heavy metal removal process from a solid raw material. The block diagram of an example of the apparatus which implements the continuous synthesis method of this invention. Sectional drawing which shows the internal structure of the fluid rotation disc type reactor in the apparatus of FIG. FIG. 5 is an enlarged view of a rotating disk of the fluidized rotating disk reactor of FIG. 4, (a) is a bird's eye view, and (b) is a side view shown in cross section. A-type single crystal synthesis X-ray analysis diagram from coal ash. X-type single crystal synthesis X-ray analysis diagram from coal ash. Y-type single crystal synthesis X-ray analysis diagram from coal ash.

Explanation of symbols

1 Raw material mixing tank
1a stirring blade
1b Motor 2 Flowing disk type dissolver
2a rotating disc
2b Rotating shaft
2c Motor 3 Fluidized rotary disk reactor
3a rotating disk
3b Rotation axis
3c motor
3d Inner tray 4 Heat exchanger for adjusting reaction temperature 5 Cooler 6 Solid-liquid separator Q Heater j Baffle plate t Projection

Claims (5)

A method of synthesizing zeolite from a solid raw material containing silica and / or alumina by an alkaline hydrothermal reaction , which is necessary for mixing the raw material with an alkaline aqueous solution and promoting dissolution in the heating step before the zeolitic reaction. was heated to a temperature, after promoting dissolution of silica and / or alumina component in the dissolution step, cooling the solution a type, X type, to a temperature suitable for synthesis of the Y-type one type of zeolite after the cooling, by adding a SiO ₂ source and / or Al ₂ O ₃ source and a given type of seed zeolite required to obtain a composition that is suitable for synthesis of the zeolite, depressive example side reactions a method for synthesizing a zeolite with a high synthesis rate, the solid material was stirred and mixed with an aqueous solution of an acid prior to mixing with the alkaline aqueous solution, cadmium contained in the solid material, lead, 6 Elution of at least one removal component selected from chromium, arsenic, mercury, selenium, fluorine, and boron into an aqueous acid solution without losing silica and / or alumina components, which are active components in the solid raw material. Then, a removal step for separating the removed component eluate is provided. In the removal step, the solid raw material is prepared with an acid aqueous solution in a preparation tank, and the removed component is eluted into the acid aqueous solution while being stirred and mixed. Continuously supply to the vessel to separate the removed component eluate, determine the removed component elution concentration of the separated eluate, discard the one with a predetermined concentration or higher, return the one with the predetermined concentration or lower to the preparation tank and return the acid A method for continuously synthesizing a high-performance zeolite comprising a step of adding and circulating .   The method for continuously synthesizing highly functional zeolite according to claim 1, wherein the reaction recovery liquid after synthesis of zeolite is used as a part of an alkaline aqueous solution to synthesize fine-grained zeolite. Continuous process for the synthesis of high performance zeolite of claim 2 wherein the addition of SiO ₂ source and Al ₂ O ₃ source and Na ₂ O source into the reaction recovery liquid. The melting in the melting step is performed while continuously mixing a mixed solution of a solid raw material and an aqueous alkali solution into a fluid disk type dissolver having a multistage rotating disk therein and sequentially stirring with the multistage rotating disk in the dissolver. either a continuous process for the synthesis of high-performance zeolite to 3. Zeolite synthesis reaction, the solution to flow a rotary disk type reactor having a multi-stage rotary disk sequentially fed inside, the claim 1-4 carried out while successively stirred by a multistage rotary disk of the reactor Continuous synthesis method of high-performance zeolite.

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