CN112341266A

CN112341266A - Zeolite biological organic fertilizer and preparation method thereof

Info

Publication number: CN112341266A
Application number: CN202011154878.2A
Authority: CN
Inventors: 阿道夫·卡洛斯
Original assignee: China Arab Zeolite Chengde Environmental Protection Technology Co ltd
Current assignee: China Arab Zeolite Chengde Environmental Protection Technology Co ltd
Priority date: 2020-10-26
Filing date: 2020-10-26
Publication date: 2021-02-09

Abstract

The invention discloses a zeolite bio-organic fertilizer and a preparation method thereof, wherein the zeolite bio-organic fertilizer comprises zeolite, the zeolite contains azospirillum, and the content of azospirillum in the zeolite is 1x10⁸The manufacturing method of the zeolite bio-organic fertilizer comprises a microorganism culture chamber stage, a solid fermentation stage, a liquid fermentation stage and a solid product stage, wherein the solid product stage is to mix the azospirillum suspension obtained in the liquid fermentation stage with zeolite, dry the mixture and grind the mixture to obtain a finished product. The zeolite biological organic fertilizer adopts zeolite as a microbial carrier, has the characteristic of beneficial interaction with crops, and is a product obtained by the preparation method of the zeolite biological organic fertilizerThe concentration is ten times higher than that of the existing product, so that the transportation cost is obviously lower, and the obtained product with higher concentration is more efficient in applying crops.

Description

Zeolite biological organic fertilizer and preparation method thereof

Technical Field

The invention relates to the technical field of organic fertilizer processing, in particular to a zeolite biological organic fertilizer and a manufacturing method thereof.

Background

In agricultural production, fertilization is an important means for ensuring high yield of crops, the using amount of chemical fertilizers in China is large, although the yield of crops is increased in a certain period, the chemical fertilizers have more and more harm to soil, water sources, agricultural products and the environment, the consequences of soil acidification, hardening, nutrition unbalance, underground water pollution, excessive heavy metal and nitrate content in the agricultural products and the like are caused, the chemical fertilizers are applied repeatedly and applied in disorder, no biological organic fertilizer is used, the organic matter in the soil is lack, and the soil fertility is reduced. The biological organic fertilizer can improve the product quality, improve the rhizosphere microbial flora of crops, improve the disease resistance of plants, promote the use of the fertilizer and improve the utilization rate of the fertilizer; the technical content of the production of the bio-organic fertilizer is relatively high, and in order to improve the effect of the product, microorganisms with specific functions need to be added into the product.

Similar biological bacteria products on the market at present are solid products which are soluble in water to form microorganism suspension and can be directly applied after being dissolved in water. The manufacturing processes for the existing products are very different and the prior art does not provide an economical and efficient method to achieve high concentrations of microorganisms in the final product.

Disclosure of Invention

In view of the above technical problems in the related art, the present invention provides a zeolite bio-organic fertilizer and a method for preparing the same, which can overcome the above disadvantages in the prior art.

In order to achieve the technical purpose, the technical scheme of the invention is realized as follows:

the zeolite biological organic fertilizer comprises zeolite, wherein the zeolite contains azospirillum, and the content of azospirillum in the zeolite is 1x10⁸Per gram.

Preferably, the zeolite is a natural zeolite.

According to another aspect of the present invention, there is provided a method for preparing the zeolite bio-organic fertilizer, comprising the following steps:

s1, pouring the diluted and sterilized culture medium on a culture dish, inoculating the azospirillum thallus into the culture dish in a controlled sterile environment, putting the culture dish into a culture furnace to provide the optimal temperature for the growth of microorganisms, and putting the culture dish into a refrigerator for later use;

s2 solid fermentation stage, wherein the solid carrier is cooked sterile corn, the cooked sterile corn is placed into a container, then the container is placed into an autoclave, the sterile corn is used for inoculating the azospirillum strain obtained in the step S1 into the container, the container is sent to a solid fermentation chamber for solid fermentation, the solid fermentation chamber is sterilized by steam, and then the extraction operation is carried out to extract the azospirillum suspended on the surface of the solid through solid-liquid extraction;

s3 liquid fermentation stage, placing the sterilized liquid culture medium into a reaction tank, inoculating the azospirillum obtained in the step S2 into the liquid culture medium through a material feed hopper, and performing liquid fermentation to obtain azospirillum suspension;

and S4, solid product stage, namely stirring and mixing the azospirillum suspension obtained in the step S3 and zeolite, drying, and grinding to obtain a finished product.

Preferably, the solid state fermentation process lasts 7-10 days.

Preferably, the pH of the medium is maintained between 5.5 and 6.5 in step S3.

Preferably, the drying temperature in step S4 is not higher than 40 ℃.

The invention has the beneficial effects that: the microbial carrier-natural zeolite used by the zeolite bio-organic fertilizer has the characteristic of beneficial interaction with crops, and the preparation method of the zeolite bio-organic fertilizer can ensure that the concentration of microorganisms in a solid product is at least ten times higher than that of the existing product in the process stages of solid fermentation, solid extraction, liquid fermentation, powder manufacturing and the like, so that the transportation cost is obviously lower, and the obtained high-concentration product is more efficient in applying the crops.

Drawings

In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings needed in the embodiments will be briefly described below, and it is obvious that the drawings in the following description are only some embodiments of the present invention, and it is obvious for those skilled in the art to obtain other drawings without creative efforts.

FIG. 1 is a schematic structural view of a cooking device according to an embodiment of the present invention;

FIG. 2 is a schematic view of a cooking apparatus according to an embodiment of the present invention in use;

FIG. 3 is a top view of a cooking device according to an embodiment of the present invention;

FIG. 4 is a schematic structural diagram of an autoclave system according to an embodiment of the present invention;

FIG. 5 is a schematic view of the usage state of the autoclave system according to the embodiment of the present invention;

FIG. 6 is a top view of an autoclave system according to an embodiment of the present disclosure;

FIG. 7 is a schematic illustration of an inoculation procedure according to an embodiment of the present invention;

FIG. 8 is a schematic illustration of a placement according to an embodiment of the invention;

FIG. 9 is a schematic view of a contactor device according to an embodiment of the present invention;

FIG. 10 is a side view of a contactor device (secondary tank hydraulic system) according to an embodiment of the invention;

FIG. 11 is a top view of a contactor device according to an embodiment of the invention;

FIG. 12 is a schematic view of an agitation tank according to an embodiment of the present invention;

FIG. 13 is a schematic view of the inside of an agitation tank according to an embodiment of the present invention;

FIG. 14 is a top view of an agitation tank according to an embodiment of the present invention;

FIG. 15 is a schematic view of a drying apparatus according to an embodiment of the present invention;

fig. 16 is a front view of a drying apparatus according to an embodiment of the present invention;

fig. 17 is a side view of a drying apparatus according to an embodiment of the present invention.

Detailed Description

The technical solutions in the embodiments of the present invention will be clearly and completely described below with reference to the drawings in the embodiments of the present invention, and it is obvious that the described embodiments are only a part of the embodiments of the present invention, and not all of the embodiments. All other embodiments that can be derived by one of ordinary skill in the art from the embodiments given herein are intended to be within the scope of the present invention.

Example 1

The zeolite biological organic fertilizer comprises zeolite, wherein the zeolite is natural zeolite, the zeolite contains azospirillum, and the content of azospirillum in the zeolite is 1x10⁸Per gram.

The preparation method of the zeolite bio-organic fertilizer comprises the following steps:

s1 microbial growth chamber stage:

the diluted and sterilized culture medium is poured onto a petri dish, the cells of azospirillum are inoculated into the petri dish in a controlled sterile environment, the petri dish is placed into a culture furnace, the culture furnace provides the optimum temperature for the growth of the microorganisms, the biomass is multiplied in this stage, and the petri dish is covered with a cover and placed in a refrigerator for standby (preventing the growth and propagation of the microorganisms until the next stage is needed).

Wherein the culture medium is selective to fungi, glucose, agar, potato agar, etc., the culture medium dilution process depends on the requirements of the culture medium, the culture medium sterilization process is carried out in an autoclave, from the energy source perspective, the culture medium can be electric or gas, in order to avoid the culture medium pollution, the sterilized culture medium can be refrigerated for standby, and the refrigerated culture medium is poured on a culture dish after being heated by a water bath during use;

the culture dish adopts a petri dish: the petri dish was stylized, dry-heated in a furnace at 120 ℃; for 3 hours. The assembly of the petri dishes is performed under a controlled environment in connection with sterility, under a laminar flow hood.

The specific process of azospirillum inoculation is as follows: the biological material was removed from the other support and inoculated by anza into petri dishes with solid media in a controlled sterile environment (laminar flow hood).

S2 solid fermentation stage:

the solid carrier is cooked sterile corn, the corn is cooked by using the cooking device shown in figures 1-3, the device comprises a stirring motor 1, a steam inlet 2, a jacket I3, a steam elimination pipe 4, a stirring blade 6, a valve 5 and a bag 7 for containing corn, wherein the power of the stirring motor is determined according to the volume of a tank, steam enters a heating mixture through the steam inlet 2 for cooking, the valve 5 removes water for cooking, then the liquid is reused for liquid fermentation, the steam elimination pipe 4 eliminates condensed water through a drain valve, the heat provided by the condensed liquid can be recovered through contacting with another cold liquid, the stirring blade 6 stirs during the cooking process, to ensure uniformity, the bag 7 containing the corn is a porous bag, allowing water to enter, but not allowing the cooked corn to exit, which is later recovered;

the water in the device is heated by steam and indirectly contacted with the corn through the shell, and the corn is boiled for 10 minutes at the boiling water temperature, and the operation comprises the following steps: placing corn in a bag, irrigating until the corn is covered, placing the bag on the upper line of a first jacket, injecting steam through the first jacket to heat water, and cooking the corn, wherein the water is drinkable, and has no special requirement for salt content, and the conduit sleeve is prepared mechanically to bear an absolute pressure of 2kg/cm²The steam of (2). The size of the apparatus depends on the quantity of material to be treated, hydraulic factors such as the stirring speed at RPM (revolutions per minute) and also on the geometry of the system and therefore on the quantity to be treated;

weighing corn, cooling the cooked corn, putting the corn into a container (bottle) after ear beating; the bottles are to be sterilized: washing with a broad spectrum disinfectant solution (such as ethanol and sodium hypochlorite), washing with drinking water, and bottling, wherein the tare corn is placed in containers which pass through a cotton filter as a separating wall for air to enter to prevent external microorganisms from contaminating the solid; the container is then placed in an autoclave, the autoclave system used is shown in fig. 4-6 and comprises a pressure gauge 8, a steam pipe 9, a drain valve 10, a flange 11 and a safety valve 12, the pressure gauge 8 is used for measuring the pressure in the container, the steam for heating the water tank enters through the steam pipe 9, the drain valve 10 is used for removing condensed water from the container in the autoclaving operation, the flange 11 is used for sealing the system and can work under the pressure higher than the atmospheric pressure, the safety valve 12 is also used for removing air when the sterilization is started and then is closed, and the function of maintaining a certain pressure is achieved, in this case 1.5 Bar.

The autoclave is operated at pressures above atmospheric and therefore is built taking these details into account, the thickness of the wall of the tank being a function of the required capacity of the autoclave. The autoclave has a manometer as instrument and a pt100 thermometer independent of the manometer, with two valves, one for drawing air at the start of sterilization and the other as safety relief valve for calibrating the pressure at which the operation is desired.

As shown in FIG. 7, the Azospirillum azotobacter strain obtained in step S1 in dish 14 is inoculated in the container with sterile corn 13 (in a controlled environment, i.e., a laminar flow box, a portion of the biomass produced is inoculated in a petri dish with sterile corn in a bottle, then the bottle is closed), and sent to a solid state fermentation chamber for solid state fermentation, which lasts for 7-10 days, including the propagation of microorganisms on the surface of corn. This activity is carried out at controlled temperatures, which must be optimal for the growth and propagation of the microorganisms. Thus, the cabinet has an air conditioning system. The inoculated pots were placed on a shelf in the manner shown in fig. 8.

Sterilizing in the reactor tank: and water to be used for solid-liquid extraction is stored in the reactor tank. This water may be drinking water from the pipe network, but must be completely free of other microorganisms in order to avoid contaminating the final product. This sterilization is performed by direct steam injection. The reactor is filled with 75% of the total water and then steam is injected until the same condensate occupies the missing volume. The initial volume of water depends on the time it is desired to keep the water vapor mixture at a certain temperature.

Solid-liquid extraction: the leaching operation is performed to extract the microorganisms suspended on the solid surface so that the corn is in intimate contact with water in the solvent, in which way the solute content of the solvent will be relatively rich and, finally, the concentration of suspended microorganisms will be relatively high. The adopted contactor device is shown in figures 9-11, and comprises a first stop valve 15, a small reactor motor 16, a return pipe 17, a biomass material bag 18, a small groove type stirrer 19, a second stop valve 20, a first ball valve 21, a first booster pump 22, a second booster pump 23, a second ball valve 24, a third ball valve 25, a fourth ball valve 26, a steam inlet pipe 27, an air inlet pipe 28, a fifth ball valve 29, a sixth ball valve 30, a seventh ball valve 31, an air atomization system 32, a bubble atomization system 33, a large groove type stirrer 34, a deflection plate 35, a second steam inlet pipe 36, a cooling water inlet pipe 37, a main water tank inlet pipe 38, a main reactor motor 39, a speed reduction system 40, an overpressure valve 41, an additive inlet hopper 42 and a second jacket 43.

The first stop valve 15 has the function of regulating the flow rate returning from the smaller reactor to the larger one, the small reactor motor 16 is used for agitation, its power depends on the volume of the vibrating tank, the liquid contained in the larger reactor is returned to the smaller reactor through the return pipe 17, the diameter of the return pipe 17 depends on the flow rate desired to be moved, and the latter depends on how fast the evacuation is carried out, the inner wall of the biomass bag 18 has pores or openings, its function is to contain solids rich in microorganisms and to allow the water to pass through while retaining these solids, the small tank agitator 19 is to maintain homogeneity and to ensure a more intimate contact between the two media (solids and liquid), it must be in such a way that the shear stresses generated on the suspension do not damage the microorganisms, the latter also being related to the number of turns of the agitator per unit of time. In this case, the stirrer is a square blade, the rotation speed is 120 rpm, the second stop valve 20 is used for regulating the flow from the large reactor to the small reactor, and the flow of the two reflux pumps must be the same in order to ensure the normal operation of the system. This is achieved by the regulation of the second 20 and first 15 stop valves, the first 21 ball valve is used to isolate the second 23 booster pump in repair and to stop the flow from small to large reactor, the first 22 booster pump allows the flow from large to small reactor, the size of which depends on the time allotted for the operation, the second 23 booster pump allows the flow from small to large reactor, the size of which depends on the time allotted for the operation, the second 24 ball valve is used to isolate the first 22 booster pump in repair and to stop the flow from large to small reactor, the flow of the conduit cutting off the third 25 ball valve is the flow into the product packaging or the next stage of processing, the fourth 26 ball valve is used to regulate the flow of steam into the large tank, the steam inlet 27 is used to inject steam for disinfecting the water used for extraction directly into the conduit, the function of the pipeline is to make two kinds of liquid contact, the air inlet pipe 28 is used to inject air to make the liquid fermentation continue, the ball valve five 29 is used to open or stop the air flow to the bigger tank, the ball valve six 30 can recover the hot steam condensation water, the heat recovery is carried out by the heat exchanger, the ball valve seven 31 can discharge the cooling water or the steam from the jacket, the air atomization system 32 is used to atomize the sterile air through the small opening of the round nozzle at the bottom of the big container for the liquid fermentation, the bubble atomization system 33 is used to ensure the intimate contact between the steam and the extraction water, thus the heat exchange is carried out, the device is composed of a zipper ball, the small opening is arranged on the zipper ball to atomize the steam, the large groove type stirrer 34 is used to keep the uniformity, the tight contact between the injected air and the microorganism suspension is ensured, the mode must be that the shearing stress generated on the suspension can not damage the microorganism, the latter is also related to the number of turns per unit of time of the stirrer, in this case a square blade, rotating at 120 rpm, deflector plates 35 are installed in order to ensure turbulent conditions during stirring, to prevent the circulation of the fluid in the form of a vortex, to improve the exchange between the liquid and gaseous media, second steam inlet pipe 36 has a ball valve to allow the passage of the fluid and to block the passage of the fluid towards the jacket of the large tank, this pipe being generated by a steam generator, which steam is used to slightly heat the mixture in the case of liquid fermentation, cooling water inlet pipe 37 to allow the circulation of cold water in the jacket when it is necessary to keep the content of the tank large at a certain temperature, main tank inlet pipe 38 to which the drinking water is connected, main reactor motor 39 for stirring, whose power depends on the volume of the tank, deceleration system 40 allows to modify the number of revolutions per unit of time of the stirrer from 60 to 150 rpm, the overpressure valve 41 is calibrated to ensure that there is no overpressure in the larger container, it opens when the internal pressure exceeds a set limit, the valve is calibrated to 1.5 bar, the anti-foaming agent and/or antibiotic enters through the additive inlet hopper 42, there is a ball valve in its lower part, allowing the entry of the elements added, the larger tank has a jacket two 43 for the cooling and heating liquid, in this case water and steam, to circulate.

The bag containing solids enriched with microorganisms is cylindrical and is fitted on its axis with a tube with small openings, as shown in figures 9-11, which allow the circulation of the fluid and thus improve the contact between the two media.

S3 liquid fermentation stage:

propagation of the biomass will be carried out in liquid medium. For this reason, the culture medium must have nutrient elements advantageous for growth and reproduction of Azospirillum azonian, and the components of the culture medium will be proportioned, which will make it possible to provide the necessary amount of nutrients to the microorganisms without surplus or defects, and the raw materials of the culture medium (Trichoderma) are shown in Table 1.

TABLE 1 media materials

Components	% P/P in the culture Medium
		A melon	95%
Potato pulp
		2%
Glucose
		1%
Corn flour
		1%
Rice
		1%

The amount of medium depends on the amount to be produced.

Dehulling-the nutrient for the culture medium, generally from tubers or the like, in which case potatoes are used. This process is carried out on a commercial mechanical debarker, the throughput of which depends on the volume of manufacture.

Size reduction-the media components were subjected to a disruption process and the equipment to perform this operation was commercial, with a final product size of 20 mesh.

Mixing in a reactor, wherein the components are mixed with water by stirring in the reactor.

Sterilization-this process is used to remove all unwanted microorganisms from the medium. Steam is injected into the mixture. The reaction tank was filled up to 80% and the remaining 20% was provided by condensed steam. After the mixture reached, it was boiled, and the steam injection was continued for 30 minutes.

Cooling in order to avoid contamination of microorganisms remaining during sterilization, the mixing is performed at a temperature of 60 to 25 c, and the process does not last for a long time. Furthermore, such hot mixtures require excessive time to cool due to thermal inertia. For this purpose, heat is exchanged by means of an external plate heat exchanger using water tubes as cooling liquid. The size and flow rate of the heat exchanger is a function of the bioreactor size and available cooling time.

Inoculation-the inoculation of the microorganisms obtained in the solid fermentation stage is carried out through a material feed hopper. The temperature of the medium should be between 25 ℃ and 30 ℃ at this time, and the liquid fermentation is started as such.

Liquid fermentation control of system parameters is important in this process. The temperature will be controlled by a thermometer inside the reactor. The pH will be controlled by a pH meter integrated into the system. The automatic system is responsible for reading these parameters and adjusting the temperature value by injecting steam into the jacket, and injecting a pH correction solution (diluting 1N (equivalent concentration, 1N is equivalent to 1 mol/L) NaOH solution) because Trichoderma naturally reduces the pH value of the culture medium with the increase of concentration, makes the culture medium acidic and reduces the growth rate, therefore the parameters need to be maintained between 5.5-6.5.

At the end of this process, there was a highly concentrated suspension of microorganisms (1X 10)⁹Individual microorganisms/ml) that will be packaged for sale in a liquid formulation or will be sent to the next process for the production of a solid formulation.

The container of the liquid product was chemically sterilized, washed with a chlorinated disinfectant (sodium hypochlorite solution) and rinsed three times with tap water.

The packaging operation can be performed manually or using filling equipment, depending on the volume to be processed. The only requirement is that the components used for the circulation of the suspension of packaged microorganisms are capable of being sterilized. There are also commercial choices in this regard.

Air compression the air compressor selected should provide commercially available lubricant-free air at a rate dependent on the volume of the fermentor and the requirements of the microorganisms being grown.

Air filtration sterilization employed a commercially available 0.2 micron pore size filter.

The reactor used was similar to the contactor device shown in figure 9.

S4 solid product stage:

the suspension of the product in a solid, such as spores, has the advantage over liquid products that the microorganisms are present in the form of spores, which leads to an extended shelf life due to the lower activity of the water, and a lower final density can be achieved at the same concentration, thus reducing the transportation costs. The firm support has a beneficial effect on the crop, it also interacts with the surrounding environment.

The powder of natural zeolite (particulate zeolite powder) and the microorganism suspension obtained in step S3 were contacted in a stirring tank as shown in fig. 12 to 14, and were continuously stirred. After 15 minutes of mixing, the process was complete and a product with a viscosity of 500cp was obtained.

The stirring tank comprises a second stirring motor 44, a coolant inlet 45, a third jacket 46, a product outlet 47, a refrigerant liquid outlet 48, a positive displacement pump 49, a stirrer 50 and a stirring rod 51.

The power of the second stirring motor 44 will depend on the size of the tank, considering that the product to be mixed is a viscous suspension, the speed of the motor should not exceed 50 rpm, so that the temperature does not increase, and cooling of the system is necessary because, when a relatively viscous mixture is produced, the temperature increases with the passage of the stirring time, the coolant will circulate through the jacket of the tank, the coolant circulates in the jacket three 46, exchanges heat with the fluid in the vessel, the coolant liquid passes through heat exchange, leaving the jacket at a higher temperature than the entering one, due to the viscosity, at the outlet of the tank there must be a positive displacement pump 49, which will carry the paste to the next operation, in a particular embodiment a screw pump, which is commercially available, the flow rate depends on the volume of the tank and the time we have allotted to the pump operation, the type of stirrer used for the stirrer 50 is commercially available, the diameter of the stirring rod 51 depends on the volume of the container.

The resulting product, having a viscosity of 500cp, was subjected to a drying operation in a drying chamber, in which sterile air was brought into lateral contact with the product in a tray. The inlet air temperature must not exceed 40 c and the equipment used is shown in fig. 15-17.

The apparatus includes hot air inlets 52, the hot air inlets 52 being distributed laterally downwardly within the trays 53 to all of the trays. The product thickness cannot exceed 0.5 cm and the distance between the pallet container shelves 54 is 5 cm. The gas collector 55 is in the middle of the combustion chamber.

The air heating process is carried out in a resistance mode, and is carried out immediately after air blowing is finished, so that the air inlet temperature can be absolutely controlled, which is a fundamental factor for the success of the drying process.

The air filter must be a sterile product with a pore size of 0.2 microns.

Grinding, namely grinding the compact dry solid obtained by drying to reduce the size of the product to 50 meshes. The mill used should be dry, it is preferably a hammer and the cutting force should be minimized.

Weighing, namely weighing the product by using a scale before the product is packaged.

And (4) packaging, wherein the final product is packaged by adopting a polyethylene aluminum melamine bag. The packaging can be completed manually or automatically by a machine according to different volumes, and is similar to the packaging of milk powder. The only assurance that is ensured is the sterility of these machines.

Sterilization a trichloroethylene bag manufacturer may be specifically asked to purchase sterilized rolls or logs of material when assembling the bag.

In addition, although there are other options to obtain a more concentrated product, the production costs are higher. Acceptable concentrations can be achieved by liquid fermentation. To concentrate more, the suspension is subjected to the action of a centrifuge. Different media used at different fermentation stages will produce different results in terms of final concentration.

In summary, according to the above technical scheme of the present invention, by using the microbial carrier-natural zeolite, the product has the characteristic of beneficial interaction with crops, and the preparation method of the zeolite bio-organic fertilizer of the present invention can make the concentration of microorganisms in the solid product at least ten times higher than that of the existing product in the process stages of solid fermentation, solid extraction, liquid fermentation, powder manufacturing, etc., so that the transportation cost is significantly lower, and the obtained high concentration product is more efficient in applying crops.

The above description is only for the purpose of illustrating the preferred embodiments of the present invention and is not to be construed as limiting the invention, and any modifications, equivalents, improvements and the like that fall within the spirit and principle of the present invention are intended to be included therein.

Claims

1. The zeolite bio-organic fertilizer is characterized by comprising zeolite, wherein the zeolite contains azospirillum, and the content of azospirillum in the zeolite is 1x10⁸Per gram.

2. The zeolite bio-organic fertilizer of claim 1 wherein said zeolite is a natural zeolite.

3. The preparation method of the zeolite bio-organic fertilizer of claim 1, which comprises the following steps:

4. The method for preparing zeolite bio-organic fertilizer according to claim 3, wherein the solid state fermentation process lasts for 7-10 days.

5. The method for preparing zeolite bio-organic fertilizer according to claim 3, wherein the pH value of the culture medium in step S3 is maintained between 5.5-6.5.

6. The method for preparing zeolite bio-organic fertilizer according to claim 3, wherein the drying temperature in step S4 is not higher than 40 ℃.