KR101600074B1

KR101600074B1 - Apparatus and method for manufacturing multiple odor absorbents

Info

Publication number: KR101600074B1
Application number: KR1020150117179A
Authority: KR
Inventors: 박진희; 문장수; 홍권일; 김재철
Original assignee: 동원중공업 주식회사
Priority date: 2015-08-20
Filing date: 2015-08-20
Publication date: 2016-03-04

Abstract

The present invention relates to a device for producing a granular composite odor adsorbent and a method for producing a complex odor adsorbent using the same, wherein the composite odor adsorbent is composed of ammonia, trimethylamine and the like, which are generated from food waste and cause odor, It has an excellent effect in adsorbing and removing hydrogen sulfide and methyl mercaptan. In addition, in the production of the composite odor adsorbent, a granular raw material having a uniform and high density can be formed through a molding apparatus, granular raw materials can be produced in a large capacity by continuous molding, It is possible to prevent the granular form breakage and to prevent the clogging of the screen by drying only the fine powder after drying the surface and the fine powder in the drying and firing apparatus and to burn the granular raw material in which the fine powder is removed at the time of firing It eliminates the rotation resistance caused by the differential and improves the product quality through efficient firing and has energy saving effect.

Description

TECHNICAL FIELD [0001] The present invention relates to an apparatus for producing a complex odor adsorbent and a method for producing the same,

The present invention relates to an apparatus for producing a complex odor adsorbent and a method for producing a complex odor sorbent using the same, and more particularly, to a method for producing a complex odor sorbent by mixing natural zeolite, ash, yellow earth, bentonite, sodium hydrogencarbonate, And a method for producing a complex odor adsorbent using the same.

Recently, due to changes in the perception of environmental rights, odor problems are becoming serious as well as air pollution. Since Korea has a mixed population of residential area and industrial area for efficient use of the limited land area, the incidence of odor complaints is very high due to high population density, and there are many difficulties in efficient management due to the variety of types and sources of odorous substances .

In addition to the large number of substances causing these odors, it is difficult to uniformly express the extent of the damage or the degree of damage due to the complex action of odorous substances or individual differences in the smell, which is the most difficult and difficult to solve It is considered to be one of the problems. Odor is one of the sensory pollution causing mental and psychological damage rather than the harmfulness to the human body. Recently, the quality of life and environmental consciousness have improved, and civil complaints are increasing every year. The damage caused by the odor is mainly limited to the vicinity of the source, but it can affect far distances depending on the weather conditions, such as wind direction, wind speed, and temperature inversion, as well as the local features of the area.

In Korea, the amount of food waste generated due to the traditional food culture has raised the need for management measures. Among them, we are trying to use food waste as a resource as much as possible.

Food waste is discharged every day from households and restaurants. The amount of such garbage is gradually increasing from 13,672 tons / day in 2010 to 13,537 tons / day in 2011 and 13,209 tons / day in 2012. Food waste It has a different composition and content, and its protein content is relatively high in terms of nutrient composition. It has a useful value as feed and compost, but it has a high water content and is easily corrupted and malodorous. Therefore, when disposing of food waste, damage is increasing due to odor such as incessant complaints around environment basic facility due to odor generated.

Food waste recycling facilities, one of the abovementioned environmental facilities, have introduced waste disposal agents since 1995 and the amount of food waste has been rapidly increasing due to the separation and discharge of food waste mixed and discharged into the standard bags. It started to be installed in the room. However, this food waste disposal facility has been recognized as a disgusting facility due to the severe odor generated during transportation and processing of food waste, and it has become a subject of complaints of residents in the surrounding area, resulting in NIMBY ('Not In My BackYard') phenomenon. In the process, malodorous substances such as mercaptans, amines and the like are generated, causing discomfort and disgust to the residents in the surrounding area, making them subject to collective complaints, and it is difficult to install and operate a food waste recycling facility.

Patent Document 1 discloses a method of adsorbing an alkaline gas such as ammonia (NH ₄ ), an acid gas such as hydrogen sulfide (H ₂ S), etc. at the same time, Since the malodor gas adsorbed at a low temperature of about 200 ° C. after the malodorous gas is sufficiently adsorbed can be regenerated by oxidative decomposition or desorption, it is possible to continuously use the malodorous gas-adsorbed oxidative decomposition and its manufacturing method have.

However, in order to form the adsorbent in the form of granules, it is troublesome to dry only the granules in the form of granules, to separate only the granules through the screen, and to transfer the remaining powder back to the molding machine. In order to increase the density of the granules, Since the process must be stopped and additional raw materials should not be added, the process must be operated in a bath type and the granules generated after the molding process must be dried and calcined together with the unnecessary energy There is a problem that it is consumed.

Published Japanese Patent Application No. 2001-0000418 (published on January 01, 2001)

In the present invention, an adsorbent containing natural zeolite, ash, loess, bentonite and sodium hydrogencarbonate is prepared in order to remove the odor generated from food waste, and thereby, mercaptan such as ammonia, trimethylamine, The adsorbent of the present invention is capable of adsorbing odor and removing odor in a complex manner.

In addition, it is possible to form granules continuously in the granular form at the time of manufacturing the granular raw material, thereby making it possible to produce a large-capacity granular adsorbent, no separate powder separation process is required, and the angle of the molding device can be easily controlled To provide an apparatus for producing a complex odor adsorbent having excellent energy efficiency by producing a uniform and high-density granular raw material through a molding apparatus, drying only the surface of the granular raw material, and then separating the fine powder to prepare an adsorbent do.

According to an aspect of the present invention, there is provided a raw material mixing apparatus (100) for mixing and uniformly supplying a raw material; A forming device 200 for forming a granular material having a uniform size by rotating the mixed raw materials at different positions depending on the particle size, A drying and firing apparatus 300 for removing fine powder contained in the granular raw material, drying and firing the powder to produce an adsorbent; And a screen crushing apparatus 400 for screening only the predetermined size of the prepared adsorbent and discharging the adsorbent having a size below the reference value to the outside to crush the screen, wherein the drying and firing apparatus 300 includes a downward inclined And a differential separator 320 for separating the fine particles contained in the granular raw material in the cylindrical rotary dryer 300. The separator 320 includes a drying unit 310 and a firing unit 330 ). &Lt; / RTI >

The molding apparatus 200 includes a rotating body 210 that includes a binder in the mixed raw material and forms a granule by aggregating while rotating the mixed raw material, a jetting unit 260 A scraper 250 disposed inside the rotating body 210 to rotate at different positions according to the size of the granule shape and a rotating body 210 rotating with the rotating body 210 and rotating the rotating body 210, And a control unit for controlling the time and the injection amount. The rotating body 210 includes an inclined disk 211, a dam 212 formed vertically to the rim of the disk 211 to prevent the granular material having a reference size or less from being discharged to the outside, And a loop part 213 provided at the upper end of the granular material 212 for rolling the granular raw material.

The differential separating unit 320 may separate fine particles contained in the granular raw material through a cylindrical rotating screen including a plurality of perforated holes.

The screening and crushing apparatus 400 includes a screening unit for selectively discharging only a predetermined size of an adsorbent and a crushing unit for crushing an adsorbent having a sub-standard size that has not passed through the screening unit and delivering the adsorbent to the granulation apparatus 200 .

Another embodiment of the present invention is a process for producing a raw material mixture comprising: a raw material mixing step of uniformly mixing raw materials including natural zeolite, Ash, loess, bentonite and sodium hydrogencarbonate (NaHCO3); Molding the mixed raw material into a granule form through a molding apparatus 200; A drying and calcining step of drying and firing the granules-shaped raw material to produce an adsorbent; And a crushing step of crushing the produced adsorbent by feeding the adsorbent to the screening crusher 400 to select only a predetermined size and discharging the adsorbent having a smaller size than the remaining standard to the outside, A drying step of applying heat to the raw material to remove moisture on the surface of the granules; A fine particle removing step of passing the raw material, which has been granulated through the drying step, through a rotating screen including a perforation hole to remove fine particles; And a firing step of applying heat to the raw material from which the fine particles have been removed.

Preferably, 20 to 25 parts by weight of ash, 4 to 7 parts by weight of loess, 1 to 3 parts by weight of bentonite and 13 to 16 parts by weight of sodium hydrogencarbonate are uniformly mixed with 100 parts by weight of natural zeolite Do.

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The present invention relates to an apparatus for producing a complex odor adsorbent and a method for producing a complex odor sorbent using the same, wherein the complex odor sorbent comprises ammonia, trimethylamine, and the like, which are generated from food waste, There is an excellent effect to adsorb and remove methyl mercaptan.

In addition, in the production of the composite odor adsorbent, a granular raw material having a uniform and high density can be formed through a molding apparatus, and granular raw materials can be produced in a large capacity by continuous molding. Further, only the granular raw material having a size larger than the reference size is discharged to the outside, so that a separate powder separation process is not required, and the granular raw material having a predetermined size or more is separated from the powder raw material, The granular adsorbent can be produced.

The granule type raw material is dried and fired in a drying and firing apparatus to separate only fine powder to prevent breakage of the granule type and to prevent clogging of the screen. In firing, granule type raw material It is possible to reduce the rotational resistance caused by the fine powder and improve the quality of the product through efficient firing and to save energy.

1 is a schematic view schematically showing an apparatus for producing a complex odor adsorbent of the present invention.
2 is a schematic diagram schematically showing a molding apparatus according to an embodiment of the present invention.
3 is a schematic view schematically showing the molding principle of a molding apparatus according to an embodiment of the present invention.
4 is a schematic view schematically showing a drying and firing apparatus according to an embodiment of the present invention.
FIG. 5 is a schematic view showing the particle state of granular raw material and fine powder while passing through the drying and firing apparatus according to an embodiment of the present invention.

DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENTS The preferred embodiments of the present invention will now be described in detail with reference to the accompanying drawings. Hereinafter, preferred embodiments of the present invention will be described in detail with reference to the accompanying drawings. As well as the fact that

Throughout this specification, when a member is "on " another member, this includes not only when the member is in contact with another member, but also when there is another member between the two members.

Throughout this specification, when an element is referred to as "including" an element, it is understood that it may include other elements as well, without departing from the other elements unless specifically stated otherwise.

In each step, the identification code is used for convenience of explanation, and the identification code does not describe the order of the steps, and each step may be performed differently from the stated order unless clearly specified in the context. have. That is, each of the steps may be performed in the same order as the specified order, substantially simultaneously or in the opposite order.

Also, throughout this specification, the reference size means a predetermined arbitrary size and can be changed as needed in the production of the adsorbent.

Hereinafter, preferred embodiments of the present invention will be described in detail with reference to the drawings.

FIG. 1 is a schematic view schematically showing an apparatus for producing a complex odor adsorbent according to an embodiment of the present invention. The apparatus for producing a complex odor adsorbent includes a raw material mixing apparatus 100 for uniformly mixing raw materials supplied thereto, (200) comprising a binder in the raw material and rotating the granules at different positions according to the size of the granules to form granules of a uniform size, removing the fine particles contained in the granular raw material, And a screen crushing apparatus 400 for screening only the predetermined size of the prepared adsorbent and discharging the adsorbent having a size below the remaining standard to the outside to crush the screen.

The raw material compounding device 100 is a device for uniformly mixing raw materials contained in the production of the complex odor absorbent of the present invention. Preferably, raw material containing natural zeolite, ash, yellow soil, bentonite and sodium hydrogencarbonate is introduced And the raw material is rotated and uniformly mixed. More specifically, the raw material compounding apparatus 100 includes a frame, a housing installed at an upper portion of the frame, into which the raw material is input, a rotatably installed inside the housing, An impeller may be included.

The raw materials mixed in the raw material compounding device 100 may be transferred to the molding device 200 through the raw material transfer device 150 to be granulated. The molding apparatus 200 is an apparatus for producing a raw material in the form of a solid granule having a uniform particle size and continuously high density. As shown in FIGS. 2 and 3, the molding apparatus 200 includes a rotating body 210 that includes a binder in the mixed raw material and forms a granule by rotating the mixed raw material while rotating the rotating body 210, A scraper 250 provided inside the rotating body 210 for rotating the rotating body 210 at different positions according to the size of the granules, And a control unit for adjusting the angle.

More specifically, the rotating body 210 is vertically connected to the drive shaft to form a granule of the raw material, and the drive shaft is rotated by the drive unit 220 and can be supported by the support frame, In order to connect the rotating body 210 with the driving shaft, a connecting flange may be further included at the upper end of the driving shaft, and the connecting flange may be coupled to the rotating body 210 by a conventional fastening means. Further, a bearing is provided at a portion where the drive shaft is connected to the support frame while the drive shaft is supported by the support frame, so that the rotation of the drive shaft can be guided, and the support frame and the rotation frame can be coupled to the support frame.

The rotating body 210 includes an inclined disk 211 and a dam portion 212 formed vertically to the edge of the disk 211 to prevent the mixed raw material from being discharged to the outside before being grown into a granule shape larger than a reference size And a loop part 213 provided at the upper end of the dam part 212 for rolling the density of the granular raw material. Therefore, when the powder is grown in the form of granules having a standard size or more while rotating in the rotating body 210 including the binder in the mixed raw material, the centrifugal force due to rotation of the granular raw material overcomes the frictional resistance and gravity resistance And can be lowered out of the rotating body 210.

Generally, the molding apparatus 200 used for molding the granule shape has a problem that the time required for the raw material powder to coagulate and grow in a granular form is very short, and therefore, the density of the granule is low, . In order to solve this problem, the loop portion 213 may be formed at the upper end of the dam portion 212 and may be formed to have a reduced diameter. The loop portion 213 may be formed in the shape of a truncated ridge or a truncated dome Do. The loop portion 213 continuously rotates in the rotating body 210 even after the granules are grown to a size larger than the reference size, thereby generating a rolling friction phenomenon. Thus, even if the granular raw material is in contact with the rotating body 210 It is prevented from being discharged to the outside, and high-density hard granules can be formed.

The loop part 213 prevents the centrifugal force of the raw material powder not grown in the granules larger than the reference size from being larger than the gravity so that the raw material powder which does not grow in the granules larger than the reference size is naturally 211, and the granular raw material can be prevented from growing beyond the reference size by bringing the raw material having the binder into contact with the granular raw material of the reference size.

A scraper 250 may be provided on the inside of the rotating body 210 at a predetermined distance from the disk 211 so as to rotate at different positions depending on the particle size. The raw material grown in the form of granules while rotating inside the rotating body 210 is moved to the upper portion of the relatively small particles and the powdery raw material due to the centrifugal force and rolling friction caused by the rotating body 210, The granular material 250 is provided at a predetermined height from the circular plate 211 of the rotating body 210 so that the granular raw material is supplied to the rear of the scraper 250, And performs a blocking plate function for blocking rotation in the rotating direction. Further, it is possible to prevent the granular material from further including the binder from the jetting unit 260 provided behind the scraper 250, and to discharge the granular material, which has grown to the reference size, to the outside of the rotating body 210 .

The height of the scraper 250 can be adjusted according to the size of the granular material by the height adjusting means. The height adjusting means may be manually or automatically operated. It can be implemented in various ways. Specifically, it is also possible to form a plurality of perforation holes in a plurality of guide shafts and to engage with a bar supporting the scrapers 250, or to use an air cylinder, a hydraulic cylinder, a power cylinder or the like.

The scraper 250 may be inclined upward in the rotating direction of the rotating body 210 so that the granular material may be lowered in a wide range. The scraper 250 may be disposed at the center of the rotating body 210 The outer end of the scraper 250 is upwardly moved along the rotation direction so that the granular material grown in the reference size is guided only in the Y axis direction and is guided in various directions in a wider range .

And a jetting unit 260 for jetting a binder to the inner side of the rotating body 210. The jetting unit 260 is a device for jetting a binder to induce binding between powdery raw material particles to be granularly grown It is preferable that the scraper 250 is disposed behind the scraper 250, that is, in the rotational direction of the rotating body 210 so as not to contact the granular raw material grown at a reference size or more.

The injection nozzle of the jetting unit 260 may be movable by a moving unit for a predetermined interval. At this time, an air cylinder, a hydraulic cylinder, a power cylinder, a mechanical cam unit, a rack and a phantom unit may be used as the moving unit So that the binder can be uniformly sprayed to the upper portion of the disk 211 of the rotating body 210 regardless of the limited spraying range of the spraying nozzle. It is preferable that a plurality of injection nozzles of the jetting unit 260 are provided so as to uniformly jet the binder. The jetting nozzles are guided along the guide rails, And can move in a constant direction.

The molding apparatus 200 may include a control unit for adjusting the rotation speed and angle of the rotating body 210 or adjusting the injection time and the injection amount of the injection unit 260. More specifically, it includes an inverter control IC for controlling the number of revolutions of the rotating body 210, a lift means 230 for controlling the angle, a timer device for controlling the injection time of the binder, and a solenoid valve for controlling the injection amount .

A bypass line is further provided when the solenoid valve for controlling the injection amount of the injector unit 260 is locked and the injection of the binder is temporarily stopped so that the injected liquid can be recovered to the tank, So that it is not burdensome.

The number of revolutions of the rotating body 210 can be controlled by an inverter control (IC), preferably in the range of 3 to 30 rpm, and when the number of revolutions is less than 3 rpm, a high- The granule shape may be broken during the drying and calcining by applying the high temperature in the drying furnace 300 at the subsequent stage. If it exceeds 30 rpm, it may be difficult to grow the granule size.

The angle of the rotating body 210 may be angle-controlled by a lift means 230 included in the support frame. The lift means 230 may be configured in various ways, and may be a screw jack or a hydraulic jack So that the angle can be adjusted automatically by fitting the fastening rod into any selected fastening hole among a plurality of fastening holes. However, it is preferable that the rotating body 210 is adjusted at an angle of 30 to 55 degrees from the ground by the lift means 230 of the support frame, and when the angle approaches the vertical direction, The granular raw material can be separated from the rotating body 210.

Specifically, the drying and firing apparatus 300 included in the apparatus for producing a complex odor adsorbent of the present invention may be configured such that only the surface of a granule is dried using a drying unit 310 of a cylindrical rotary dryer provided with a downward inclination, And then drying only the granular raw material of the reference size remaining by using the firing portion 330. In this case,

The cylindrical rotary dryer constituting the drying and firing apparatus 300 of the present invention is provided so as to be inclined downward toward the other side discharged from one side to which the granular raw material is fed, and the granular raw material is continuously moved along the slope Loses. In addition, the cylindrical rotary dryer includes a differential separator 320 for separating fine particles, and a drying unit 310 for feeding the granular material around the differential separator 320, A firing portion 330 may be provided.

The differential separating unit 320 may separate the fine particles contained in the granular raw material through a cylindrical rotating screen including a plurality of perforated holes. The cylindrical rotary dryer may be rotated together with the cylindrical rotating screen, and the non-granular material of the reference size may be discharged to the outside through the perforation hole of the cylindrical rotating screen.

The drying unit 310 may dry only the surface of the granular raw material in a space where the granular raw material and the fine powder are mixed and dried together to prevent the granular form from being broken by the cylindrical rotating screen, In order to solve the phenomenon, only the minimum drying process is carried out, and the degree of drying may be different depending on the granular raw material and the characteristics of the finished product.

Accordingly, the firing portion 330 can burn only the granular raw material from which the fine particles have been removed, and can eliminate the rotational resistance due to the fine powder. This can increase the number of revolutions of the granular raw material, have. Accordingly, the granular adsorbent manufactured through the firing portion 330 can be manufactured more roundly and firmly, thereby improving the quality, and can be manufactured with a low volume and a high density, leading to a reduction in the cost of packaging and the saving of the storage space. There is an advantage to settle.

In addition, since fine particles are removed in the middle of the drying and firing apparatus 300 to prevent scattering of the fine particles in the workplace, cleanliness and safety of the workplace can be achieved.

Referring to the drying and firing apparatus 300 shown in FIG. 4, an inlet hood and an outlet hood may be included at one or both ends of the cylindrical rotary dryer, and an intermediate hood may be further included to surround the cylindrical rotary screen . The inlet hood, the outlet hood, and the intermediate hood serve as a connection of the body of the rotary dryer to be rotated and the non-rotating member such as the inlet, outlet, differential outlet, and the like.

The hood has a sealing device between the hood and the rotating body so as to block the inflow of outside air. The inlet hood, the outlet hood and the intermediate hood may each include a sealing device. The inlet and outlet are formed in the inlet hood and the outlet hood, respectively, and a differential outlet is formed in the intermediate hood.

Preferably, the charging unit is provided on an inclined upper portion of a cylindrical rotary dryer, which is a place where the granular material to be dried is input to the rotary dryer.

Preferably, the discharge unit is provided at an inclined lower portion of an inclined cylindrical rotary dryer for discharging the adsorbent produced by firing by the firing unit 330 of the rotary dryer, and the discharge unit may be formed into a hopper shape , A rotary valve or a double gate may be provided to prevent hot air from leaking through the discharge portion.

The differential discharge unit collects the fine particles discharged from the perforation hole of the cylindrical rotating screen and discharges the discharged fine particles to the outside. The differential discharge unit is also formed into a hopper shape, and a rotary valve or a double gate is installed, Is prevented from leaking. The conveyor for discharging the adsorbent and the conveyer for discharging the fine particles may be disposed at a lower portion of the discharge portion and a conveyor for discharging the granular material, respectively, A belt conveyor, a screw conveyor, a chain conveyor, or the like may be used.

At this time, the fine particles separated and discharged from the differential discharge conveyor can be transferred to the molding apparatus 200 and reintroduced.

The inlet hood or the outlet hood is formed with an exhaust port and the air introduced through the air supply device is heated by hot air by the hot air generating part 340. The granular raw material is fired in the rotary dryer and then discharged through the air outlet .

Since the cooled air and the evaporated water vapor used for drying and firing may include dust, it is preferable to connect the exhaust duct to the exhaust port and further purify the exhaust duct by including a dust filter bag. To the atmosphere.

When the hot air generating part 340 is provided on the charging part side, the direction of movement of the granular raw material and the hot air is the same as that of the continuous drying firing. When the hot air generating part 340 is provided on the discharging part side, If the gas is countercurrent, relatively hot air can be used at the inlet side, and relatively hot air can be used at the portion where the adsorbent is discharged. Therefore, the efficiency and energy of the firing portion 330 The efficiency of consumption can be increased. However, in some cases, it is preferable to use co-current when the surface of the granular raw material is not dried well. Accordingly, the hot air generating part 340 may be provided on the inlet side and the outlet side, respectively, and the drying and firing can be progressed alternately in the countercurrent flow and the cocurrent flow. In this case, It is preferable that an exhaust port is formed in the hood.

The hot air generating unit 340 can supply hot air to the cylindrical rotary dryer through a hot air supply duct. In order to prevent energy loss due to the hot air supply duct contacting the outside air, .

The granular adsorbent produced through the drying and calcining apparatus 300 is transferred to the screening and crushing apparatus 400 through the adsorbent conveying apparatus 350. When the granular adsorbent does not satisfy the standard size, the screening device 400 breaks the granular material into a fine particle size at the crushing part and transfers the crushed material to the molding device 200 It can be transferred and reintroduced. The crushing unit can be crushed while rotating a plurality of crushing blades at a high speed by driving the motor, and can be re-introduced into the molding apparatus 200 by passing through a perforated body and using a conveyer for differential discharge.

On the other hand, a raw material mixing step of uniformly mixing raw materials including natural zeolite, ash and additives, a step of molding the mixed raw material into a granule shape through a molding device 200, A drying and firing step of drying and firing the adsorbent to produce an adsorbent, the produced adsorbent is transferred to a screening and crushing apparatus 400 to select only a predetermined size, A complex odor adsorbent can be produced.

The raw material mixing step is a step of uniformly mixing raw materials including natural zeolite, ash, loess, bentonite and sodium hydrogencarbonate, preferably 20 to 25 parts by weight of ash, 4 to 7 parts by weight of loess 1 to 3 parts by weight of bentonite, and 13 to 16 parts by weight of sodium hydrogencarbonate.

The natural zeolite is a natural mineral having various physico-chemical properties which are industrially useful because of a pore structure peculiar to the surface pore existing in the crystal. The natural zeolite has a structure of Si , Al) O ₄ Tectosilicates are structured in three dimensions, with all the oxygen atoms in the tetrahedron being shared by another tetrahedron. Also, the natural zeolite has a lattice structure (specific gravity: 2.0-2.3) which is large enough to form a large pore size of 2.3-7.5 Å in the crystal within the crystal, and the size of the pore is 4-12 The oxygen is determined by the shape of the oxygen ring at the entrance to the structural pore and by the number of intervening oxygen.

In particular, natural zeolites are collected in the form of "zeolitic tuff", which is mostly degraded to fine-grained tuff, and is a hydrated silicate containing a small amount of Na, K, Ca, Mg, As minerals, the types are clinoptilolite, mordenite, heulandite, phillipsite, erionite, chabazite and periorite ferrierite and the like. In the present invention, the type of natural zeolite is not particularly limited, and natural zeolite collected from nature can be selectively used.

The fly ash has a large specific surface area and a large number of pores, and thus has good adsorption power, reduces hydration heat, and is economical because it can lower the unit cost of the adsorbent including the ash in terms of recycling waste materials. In addition, there is an excellent effect in increasing the porosity, improving the melting point, and lightening the weight of the composite odor adsorbent. The ash is preferably contained in an amount of 20 to 25 parts by weight of ash relative to 100 parts by weight of natural zeolite in the composite odor adsorbent using mixed zeolite. If the amount is less than 20 parts by weight or more than 25 parts by weight, . In addition, the particle size of the ash can be used without particular proposal if the particle size is such that the compound odor adsorbent does not cause problems in moldability during production.

Yellow loess is a weakly alkaline soil collected from the lower layer of the ground, which is different from the normal surface layer. It is rich in calcium carbonate and consists of various mineral particles such as quartz, feldspar, mica and calcite. It is also known that loess is chemically composed of silica, iron, alumina, magnesium, sodium, potassium, lime, smectite, etc., emitting far infrared rays, generating oxygen and deodorizing function. And the strength of the adsorbent is increased by lowering the melting point in the production of the composite odor adsorbent including the yellow loess.

The particle size of the loess is not particularly limited as long as it does not cause problems in the moldability of the adsorbent, but preferably a particle size of 0.02 to 0.05 mm can be used. The yellow loess of the present invention may be contained in an amount of 4 to 7 parts by weight based on 100 parts by weight of the natural zeolite. If the yellow loess component is less than 4 parts by weight, it is difficult to expect a far-infrared radiation and deodorizing effect. There is a problem that the moldability of the resin composition decreases.

Bentonite is a volcanic ash and rhyolite of the Neogene period, which is formed by stratification of volcanic rocks of Pelvic volcanism (rock formation) and formed stratification. The bentonite is composed of Montmorilllite-based expansive three- Si), and it can be expressed as Al ₂ Si ₄ (OH), which is a chemical structure of pyrophylite. In addition, the bentonite is gelled due to its swelling property by water in powder state. When the compounded zeolite is incorporated in the mixed zeolite adsorbent using the mixed zeolite of the present invention, the natural zeolite, fly ash, loess, bentonite, sodium hydrogencarbonate NaHCO ₃ ) and the organic binder to maintain the shape of the formed adsorbent to prevent deformation.

The bentonite is preferably contained in an amount of 1 to 3 parts by weight based on 100 parts by weight of the natural zeolite. When the amount of the bentonite is less than 1 part by weight, the strength of the adsorbent is lowered and the granule shape is easily broken. .

Sodium hydrogencarbonate generates pores or pores due to the generation of HCO ₃ gas during decomposition by heat during drying, and Na ⁺ in the inorganic system remains in the adsorbent even after firing, and can help form a structural force. In addition, natural zeolite, ash, loess, and bentonite can be adhered or adhered to the adsorbent of the present invention in the process of forming the pores or pores. The sodium hydrogencarbonate is preferably contained in an amount of 13 to 16 parts by weight based on 100 parts by weight of the natural zeolite. When the amount is less than 13 parts by weight, the desired structural force can not be imparted to the adsorbent. There may be a problem that the strength is excessively deteriorated.

The step of shaping the mixed raw material into a granule form through a molding apparatus includes a step of molding granules while rotating the raw materials and the binder mixed in the rotating body and preferably 100 parts by weight of the mixed raw materials 1 to 5 parts by weight of an organic binder may be contained and granulated through a molding apparatus.

The organic binder enhances the bonding strength between the mixed raw materials and improves the adhesion force to grow granules. The organic binder is composed of carbon, hydrogen, and oxygen as chemical components. In addition, inorganic binders such as sodium, magnesium, calcium, . As the organic binder, it is preferable to use at least one of molasses and carboxy methyl cellulose, and it may be a mixture of molasses and carboxymethyl cellulose, It can also be used. Preferably, the organic binder may be used by mixing water and molasses in a ratio of 1: 1 to 3: 1.

The amount of the organic binder is preferably 1 to 5 parts by weight based on 100 parts by weight of the mixture. If the amount of the organic binder is less than 1 part by weight, porosity may be insufficient due to oxidation of organic materials during firing, A problem may arise in which the adhesive strength is lowered and the shape of the adsorbent can not be maintained.

In the molding step, when the raw materials mixed in the rotating body and the organic binder are aggregated while rotating and the mixed raw materials in the form of powder are grown into granules, the centrifugal force due to the rotation causes the frictional resistance and gravity resistance The mixed raw material in the form of relatively small particles and powder is moved to the upper side and discharged to the outside of the rotating body so that only the granular raw material having the standard size or more can be obtained. Since the time required for the mixed raw material in the powder form to grow in the form of granules is very short, the density of the granular raw material is low, the strength is not rigid and the specific gravity can be lightened. The granules can be further rotated inside the rotating body even after the growth, so that it becomes possible to obtain a dense and hard granular raw material through rolling friction.

The drying and firing step may include a drying step of applying heat to the granular raw material, a drying step of removing heat from the granular surface by applying heat to the granular raw material, A fine particle removing step of passing fine particles through a rotating screen including a hole, and a sintering step of applying heat to the raw material from which the fine particles have been removed to obtain a sintered granular adsorbent.

Referring to FIG. 5, after a granular raw material and a fine powder are mixed in a cylindrical rotary dryer, the mixture is dried to dry only the surface by applying heat, and then passed through a rotating screen including perforated holes to remove fine powder, An adsorbent can be produced.

The sintering step is a step of drying only the surface of the granular raw material by heating the cylindrical rotary dryer at 80 to 150 ° C in order to prevent the granular raw material from being broken, more preferably from 100 to 120 ° C It can be dried by applying heat. If the temperature of the drying step is out of the range of 80 to 150 ° C, the granular raw material may be broken or cracked and the quality may be deteriorated.

The granular raw material having the dried surface through the drying step is passed through a rotating screen including a perforated hole to remove fine particles, and the granular form mixture after the forming step is mixed with fine powders And unnecessary energy waste is generated in drying and firing granule particles. Therefore, it is preferable that the fine particles passing through the rotating screen including the perforated holes and excluding the granular raw material larger than the reference size are discharged to the outside, and only the granular raw material is transferred to the firing step and fired.

In the firing step, heat is applied to the granular raw material having undergone the fine powder elimination step, and as the firing step proceeds, moisture in the granular mixture is evaporated, and humidity or humidity increases in the air The evaporation of water vapor is further difficult to cause a phenomenon of adhesion between the particles of the granule type mixture or a phenomenon in which the granule type raw material is adhered to the inside of the apparatus. Therefore, the granular type raw material is directly subjected to hot- .

The calcining step is a step of adding an adsorbent to the granular raw material by applying hot air at a temperature of 250 to 800 ° C to produce an adsorbent. More preferably, the granular raw material is calcined by applying hot air at 450 to 600 ° C. If the material is fired at a temperature of less than 450 ° C, the inside of the granular material may not be properly fired so that the shape may not be maintained and may be flared or cracked. If fired at a temperature higher than 600 ° C, The zeolite may undergo phase transformation or phase collapse and adsorption performance may be deteriorated.

The granular raw material is heated in the drying step and the firing step so that the granular raw material can be slowly heated and dried, and the granular raw material is heated while being heated for a predetermined period of time, .

Only the granular raw material from which the fine particles have been removed in the firing step after the fine powder removing step can be fired so that the rotational resistance due to the fine powder can be eliminated and the firing can be efficiently performed because the number of revolutions of the granular raw material is increased. Therefore, the granular raw material to be finished is more round, harder and more improved in quality, and economical due to its lower volume and higher density.

In addition, it is possible to prevent the scattering of the fine particles in the workplace by eliminating the fine powder in advance before the firing step, thereby making the workplace clean and safe.

The granule-type adsorbent prepared through the above-described firing step may be subjected to a screening process in which only a predetermined size is selected in advance, and the adsorbent having a size smaller than the remaining standard is discharged to the outside, And granular adsorbents that do not meet the remaining 0.5 to 20 mm size can be crushed.

In the screening step, the adsorbent having a sub-standard size is pulverized into a powder form through a pulverizer, and the pulverized pulverized powder is introduced into a molding step together with the fine powder discharged in the pulverizing step, and then mixed with the raw materials mixed in the mixing step, And may be molded into an adsorbent.

Hereinafter, an embodiment of the present invention will be described. However, the scope of the present invention is not limited to the following preferred embodiments, and a person skilled in the art can carry out various modifications of the contents described in the present invention within the scope of the present invention.

[Experimental Example 1]

Raw materials containing NaHCO ₃ in natural zeolite, ash, yellow soil and bentonite having the composition ratios shown in the following Table 1 were put into a raw material mixing apparatus 100 and mixed uniformly.

The organic binder was prepared by mixing water and molasses (33 wt%) at a ratio of 2: 1 at 30 캜.

A granule type raw material having a size of 0.5 to 20 mm was prepared at a ratio of 100 g of the starting material and 3.3 g of the organic binder in the ratio shown in Table 2 below using a molding machine.

The granular raw material was put into a dry calcining apparatus to prepare an adsorbent. The drying and firing apparatus was rotated for 30 minutes while maintaining the temperature within the range of 100-120 ° C. The fine powder contained in the granular raw material was removed through a rotating screen and then moved to the firing portion. The granular adsorbent prepared after sintering by hot air at a temperature of < RTI ID = 0.0 > 1 C < / RTI >

Examples 1 to 3 and Comparative Examples 1 to 4 were prepared by selecting only the particle size of the granules of 0.5 to 20 mm from the granular adsorbent through the screening crusher. The granule type adsorbent whose size did not satisfy 0.5 ~ 20 mm was crushed and re-transferred to the molding machine.

Constituent Natural zeolite Fly Ash ocher Bentonite SiO ₂ 71.0 54.1 52.9 68.57 Al ₂ O ₃ 11.4 14.4 23.4 14.79 K ₂ O 2.92 1.18 2.53 0.51 CaO 2.27 1.0 0.20 3.29 MgO 0.67 0.28 0.88 3.16 Na ₂ O 0.40 0.03 0.35 0.15 Fe ₂ O ₃ 0.74 4.84 8.70 3.95 TiO ₂ 0.08 0.86 1.11 0.03 MnO 0.06 - 0.07 0.07 P ₂ O ₃ - 0.29 0.12 0.08 Other 10.46 23.02 9.74 5.40

^{(unit :%)}

Zeolite Fly Ash ocher clay Starch Bentonite NaHCO ₃ Example 1 72.4
(100) 14.5
(20) 2.9
(4) - - 0.75
(One) 9.45
(13) Example 2 70
(100) 15
(21.4) 4
(5.7) - - One
(1.4) 10
(14.3) Example 3 67
(100) 16.5
(24.6) 4.5
(6.7) - - 1.5
(2.2) 10.5
(15.7) Comparative Example 1 74
(100) 14
(18.9) 2.5
(3.4) - - 0.5
(0.7) 9
(12.2) Comparative Example 2 65
(100) 17
(26.2) 5
(7.7) - - 2
(3.1) 11
(16.9) Comparative Example 3 70
(100) 15
(21.4) 4
(5.7) 10
(14.3) - One
(1.4) - Comparative Example 4 60
(100) 20
(33.3) - - 15
(25) - 5
(8.3)

^{(Unit: g, in parentheses)} ^{Weight portion} ⁾

[Experimental Example 2]

Performance evaluation according to drying temperature and firing temperature

In order to measure the maximum firing temperature at which the phase collapse of the zeolite does not occur during the production of the adsorbent through the experimental method of Experimental Example 1, the natural zeolite was subjected to an organic acid conversion Iodine adsorption performance was evaluated. The iodine adsorption performance was evaluated by weighing granular natural zeolite calcined in iodine solution for 24 hours.

Firing temperature (캜) 500 ℃ 600 ℃ 700 ℃ 800 ° C abandonment
Oxidation
Degree Before firing (g) 194.38 192.69 192.34 192.04 After firing (g) 170.30 165.95 165.47 163.69 Weight change (%) 12.4 13.9 14.0 14.5 iodine
absorption
Performance Before iodine impregnation (g) 50.06 50.11 50.32 50.19 After iodine impregnation (g) 62.5 63.57 61.81 61.18 Weight change (g) 12.44 13.46 11.49 10.99 Volume change (%) 46.15 49.94 42.63 40.77 Adsorption performance (%) 19.9 21.1 18.6 18.0

Table 3 shows the results of the evaluation of the degree of organic matter oxidation and iodine adsorption performance at the firing temperature measured by the firing test. The firing efficiency was the highest at the firing temperature of 500 to 700 ° C., It was found that the adsorption function was reduced due to the clogging of the micropores due to the collapse of the structural defects inside the natural zeolite. Therefore, it was found that when the maximum firing temperature is 500 to 700 ° C., the adsorption efficiency is excellent.

According to the results of Table 3, the maximum firing temperature was set to 500 to 700 ° C., and the granular raw material, Example 1, was subjected to the four conditions of Table 4, Dried and calcined to prepare an adsorbent. The drying temperature was set to 80 to 150 ° C. The sintering temperature was set to 250 to 800 ° C while the total cumulative heating time was set to 90 minutes. Also, the experiment was carried out with a drying time> firing time for T1 or T2 and a firing time for T3 or T4.

division Set temperature
(° C) dry Plasticity Cumulative time
(min) Heating time (min) Duration (min) Heating time (min) Duration (min)
T1 80 10 20 - - 30 150 10 20 - - 60 450 - - 5 10 75 600 - - 5 10 90

T2 80 10 20 - - 30 150 - 30 - - 60 300 - - 5 5 70 450 - - 5 5 80 600 - - 5 5 90 T3
80 10 30 - - 40 600 - - 10 40 90
T4 80 10 10 - - 20 150 10 10 - - 40 450 - - 5 5 50 600 10 30 90

The hydrophobic test was conducted on T1 to T4 prepared according to Table 4 to measure the release phenomenon against water. Experimental results showed that cracking or cracking of filter media occurred after firing and T1 and T3 showed water melting phenomenon in hydrophobic experiments. However, in case of T4, the strength was maintained and no cracking or cracking phenomenon could be observed. In the hydrophobic test, it was slightly dissolved in water but the shape did not change. Therefore, it was found that the drying temperature and the calcination temperature of the complex odor adsorbent using the mixed zeolite of the present invention are preferably 80 to 150 ° C. and 250 to 800 ° C., respectively.

Drying and firing equipment Energy consumption comparison

When 50 ton / hr of granular raw material prepared through the above Experimental Example 1 was fed into a desiccant using a drying apparatus having a capacity of 150 ton / hr, the amount of energy consumption of the prior art and the drying And the amount of energy consumption during the generation of the countercurrent hot air was compared at the part and the firing part.

The moisture content of the raw material charged into the dry calcining apparatus was 15%, and the residual moisture of the adsorbent was 4%.

Conventional dry baking apparatus Drying section Plastic part Granule heating temperature
(Kcal / hr)
3,825,000
3,060,000
273,000 Moisture heating temperature
(Kcal / hr)
2,250,000
1,800,000
90,000 Moisture evaporation latent heat
(Kcal / hr)
8,893,500
4,042,500
1,347,500 Body loss calorie
(Kcal / hr)
879,200
329,700
329,700 Exhaust Loss Calories
(Kcal / hr)
4,435,200
3,158,400
- Total calorie consumption
(Kcal / hr)
20,282,900
12,390,200
2,040,200

From the results of Table 5, it can be seen that the energy saving amount according to the present invention corresponds to a total of 5,852,500 Kcal / hr (20,282,900- (12,390,200 + 2,040,200)). It can be seen that the energy saving ratio is about 28.85%.

[Experimental Example 3]

Iodine adsorption performance evaluation

Examples 1 to 3 and Comparative Examples 1 to 4 prepared in Experimental Example 1 were impregnated in an iodine solution for 24 hours, and weight and volume changes were measured.

Name of sample Precipitation (g) After impregnation (g) Weight change (g) Volume change (%) Adsorption performance (%) Example 1 15.52 22.50 6.98 28.94 32 Example 2 15.43 23.58 8.15 30.24 34 Example 3 15.39 22.46 7.07 29.99 33 Comparative Example 1 15.88 22.25 6.37 23.63 28 Comparative Example 2 15.71 22.09 6.38 23.67 29 Comparative Example 3 15.26 22.11 6.85 25.41 31 Comparative Example 4 15.81 23.11 7.30 27.08 31

From the results of Table 6, it can be seen that Examples 1 to 3 are superior in iodine adsorption performance to Comparative Examples 1 to 4. It was also confirmed that the adsorption performance of the complex odor adsorbents of Examples 1 to 3 was superior to that of the natural zeolite of Experimental Example 1 in comparison with the iodine adsorption performance evaluation.

[Experimental Example 4]

Evaluation of compressive strength

The compressive strength of each of Examples 1 to 3 and Comparative Examples 1 to 4 prepared in Experimental Example 1 and commercially available adsorbents DW1 to DW4 (KYOCERA CO., LTD.) Were measured after ten cycles each by using a compressive strength meter Respectively.

Name of sample Compressive strength ( Kgf ) Example 1 5.13 Example 2 5.90 Example 3 5.23 Comparative Example 1 4.21 Comparative Example 2 4.37 Comparative Example 3 0.83 Comparative Example 4 3.40 DW1 (Zeolite) 22.8 DW2 (multi-pore zeolite) 26.0 DW3 (loess ball) 4.90 DW4 (low temperature baked loam ball) 5.70

The results of Table 7 show that DW1 and DW2 which are commercially available products (600 to 1000 ° C) manufactured by high temperature baking are superior to those of Examples 1 to 3. However, DW3 to DW4 (200 to 600 ° C) The compressive strength was similar.

It was also confirmed that the compressive strength of Comparative Example 3 containing no sodium hydrogencarbonate and Comparative Example 4 containing starch were significantly lower than those of Examples 1 to 3 and Comparative Examples 1 and 2.

[Experimental Example 5]

Evaluation of adsorption performance of odor-inducing substances

10 g of each of the adsorbents DW1 to DW4 prepared in Examples 1 to 3 and Comparative Examples 1 to 4 prepared in Experimental Example 1 and commercially available adsorbents DW1 to 4 were sampled and injected into mercaptan, ammonia, acetaldehyde, and trimethylamine solutions as malodorous substances And the adsorption rate of the malodorous substance was measured by measuring the weight by time.

2 hr 4 hr 6 hr 8 hr 12 hr 16 hr 20 hr 24 hr Example 1 0.372 0.321 0.302 0.289 0.261 0.227 0.206 0.187 Example 2 0.420 0.370 0.340 0.310 0.270 0.230 0.210 0.190 Example 3 0.396 0.372 0.354 0.304 0.291 0.209 0.199 0.192 Comparative Example 1 0.309 0.284 0.251 0.221 0.201 0.184 0.157 0.134 Comparative Example 2 0.333 0.301 0.276 0.244 0.205 0.192 0.179 0.167 Comparative Example 3 0.318 0.273 0.24 0.201 0.188 0.169 0.162 0.123 Comparative Example 4 0.299 0.287 0.261 0.236 0.204 0.191 0.191 0.146 DW1 0.287 0.210 0.198 0.186 0.180 0.174 0.174 0.156 DW2 0.382 0.382 0.342 0.296 0.25 0.217 0.211 0.197 DW3 0.345 0.331 0.317 0.296 0.268 0.254 0.246 0.232 DW4 0.228 0.222 0.204 0.173 0.154 0.136 0.111 0.093

^{(Unit: g / g)}

First, the adsorption performance against mercaptan, which is one of the odor inducing substances, was evaluated. As shown in Table 8, it was confirmed that Example 2 showed the highest adsorption efficiency at 0.420 g / g. Next, it was found that the adsorption efficiency was 0.396 g / g in the order of DW2 commercially available in Example 3 and 0.382 g / g.

2 hr 4 hr 6 hr 8 hr 12 hr 16 hr 20 hr 24 hr Example 1 0.310 0.300 0.287 0.274 0.261 0.248 0.240 0.228 Example 2 0.314 0.304 0.284 0.275 0.265 0.255 0.245 0.245 Example 3 0.320 0.301 0.280 0.267 0.257 0.251 0.241 0.231 Comparative Example 1 0.259 0.259 0.259 0.259 0.247 0.240 0.231 0.218 Comparative Example 2 0.262 0.281 0.271 0.254 0.241 0.229 0.216 0.207 Comparative Example 3 0.258 0.251 0.246 0.241 0.234 0.234 0.234 0.234 Comparative Example 4 0.243 0.231 0.225 0.216 0.213 0.210 0.200 0.200 DW1 0.110 0.110 0.108 0.052 0.052 0.052 0.052 0.052 DW2 0.258 0.258 0.253 0.224 0.174 0.174 0.174 0.174 DW3 0.267 0.257 0.257 0.237 0.232 0.227 0.227 0.227 DW4 0.097 0.097 0.097 0.087 0.070 0.070 0.070 0.070

^{(G / g)}

Table 9 shows the results of the adsorption rate test using formaldehyde, which is one of the odor inducing substances, that 0.320 g / g was the best adsorption rate in Example 3, 0.314 g / g in Example 2, 0.310 g / g, and DW3 was 0.267 g / g.

2 hr 4 hr 6 hr 8 hr 12 hr 16 hr 20 hr 24 hr Example 1 0.310 0.281 0.251 0.222 0.204 0.184 0.174 0.173 Example 2 0.320 0.290 0.260 0.240 0.210 0.190 0.180 0.180 Example 3 0.318 0.289 0.257 0.231 0.208 0.181 0.177 0.177 Comparative Example 1 0.275 0.259 0.241 0.212 0.198 0.172 0.154 0.152 Comparative Example 2 0.277 0.261 0.242 0.201 0.178 0.161 0.143 0.134 Comparative Example 3 0.271 0.244 0.221 0.190 0.165 0.165 0.165 0.165 Comparative Example 4 0.280 0.270 0.254 0.200 0.170 0.140 0.120 0.120 DW1 0.128 0.128 0.122 0.118 0.115 0.109 0.109 0.109 DW2 0.263 0.258 0.253 0.234 0.194 0.154 0.119 0.119 DW3 0.252 0.247 0.247 0.227 0.217 0.168 0.128 0.128 DW4 0.099 0.096 0.094 0.091 0.089 0.089 0.070 0.070

^{(G / g)}

Table 3 shows the results of adsorption experiments using ammonia among the odor-inducing substances. Example 2 showed the highest adsorption rate at 0.320 g / g, 0.318 g / g in Example 3, 0.310 g / g, and Comparative Example 4 was 0.280 g / g.

2 hr 4 hr 6 hr 8 hr 12 hr 16 hr 20 hr 24 hr Example 1 0.302 0.265 0.241 0.215 0.176 0.157 0.129 0.118 Example 2 0.307 0.267 0.238 0.208 0.188 0.168 0.139 0.129 Example 3 0.305 0.261 0.241 0.207 0.185 0.170 0.135 0.123 Comparative Example 1 0.287 0.249 0.221 0.197 0.176 0.148 0.121 0.105 Comparative Example 2 0.291 0.254 0.232 0.211 0.171 0.137 0.112 0.091 Comparative Example 3 0.301 0.248 0.229 0.183 0.157 0.111 0.059 0.059 Comparative Example 4 0.340 0.307 0.267 0.227 0.187 0.147 0.127 0.093 DW1 0.139 0.099 0.079 0.053 0.033 0.020 0.007 0.007 DW2 0.191 0.151 0.125 0.099 0.072 0.046 0.033 0.026 DW3 0.250 0.204 0.164 0.125 0.092 0.059 0.039 0.026 DW4 0.145 0.099 0.079 0.059 0.039 0.026 0.020 0.013

^{(G / g)}

Table 11 shows the results of adsorption experiments using trimethylamine among the odor inducing substances. As a result of the adsorption test, the adsorption performance of Comparative Example 4 was 0.340 g / g, that of Example 2 was 0.307 g / g, that of Example 3 was 0.305 g / g, and Example 1 0.302 g / g.

The results of Tables 8 to 11 of Experimental Example 5 show that adsorption ratios of mercuric compounds such as mercaptan, formaldehyde, ammonia, and trimethylamine, which are malodorous substances, Example 3, Comparative Example 4 and DW2 showed a high adsorption rate. In Example 2, however, adsorption efficiency of mercaptan, formaldehyde, ammonia, and trimethylamine was comparatively evaluated, Respectively.

[Experimental Example 6]

Pilot - test Performance evaluation of adsorption tower

The adsorption experiment was conducted to evaluate the malodor removing performance of Example 2, which was rated excellent in Experimental Example 5 above.

A solution containing hydrogen sulfide, acetaldehyde, trimethylamine, and ammonia, which are major odor inducing substances generated in a food processing facility, is boiled in lukewarm water, and the gaseous phase gas is volatilized to a mixed odor absorbent Was passed through a packed bed to measure the outflow concentration after 2 hours and 4 hours.

division Influent concentration
(ppm) Effluent Concentration (ppm) Reduction rate (%) 2 hours 4 hours 2 hours 4 hours ammonia 2.865 0.454 1.937 84.2 32.4 Acetaldehyde 8.096 0.133 0.994 98.4 87.7 Trimethylamine 1.434 - 0.159 - 88.9 Complex odor 30,000 times 100 144 - -

As shown in Table 12, the ammonia concentration was measured to be 0.454 ppm and 1.937 ppm at the inlet concentration of 2.868 ppm after 2 hours and 4 hours, respectively, and the reduction rate was 84.2% and 32.4%, respectively. Acetaldehyde had an inlet concentration of 8.096 ppm , The reduction rate was measured as 98.4% and 87.7% at 0.133 ppm and 0.994 ppm after 2 hours and 4 hours, respectively, and trimethylamine was not detected at 0.159 ppm after 2 hours and 4 hours after the introduction at 1.434 ppm The reduction rate was measured as 88.9%.

The results of Experimental Examples 5 and 6 demonstrate that the complex odor adsorbent of the present invention can adsorb odor-causing substances such as ammonia, acetaldehyde, trimethylamine, mercaptan, etc., And it was confirmed that the efficiency of desorption by microwaves was excellent and the efficiency of regenerated energy was excellent.

The apparatus and method for producing a composite odor adsorbent according to the present invention are not limited to the above-described embodiments, and various modifications and changes may be made without departing from the spirit and scope of the present invention, The present invention is not limited to the scope of the claims of the present invention.

100: raw material mixing apparatus 150: raw material feeding apparatus
200: forming device
210: Rotor 211: Disc
212: dam part 213: loop part
220: drive device 230: lift means
250: scraper 260:
300: Drying and firing apparatus 310: Drying unit
320: differential separator 330: fired part
340: hot air generating part 350: adsorbent conveying device
400: Screen shredding device

Claims

A raw material mixing apparatus (100) for uniformly mixing raw materials supplied thereto;
A forming device 200 for forming a granular material having a uniform size by rotating the mixed raw materials at different positions depending on the particle size,
A drying and firing apparatus 300 for removing fine powder contained in the granular raw material, drying and firing the powder to produce an adsorbent; And
And a screening and crushing apparatus 400 for screening only the predetermined size of the prepared adsorbent and then discharging the adsorbent having a size smaller than the remaining standard to the outside,
The drying and firing apparatus 300 includes:
And a differential separator (320) for separating the fine particles contained in the granular raw material in the cylindrical rotary dryer provided at a downward slope,
And the drying unit (310) and the burning unit (330) are divided around the differential separating unit (320).

The method according to claim 1,
The molding apparatus (200)
A rotating body 210 including a binder in the mixed raw material and rotating the mixed raw material in a granule shape while rotating the mixed raw material;
A jetting unit 260 disposed inside the rotating body 210 for jetting the binder;
A scraper 250 provided inside the rotating body 210 to rotate at different positions according to the size of the granule shape; And
And a control unit for controlling the number of revolutions and angle of the rotating body (210) or the injection time and injection amount of the injection unit (260).

3. The method of claim 2,
The rotating body 210 is
An original plate 211 inclined;
A dam portion 212 formed perpendicularly to the rim of the circular plate 211 to prevent the granular material having a reference size or less from being discharged to the outside; And
And a loop part (213) provided at an upper end of the dam part (212) for rolling the granular raw material.

delete

The method according to claim 1,
Wherein the differential separating unit (320) separates the fine particles contained in the granular raw material through a cylindrical rotating screen including a plurality of perforated holes.

The method according to claim 1,
The screening and crushing apparatus 400 includes a sorting unit for sorting the adsorbent into a predetermined size and discharging the adsorbent to the outside; And
And a crushing unit for crushing the adsorbent having a sub-standard size that has not passed through the sorting unit and delivering the crushed adsorbent to the granule forming apparatus 200.

A raw material mixing step in which a raw material including natural zeolite, Ash, loess, bentonite and sodium hydrogencarbonate (NaHCO3) is uniformly mixed;
Molding the mixed raw material into a granule form through a molding apparatus 200;
A drying and calcining step of drying and firing the granules-shaped raw material to produce an adsorbent;
And crushing the produced adsorbent by transferring the adsorbent to a screening crusher 400 to select only a predetermined size,
The drying and firing step comprises:
A drying step of applying heat to the granular shaped raw material to remove moisture on the granular surface;
A fine particle removing step of passing the raw material, which has been granulated through the drying step, through a rotating screen including a perforation hole to remove fine particles; And
And a calcining step of applying heat to the raw material from which the fine particles have been removed.

8. The method of claim 7,
The raw material mixing step includes uniformly mixing 20 to 25 parts by weight of ash, 4 to 7 parts by weight of loess, 1 to 3 parts by weight of bentonite and 13 to 16 parts by weight of sodium hydrogen carbonate with respect to 100 parts by weight of natural zeolite By weight based on the total weight of the adsorbent.

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