May I ask about the content in BB fertilizer?

Help, brother! How do I make mixed fertilizer? With a content of 15 each for nitrogen, phosphorus, and potassium

I. TEC ACES Process This method combines an aqueous solution circulation process with carbon dioxide stripping technology. It is characterized by a high ammonia/carbon dioxide ratio and a high conversion rate ； Plate trays are installed in the upper part of the stripping tower, while a liquid film heat exchanger is located in the lower part, resulting in high stripping efficiency ； The heat from the high-pressure ammonium methoxide condenser is used to recover by-product steam, resulting in a high heat utilization rate. Its process flow is described as follows. 1. Synthesis 　　Liquid ammonia supplied from outside is pressurized by a high-pressure ammonia pump and then fed into the urea synthesis tower via an ammonia preheater. 　　Carbon dioxide supplied from outside is compressed to 18.2 MPa by a carbon dioxide compressor and then sent to the air lift tower; air for corrosion prevention is added at the middle section of the carbon dioxide compressor. 　　The recycled ammonium methoxide solution from the recycling section is pumped by a high-pressure ammonium methoxide pump to Ammonium Methoxide Condenser No. 2 and the high-pressure washer. The operating pressure of the synthesis tower is 18.04 MPa, the operating temperature is 190°C, the molar ratio of ammonia to carbon dioxide is 4, the conversion rate of carbon dioxide is X%, and the products of the synthesis reaction overflow from the central tube and are discharged to the stripping tower at the bottom of the tower. At the upper part of the stripping tower, the synthetic urea solution from the synthesis tower comes into contact with carbon dioxide gas from the lower part, enabling effective carbon dioxide stripping. At the lower part of the stripping tower, ammonium carbamate and excess ammonia contained in the synthetic urea solution are decomposed and separated through carbon dioxide stripping and steam in a falling film heat exchanger. The operating pressure of the stripping tower is 18.04 MPa, and the temperature is 177°C; the gas at the top of the tower is sent to Ammonium Methane Condensers No. 1 and No. 2. 　　In the ammonium methanate condenser, the gas from the top of the stripping tower is condensed and absorbed by the recycled ammonium methanate solution. The heat of condensation and the heat of absorption are used to generate steam at 0.59 MPa in the No. 1 ammonium methanate condenser, as well as to heat the urea solution at the outlet of the stripping tower in the No. 2 ammonium methanate condenser. Both the gas and the solution at the bottom of the methylammonium condenser are sent to the synthesis tower. 　　The gas coming out of the top of the synthesis tower contains a small amount of ammonia and carbon dioxide, which is sent to a high-pressure scrubber for recovery. In the scrubber, ammonia and carbon dioxide are recovered using a circulating ammonium methoxide solution, which is then sent to Ammonium Methoxide Condenser No. 1 as an absorbent. The gas emerging from the top of the scrubber is sent to a high-pressure decomposer to further recover ammonia and carbon dioxide. 2. Purification The urea solution coming out of the bottom of the stripping tower is first preheated to 155°C in Condenser No. 2 using ammonia methanol, and then sent to the high-pressure decomposer. There, it is further heated by the steam condensate from the internal heat exchanger, which causes ammonium carbamate to decompose into gaseous ammonia and carbon dioxide. The resulting gases are then sent to the high-pressure absorption tower. After most of the ammonium carbamate is separated in the high-pressure decomposer, the urea solution is sent to the low-pressure decomposer at a pressure of 0.35 MPa, where it is further purified to achieve residual ammonia and carbon dioxide levels of 0.5% and 0.4%, respectively. 　　The gas separated by the low-pressure decomposer is sent to the low-pressure absorption tower, while the urea solution is sent to the flash separator for the final stage of purification; residual ammonia and carbon dioxide are further separated through vacuum flashing. 　　The urea solution at the outlet of the urea solution tank contains about 70% urea and about 0.4% ammonia; this urea solution is pumped by a urine pump to the concentration process. 3. Concentration and granulation The urea solution is first sent to a vacuum concentrator, where it is concentrated to about 84% urea. 　　The urea solution is heated to 132°C by low-pressure steam under a vacuum of 0.02 MPa, resulting in a urea concentration of 95.5% in the vacuum concentrator. The concentrated urea solution is sent to the final concentrator, where it is heated to 138°C by low-pressure steam. In the final separator, under a vacuum of 0.3 MPa, the solution is concentrated to contain 99.8% urea, and then it is pumped by a molten urea pump to the top of the granulation tower. Granules are sprayed into the tower through granulation nozzles; the urea that falls to the bottom of the tower is sent to a warehouse via conveyor belt for storage or packaging. 4. Recovery The overhead gas from the low-pressure decomposer is sent to the low-pressure absorption tower. The ammonium methanate solution formed in the high-pressure absorption tower is pumped by an ammonium methanate pump; part of it is circulated to the No. 2 ammonium methanate condenser, while the other part is circulated to the No. 1 ammonium methanate condenser via the scrubber tower in the synthesis section. 5. Treatment of process condensate The condensate from the surface condenser of the final concentrator is collected in a process condensate tank and then pumped via an absorption pump to the scrubber tower, where it is used to wash the off-gases from the high-pressure absorption tower. The process condensate from the first and second surface condensers is stored in a process condensate tank, and then pumped to a process condensate stripping tower via a process condensate pump. Ammonia and carbon dioxide are stripped from the condensate through steam stripping, and the gas at the top of the tower is sent to a low-pressure decomposer for recovery. The stripping condensate from the middle section of the process condenser stripper is pumped to the urea hydrolyzer, where the urea is completely hydrolyzed into ammonia and carbon dioxide. The process condensate from the urea hydrolyzer is sent back to the lower part of the process condensate stripping tower, where ammonia and carbon dioxide are stripped off. In the treated process condensate, the concentrations of urea and ammonia are both less than 1×10—6, allowing it to be used as boiler feed water after being sent out of the restricted area. II. TEC’s full-cycle improved Method C process: Its feature is that urine is first crystallized, and then melted and granulated to reduce dicyandiamide formation. 　　The process flow is briefly described as follows: 1. Urea synthesis Liquid ammonia from the outside is pressurized to 26 megapascals using a high-pressure liquid ammonia pump and then fed into the synthesis tower. 　　Carbon dioxide gas from outside is pressurized to 26 MPa by a carbon dioxide compressor and sent into the synthesis tower. 　　Ammonia and carbon dioxide react within the tower; the operating pressure of the synthesis tower is 25 MPa, the temperature at the top is 200°C, the ammonia/carbon dioxide ratio is 4, the water/carbon dioxide ratio is 0.37, and the conversion rate of carbon dioxide is 71.7%. 2. Decomposition and crystallization separation of urine (1) High-pressure decomposition: The reactants coming out of the top of the synthesis tower are depressurized to 1.7 megapascals using a pressure reducing valve before entering the high-pressure decomposition tower; heat is supplied by the reboiler in this tower. (2) Low-pressure decomposition: The solution coming out of the bottom of the high-pressure decomposition tower is depressurized to 0.25 megapascals via a level control valve and then enters the upper part of the low-pressure decomposition tower. There, sensible heat is used to vaporize some of the ammonia and carbon dioxide; these gases then enter the heat exchanger and reboiler simultaneously before returning to the packing section at the lower part of the low-pressure decomposition tower, where they come into countercurrent contact with the rising carbon dioxide gas, thereby facilitating further decomposition of methylammonium into ammonia and carbon dioxide. (3) Gas separation: The urea solution containing a small amount of ammonia and carbon dioxide, coming out from the bottom of the low-pressure decomposition tower, is further depressurized to 0.03 MPa and fed into the upper part of the gas separation tower. Ammonia and carbon dioxide separation is achieved using sensible heat. After flashing, it overflows to the lower part of the tower ； At the lower part of the tower, there is a packing section and a U-tube heater. The urine comes into countercurrent contact with air supplied by an exhaust gas recirculation blower via the packing, thereby enabling the separation of ammonia and carbon dioxide. Subsequently, the urine is heated using the U-tube heater, at which point its concentration reaches 74%. (4) Urine crystallization: The urea solution with a concentration of 74% coming out from the bottom of the gas separation tower is pumped to the crystallizer using a urine pump. Vacuum crystallization is employed in the upper part of the crystallizer; through vacuum evaporation in that upper section, the concentration of urine reaches 82%–86%. In the lower part of the crystallizer, crystalline urea is formed, along with concentrated urine containing this crystalline urea. This mixture is pumped to a centrifuge for separation. The crystalline urea obtained after centrifugation contains less than 2.4% water and 0.1% biuret. The reduction in the biuret content is achieved by adding biuret-containing washing water, which carries the biuret back into the mother liquor. The pseudo-mother liquor coming out of the centrifuge is collected in the mother liquor storage tank; a portion of it is pumped by the mother liquor pump into the low-pressure absorption tower and eventually returns to the synthesis tower, while the majority of it returns to the crystallizer for further concentration and crystallization. 3. Drying and granulation The powdered urea coming out of the centrifuge enters an air-flow dryer. It is transported to the top of the tower via air-conveying pipes, drawn in by the exhaust fan of the air-flow dryer located at the top of the granulation tower. There, the urea passes through a cyclone separator, where it is separated out and then sent to a melter. After being melted, the urea is fed to the nozzles in the granulation tower for granulation. Granular urea falls into the fluidized bed cooler, where it is cooled; after that, it overflows from the fluidized bed and is transported to a warehouse via belt conveyor for storage or packaging. 4. Recovery The ammonia and carbon dioxide separated in each decomposition tower are recovered separately and then returned to the synthesis tower. three ； Casale HEC urea process The HEC urea process is a patented technology of Casale Company, and its features include: (1) the use of two urea synthesis towers. The first tower is the main synthesis tower, with an operating pressure of 22–24 MPa, a temperature of 195°C, an ammonia/carbon dioxide ratio of 3.6, a water/carbon dioxide ratio of 0, and a carbon dioxide conversion rate of 75%. The second tower is an auxiliary synthesis tower, also known as a secondary tower; its operating pressure is 16 MPa, the temperature is 190°C, the ammonia/carbon dioxide ratio is 4.5, the water/carbon dioxide ratio is 1.3, and the carbon dioxide conversion rate is 61.0%. The average conversion rate of the two towers is 71%, which is higher than that of other urea production processes. (2) The equipment for medium-pressure and low-pressure recovery systems is small. (3) Lower material and energy consumption. Applying this method to the technical renovation of urea plants using the full-circulation process can reduce ammonia and steam consumption, resulting in good economic benefits. The evaporation system is similar to other processes; the process flows for the high-pressure section and the recovery section are described as follows: Carbon dioxide from outside the system is pressurized to 25 megapascals by a carbon dioxide compressor, and then mixed with liquid ammonia that has been pressurized by a high-pressure liquid ammonia pump. This mixture then enters the ammonium methanate condenser, where the reaction between ammonia and carbon dioxide generates heat used to produce low-pressure steam. After exiting the ammonium methanate condenser, the reaction mixture proceeds to the first synthesis tower. From the top of this tower, it goes to the separator in the high-pressure decomposer, which uses steam at 2.45 megapascals to facilitate gas stripping. The solution coming out of the upper part of the separator enters the second synthesis tower. The ammonium methoxide solution recovered from the medium-pressure absorber is pumped into the second synthesis tower using a high-pressure ammonium methoxide pump. The urea solution exiting the second synthesis tower is also sent to the separator in the upper part of the high-pressure decomposer. The urea solutions from tower 1 and tower 2 emerge at the bottom of the high-pressure decomposer and then enter the medium-pressure decomposer; from there they go on to the low-pressure decomposer. The urea solution coming out of the low-pressure decomposer is sent to an evaporator, where the water is removed under vacuum until the urea concentration reaches 4%. Afterwards, it is pumped to a granulation tower using a molten urea pump for granulation. The gas separated from the upper part of the low-pressure separator is sent to the low-pressure condenser; the ammonium carbonate solution emerging from the low-pressure condenser passes through a gas-liquid separator before being pumped by a low-pressure ammonium carbonate pump to the bottom of the medium-pressure absorption tower. 　　The gas coming out of the top of the second synthesis tower is sent to the separator in the upper part of the medium-pressure decomposer. The gas exiting the upper separator first has its heat recovered by the lower heater of a vaporizer, and then it is sent to the medium-pressure absorption tower where it comes into contact with liquid ammonia sprayed from the upper part of the tower; this results in the formation of ammonium methoxide solution, which is then pumped into the second synthesis tower using a high-pressure ammonium methoxide pump. The ammonia gas exiting from the top of the medium-pressure absorption tower is sent to the ammonia condenser, where it is condensed into liquid ammonia that then flows into the liquid ammonia storage tank for reuse

:'Is there a simple way to express it? In other words, if nitrogen, phosphorus, and potassium are each at 15 levels, then how much large-grained urea is needed? It’s made by mixing in potassium fertilizer – is that correct?

Domestically and internationally, research on fertilizers is being conducted; worldwide, the production and use of chemical fertilizers have undergone three phases of transformation. Before the 1960s, most of the chemical fertilizers produced were low-concentration fertilizers made of simple substances ； During the 1960s to 1980s, developed countries **developed high-concentration fertilizers and compound fertilizers ； In the past 20 years, developed countries have begun to focus on research into slow/controlled-release fertilizers, biofertilizers, organic compound fertilizers, and functional fertilizers, which have become hot topics in the research and development of new types of fertilizers. 1. Slow/controlled-release fertilizers: The main advantage of slow/controlled-release fertilizers is that the release of nutrients occurs simultaneously with their absorption by crops. This simplifies fertilization procedures, allowing a single application to meet the nutrient needs of crops throughout their growth period. There is less loss of fertilizer, higher utilization efficiency, and these fertilizers are environmentally friendly. Countries around the world are gradually realizing that one of the most effective measures to improve fertilizer utilization is to research new types of slow/controlled-release fertilizers. Since the 1980s, developed countries such as the United States, Japan, Europe, and Israel have shifted their research focus from scientific fertilization techniques to the development of new slow/controlled-release fertilizers, aiming to significantly improve fertilizer efficiency by altering the properties of the fertilizers themselves. Slow/controlled-release fertilizers are regarded as an important development direction for the fertilizer industry in the 21st century. Currently, there are mainly the following 4 types of slow/controlled-release fertilizers. (1) Encapsulated slow/controlled-release fertilizers ； Encapsulated slow/controlled-release fertilizers mainly consist of an encapsulating material applied to the surface of the fertilizer particles to regulate the release of nutrients. In 1957, the United States was the first to conduct research on sulfur-coated urea. In 1961, TVA carried out pilot tests on sulfur-coated urea (SCU) using a plant with a capacity of 1–7 kg/h. In 1978, a demonstration plant for SCU with a capacity of 10 t/h was built in the United States. Meanwhile, research was also conducted on potassium thiosulfate chloride (SCK) and diammonium thiosulfate phosphate (SCP). Sulfur-coated urea remains the leading product in the United States at present. The United States was also the first country to commercially produce resin-coated fertilizers. In 1967, the alkyd resin-coated fertilizer Osmocote was produced in California, and it has since become a renowned brand of controlled-release fertilizer worldwide. Japan began researching coated controlled-release fertilizers in the 1960s. After the 1970s, focus was placed on researching thermoplastic resin polyolefin-coated fertilizers, commonly referred to as the POCF process. By adjusting the ratio of PE to EVA and using inorganic fillers as pore-forming agents, film-based controlled-release fertilizers with release periods ranging from 40 to 360 days can be produced. The development of biodegradable polymer coating materials and the research on fertilizers with different nutrient release patterns represent the research directions in coated fertilizers. Since the 1980s, countries such as Israel, Germany, the United Kingdom, Canada, Italy, and India have also carried out research on coated slow/controlled-release fertilizers, attempting to use polymers, peat, lignin, paraffin, inorganic nutrient materials, etc. to coat urea and other substances in order to create slow/controlled-release fertilizers. The first symposium on ring/controlled-release fertilizers was held in Shefferld, Alabama, United States, in July 1991 ； In 1993, an international seminar on controlled/retarded-release fertilizers was also held in Israel. Currently, the global consumption of slow/controlled-release fertilizers amounts to 1 million tons in terms of physical volume, with coated fertilizers accounting for more than half of this amount; in some cases, this proportion exceeds 90%. Synthetic micro-fibrous slow-release fertilizers: One type consists of synthetically derived organic nitrogen compounds that are slightly soluble in water, such as urea-formaldehyde fertilizers (Ureaform), isobutylidene diurea (IDBU), and cyanoacrylate diurea (CDU), among others ； Another category consists of slightly water-soluble or citrate-soluble synthetic inorganic fertilizers, such as partially acidified phosphate rock (PAPR) and ammonium potassium phosphates of divalent metals. Urea-formaldehyde compounds and fertilizer-releasing agents are the condensation of urea with aldehydes, with urea formaldehyde (UF) being the most common one. In 1924, Germany’s Badische Anilin and Sodawerke company obtained the first patent for the production of urea-based fertilizers, and industrial production began in 1955. Germany published a process for the preparation of levulinic aldehyde and urea in 1924. Mitsubishi Corporation of Japan filed a patent in 1961–1962 for the production of isobutylidene diurea (IBDU) via the reaction of urea and isobutyraldehyde, and starting in 1964, it was sold in small quantities on the Japanese market. In the early 1990s, century slow/controlled-release fertilizers still relied mainly on soluble urea derivatives, accounting for over 50%. Europe traditionally uses slightly soluble urea-based compounds as slow-release fertilizers. Its proportion accounts for over 70% of the sales volume of slow-release fertilizers. Furthermore, fertilizer is affected significantly by factors such as soil moisture, pH, and microorganisms in terms of the rate at which nutrients are released; moreover, it is expensive, which has led to a declining demand for such fertilizers. Chemically inhibitory slow-release fertilizers regulate the activity of soil microorganisms by adding urease inhibitors and nitrification inhibitors, thereby slowing down the hydrolysis of urea and the nitrification of ammonia nitrogen, and thus achieving a gradual release of nitrogen from the fertilizer ； In the 1960s, efforts to screen for soil urease inhibitors began to gain attention. HQ (hydroquinone), NB-PT (N-butyl thiophosphoryltrimine), PPD (o-phenylphosphoryldiamine), TPTA (thiophosphoryltrimine), CHPT (T-tricyclammonium phosphate), etc., are important soil urease inhibitors for screening studies. Since the 1950s, foreign countries have begun to develop nitration inhibitors; the main products studied include derivatives of pyridine, pyrimidine, thiourea, thiazole, mercury, etc., as well as potassium dinitrinate, chlorobenzene isothiocyanate, hexachloroethane, sodium pentachlorophenate, and others. Dicyandiamide (DCD) is a widely used nitrification inhibitor in situations where the utilization efficiency of nitrogen fertilizers is already high. Matrix compound fertilizers and adhesive slow-release/controlled-release fertilizers involve mixing fertilizer nutrients with substances that can reduce their solubility; through processes such as complexation and cementation, fertilizers that release nutrients slowly are created. In particular, organic polymer materials, modified peat and weathered coal, as well as organic substances combined with fertilizers, are used for binding purposes to alter the rate at which nutrients are released, thereby creating slow-release fertilizers. Currently, research in this field is focused on slow-release fertilizers, and the prospects are promising. Furthermore, the use of slow-release fertilizers of different types and release rates, combined with \"heterogeneous rate control,\" to maximize the synchronization between the nutrient release pattern of these fertilizers and the uptake by crops, is given widespread attention in the research and application of slow-release fertilizers. Currently, the global annual consumption of slow/controlled-release fertilizers is around 1 million tons. Of this amount, the United States and Canada account for 600,000 tons per month (about 60%), Japan accounts for 200,000 tons per month (about 20%), Western Europe and Israel account for 150,000 tons per month (about 15%), while other regions consume more than 50,000 tons per month. This figure is significantly higher than the growth rate of conventional fertilizers on a seasonal basis. At present, the main issue affecting the development of slow/controlled-release fertilizers is price. Due to their high price, controlled-release fertilizers are used in non-agricultural markets such as lawns and nurseries in the United States and Western Europe, as well as in Japan. Reducing production costs and enabling use in field crops are important directions in the development and production of slow/controlled-release fertilizers. Research on slow/controlled-release fertilizers in our country started relatively late; in the 1970s, the Nanjing Institute of Soil Science of the Chinese Academy of Sciences conducted research on the development of long-acting ammonium carbonate. Entering the 1980s, and especially in recent years, as the use of chemical fertilizers has increased while their efficiency has declined, leading to greater pollution of agricultural products and the environment by these fertilizers, research on slow/controlled-release fertilizers in China has accelerated. Starting in 1983, Zhengzhou Institute of Technology and other institutions in China took the lead in systematically developing coated controlled-release fertilizers using nutrient-coating technologies. They successively created three improved versions of such products: calcium-magnesium-phosphorus fertilizer coating urea (1983), partially acidified phosphate rock coating urea (1991), and ammonium potassium phosphates of divalent metals coating urea (1995). The time over which nutrients are released under controlled conditions exceeded 95 days, overcoming the major technical challenges related to controlling nutrient release in coated materials, both domestically and internationally. An industrial production line with an annual output capacity of 10,000 tons has been developed; the product is branded as Luxacote and is exported to the United States, Australia, Singapore, Japan, and other countries, ranking alongside OsmoCote, MEISTER, and Nutri-Cote. Currently, with funding from the **863 Program**, efforts are being made to further reduce costs, with a focus on developing specialized controlled-release fertilizers suitable for field crops. These products have been tested on a large scale in corn fields in regions such as Henan and Shandong, resulting in yield increases of over 10%, as well as a 10-percentage-point increase in fertilizer efficiency. In the development of resin-coated controlled-release fertilizers, China mainly draws on Japanese experience. Starting in 1992, the Beijing Academy of Agriculture and Forestry Sciences took the lead in systematically conducting research on urea coated with resin. Based on the adoption of Japanese technology, significant improvements and breakthroughs have been achieved in areas such as solvents, coating materials, and equipment. The study identified low-toxicity solvents with a recovery rate of over 98% ； Continuous production equipment has been developed to apply for a **patent. A cheap polyacrylamide is selected as the coating material and modified through degradation. At present, a urea-coated resin production line with an annual capacity of over 3,000 tons has been established, capable of producing a range of coated ureas with nutrient release durations of 30 to 200 days or longer. These products come in linear and S-shaped release patterns. Using coated urea as the base material, N, P, and K compound controlled-release fertilizers were formulated through heterogeneous rate variation technology. These fertilizers were tested on a large scale in crops such as rice and corn in Beijing, the Northeast, Shandong, Guangdong, and other regions, with good results obtained. The product received the **Key New Product Certificate in 2002. The Institute of Soil and Fertilizer Science of the Chinese Academy of Agricultural Sciences, South China Agricultural University, and other institutions have carried out extensive research on substrate composition, controlled-release mechanisms via cementation, the development of coating materials – particularly those made from industrial and agricultural waste – as well as on film-forming processes and mechanisms. They have also worked on the development of multi-functional controlled-release fertilizers with properties such as organic composition, water retention, and disease prevention. A reaction film-forming technology was invented to produce coated controlled-release materials using equipment that operates at room temperature. The matrix-composite, water-retaining controlled-release fertilizers developed were demonstrated on a large scale in crops such as corn in Shandong, as well as vegetables and cotton in Guangdong and Xinjiang. The Shenyang Applied Ecology Research Institute has also carried out extensive work on developing slow-release fertilizers using urease inhibitors and nitrification inhibitors, and these products have been demonstrated in field crops. In addition, China Agricultural University has conducted extensive research on the release mechanisms and evaluation of controlled-release fertilizers. The Institute of Soil and Fertilizer Science, Chinese Academy of Agricultural Sciences, has taken the lead in China in carrying out long-term field studies on slow-release fertilizers at its \"Long-Term Monitoring Site for Soil Fertility and Fertilizer Efficiency in Brown Soil.\" Following the long-term field experiments with conventional chemical fertilizers, these studies hold great value for conducting fundamental research on the evolution of the efficacy of slow-release fertilizers as well as their environmental impact. Although research on slow/controlled-release fertilizers in our country started relatively late, it features distinct characteristics, with a wide range of products and technologies such as resin coating, nutrient material encapsulation, matrix compounding, cementation-based controlled release, and enzymatic inhibition. Especially in recent years, **the government and local authorities** have attached great importance to the research and industrialization of new slow/controlled-release fertilizers. The project \"Development and Industrialization of Environmentally Friendly Fertilizers\" under the 863 Program during the 10th Five-Year Plan period (2001AA246023), jointly undertaken by five institutions including the Institute of Soil and Fertilizer Science of the Chinese Academy of Agricultural Sciences, China Agricultural University, South China Agricultural University, Zhengzhou University, and the Beijing Academy of Agriculture and Forestry Sciences, aims to introduce controlled-release fertilizers into field crops. To date, more than 10 related invention patents have been obtained or applied for; over 50 products at various development stages – industrial-scale, pilot-scale, and laboratory-scale – have been developed. Additionally, three production lines capable of manufacturing controlled-release fertilizers in quantities exceeding 10,000 tons per year have been established, with functions including the coating of nutrients with resins and the creation of composite substrates. The cost of these products is only 1/4 or less than that of similar foreign products. They have been widely demonstrated in the cultivation of crops such as rice, corn, vegetables, and cotton in regions including the Northeast, Beijing, Shandong, Henan, Xinjiang, and Guangdong; some of these products have been exported to countries such as the United States, Japan, Singapore, and Australia. China’s controlled-release fertilizer technology is generally not on par with that of developed countries, especially in terms of industrialization. At present, China’s annual consumption of slow/controlled-release fertilizers is around 20,000 tons in terms of physical volume. The main brands available on the market include Osmocote and Osmocoteplus from the United States, MESTER and Nutricote from Japan, as well as Multicote from Israel – all of these are coated controlled-release fertilizers, with market prices exceeding 10,000 yuan per ton. China’s current industrial production capacity for slow/controlled-release fertilizers exceeds 100,000 tons, but the utilization rate is low

Reply to Floor 1: It depends on the nitrogen, phosphorus, and potassium content in the raw materials you choose. In simple terms, urea, diammonium compounds, and potassium fertilizers are mixed together in certain proportions.

If granular diammonium phosphate (14-43-0), granular potassium chloride (0-0-60), large-grain urea (46-0-0), and large-grain filler are used, then per bag the composition is 17.45 kilograms of granular diammonium phosphate (14-43-0), 12.5 kilograms of granular potassium chloride (0-0-60), 11.00 kilograms of large-grain urea (46-0-0), and 9.05 kilograms of large-grain filler.