CN1154613C - Flexible process for preparing different kinds of phosphate - Google Patents
Flexible process for preparing different kinds of phosphate Download PDFInfo
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- CN1154613C CN1154613C CNB001126938A CN00112693A CN1154613C CN 1154613 C CN1154613 C CN 1154613C CN B001126938 A CNB001126938 A CN B001126938A CN 00112693 A CN00112693 A CN 00112693A CN 1154613 C CN1154613 C CN 1154613C
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Abstract
The present invention relates to a flexible production method for preparing various kinds of phosphate, particularly to a method for producing various kinds of phosphate on one production line, which belongs to a method for producing phosphate. The present invention adopts a two-step method (desiccation and polymerization)to produce the phosphate. Orthophosphate powders obtained by desiccation are respectively conveyed in a production line of which the polymerization temperature is more than 550 DEG C and a production line of which the polymerization temperature is less than 550 DEG C for polymerization. Finally, various kinds of phosphate can be produced. The present invention has the advantages of little device investment, high product quality, multiple products and low producing power consumption.
Description
The present invention belongs to a method for producing phosphate, particularly to a method for producing various phosphates in a production line.
At present, the domestic method for producing phosphate is a one-step drying polymerization method, phosphoric acid is directly dried and polymerized after reacting with alkali, only 1-3 products can be produced on one production line by the method, the method is difficult to adapt to the changing market demand, the quality of the produced products is poor, the food-grade standard is difficult to meet, in addition, the energy consumption in production is high, and the product cost is increased.
The invention aims to provide a flexible production method for preparing various phosphates, which can simultaneously prepare various phosphates on one production line, reduce the investment of equipment, improve the quality of products and reduce the energy consumption of production.
The process steps for realizing the purpose of the invention are as follows:
(1) neutralizing, adding phosphoric acid and alkali into a neutralizing tank after respectively metering, reacting under stirring, pumping water vapor out of the neutralizing tank by a fan, adding phosphoric acid and alkali, adjusting the pH value and Na/P (or K/P) of a neutralizing solution to required values, and pumping into an intermediate tank;
(2) drying, namely drying the neutralized liquid from the intermediate tank into orthophosphate dry powder by using a dryer, and conveying the orthophosphate dry powder into a coking furnace or/and a melting furnace;
(3) ①, when producing phosphate products with drying or polymerization temperature less than 550 ℃, drying and polymerizing by a coking furnace, indirectly heating by hot gas from a hot blast stove by the coking furnace, and when producing phosphate products with polymerization temperature more than 550 ℃, polymerizing by a melting furnace by ②;
(4) and (4) processing a finished product, quenching after polymerization is finished, and crushing to obtain the finished product.
And when the neutralization solution is in the intermediate tank, the temperature is kept at 70-90 ℃ to avoid crystallization. The hot gas from the coking furnace is exhausted into the atmosphere except a small amount, and most of the hot gas is returned to the hot blast stove for cyclic utilization, so that the energy consumption in production is reduced.
The present invention prepares orthophosphate dry powder, and then polymerizes in a coking furnace or/and a melting furnace according to the different polymerization temperatures of various products, so that various different phosphate products can be produced simultaneously.
The technical solution of the present invention will be described in further detail with reference to the accompanying drawings and several embodiments of the present invention.
FIG. 1 is a process scheme of the flexible production process of various phosphates according to the present invention.
Example 1: production of sodium hexametaphosphate
Respectively adding 1130 kg of 40 deg.C 85% industrial grade or food grade phosphoric acid and 1363 kg of 40 deg.C 30% industrial grade or food grade caustic soda (sodium hydroxide) into a neutralization tank, and neutralizing under stirringReaction formula ). And pumping water vapor in the neutralization tank by using a fan, removing heat generated by the reaction, and keeping the temperature of the neutralization liquid at 70-120 ℃. Adding caustic soda or phosphoric acid, and adjusting the pH value of the neutralization solution to 5.0-5.4. And then pumping the neutralization solution into a high-level intermediate tank, wherein the intermediate tank is provided with a heat preservation device, so that the temperature is kept between 70 and 90 ℃, and the neutralization solution is prevented from crystallizing in the intermediate tank to influence the quality of the product. The neutralizing liquid flowing out of the high-level middle tank is dried by a scraper dryer at 150 ℃ to form sodium dihydrogen phosphate dry powder with the water content of less than 3.5 percent. Feeding sodium dihydrogen phosphate dry powderMelting and polymerizing for 20 minutes in a melting furnace at 750-850 ℃ (the polymerization reaction formula is ]. And then quenching the hexa-partial melt from the melting furnace to 60-80 ℃ in 3-5 seconds, and then crushing, sieving and the like to obtain one ton of products.
Example 2: production of sodium pyrophosphate
870 kg of 40 ℃ 85% industrial grade or food grade phosphoric acid and 2033 kg of 40 ℃ 30% industrial grade or food grade caustic soda (sodium hydroxide) are respectively added into a neutralization tank and subjected to neutralization reaction under the stirring action (reaction formula) ). And pumping water vapor in the neutralization tank by using a fan, removing heat generated by the reaction, and keeping the temperature of the neutralization liquid at 70-120 ℃. Adding caustic soda or phosphoric acid, and adjusting the pH value of the neutralization solution to 9.10-9.40. And then pumping the neutralization solution into a high-level intermediate tank, wherein the intermediate tank is provided with a heat preservation device, so that the temperature is kept between 70 and 90 ℃, and the neutralization solution is prevented from crystallizing in the intermediate tank to influence the quality of the product. The neutralizing liquid flowing out of the high-level middle tank is dried by a scraper dryer at 150 ℃ to form disodium hydrogen phosphate dry powder with the water content of less than 3.5 percent. And (3) delivering the disodium hydrogen phosphate dry powder to a coking furnace at 160-240 ℃, coking for 30 minutes, and providing heat by the coking furnace through hot air generated by a hot blast stove with a kerosene burner. The hot air and the heated material are not in direct contact in the coking furnace, the heat is transferred in an indirect mode, most of the hot air from the coking furnace is pressurized by a high-temperature fan and returns to the hot blast stove except for a small part of the exhausted hot air, and the hot air is mixed with the hot air newly generated by the kerosene burner so as to reduce the energy consumption. Then cooling the sodium pyrophosphate from the coking furnace by a blade cooler, and then crushing, sieving and other processes to obtain one ton of products.
Example 3: production of sodium acid pyrophosphate
870 kg of 40 ℃ 85% industrial grade or food grade phosphoric acid and 2033 kg of 40 ℃ 30% industrial grade or food grade caustic soda (sodium hydroxide) are respectively added into a neutralization tank and subjected to neutralization reaction under the stirring action (reaction formula) ). And pumping water vapor in the neutralization tank by using a fan, removing heat generated by the reaction, and keeping the temperature of the neutralization liquid at 70-120 ℃. Adding caustic soda or phosphoric acid, and adjusting the pH value of the neutralization solution to 5.0-5.4. And then pumping the neutralization solution into a high-level intermediate tank, wherein the intermediate tank is provided with a heat preservation device, so that the temperature is kept between 70 and 90 ℃, and the neutralization solution is prevented from crystallizing in the intermediate tank to influence the quality of the product. The neutralizing liquid flowing out of the high-level middle tank is dried by a scraper dryer at 150 ℃ to form disodium hydrogen phosphate dry powder with the water content of less than 3.5 percent. Delivering the disodium hydrogen phosphate dry powder into a coking furnace at 220-250 ℃, coking for 30 minutes,the coking furnace is supplied with heat by hot air generated from a hot blast stove with a kerosene burner. The hot air and the heated material are not in direct contact in the coking furnace, the heat is transferred in an indirect mode, most of the hot air from the coking furnace is pressurized by a high-temperature fan and returns to the hot blast stove except for a small part of the exhausted hot air, and the hot air is mixed with the hot air newly generated by the kerosene burner so as to reduce the energy consumption. Then cooling the sodium pyrophosphate from the coking furnace by a blade cooler, and then crushing, sieving and other processes to obtain one ton of products.
According to the technical scheme of the invention, as the two-step method is adopted for production, more than ten phosphate products can be produced on one production line, the products comprise monosodium phosphate, disodium phosphate, trisodium phosphate, sodium pyrophosphate, sodium acid pyrophosphate and the like when the polymerization temperature is less than 550 ℃, and the products comprise sodium hexametaphosphate, sodium tetrapolyphosphate, sodium acid hexametaphosphate and the like when the polymerization temperature is more than 550 ℃, so that the changing requirements of the market on various products can be met, and the additional investment cost for preparing various products is reduced; the indirect heating mode is adopted, the temperature is easily controlled, the product is prevented from being polluted by a heating medium, the product quality can be improved, meanwhile, the hot air is easily recycled, the production energy consumption is reduced, and the product cost is reduced.
Claims (2)
1. A flexible production method for preparing various phosphates is characterized by comprising the following process steps:
(1) neutralizing, adding phosphoric acid and caustic soda after respectively metering, adding into a neutralizing tank, stirring for reaction, pumping water vapor in the neutralizing tank by using a fan, adding phosphoric acid and alkali, adjusting the pH value and Na/P of a neutralizing solution to required values, and pumping into an intermediate tank, wherein the temperature of the neutralizing solution in the intermediate tank is kept at 70-90 ℃;
(2) drying, namely drying the neutralized liquid from the intermediate tank into orthophosphate dry powder by using a dryer, and conveying the orthophosphate dry powder into a coking furnace or/and a melting furnace;
(3) ①, when producing phosphate products with drying or polymerization temperature less than 550 ℃, drying and polymerizing by a coking furnace, indirectly heating by hot gas from a hot blast stove by the coking furnace, and when producing phosphate products with polymerization temperature more than 550 ℃, polymerizing by a melting furnace by ②;
(4) and (4) processing a finished product, quenching after polymerization is finished, and crushing to obtain the finished product.
2. The flexible process of claim 1 wherein the hot gas from the coke oven is recycled to the hot blast stove for a major portion.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB001126938A CN1154613C (en) | 2000-02-17 | 2000-02-17 | Flexible process for preparing different kinds of phosphate |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB001126938A CN1154613C (en) | 2000-02-17 | 2000-02-17 | Flexible process for preparing different kinds of phosphate |
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| Publication Number | Publication Date |
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| CN1309080A CN1309080A (en) | 2001-08-22 |
| CN1154613C true CN1154613C (en) | 2004-06-23 |
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| CNB001126938A Expired - Fee Related CN1154613C (en) | 2000-02-17 | 2000-02-17 | Flexible process for preparing different kinds of phosphate |
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Families Citing this family (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102951625A (en) * | 2011-08-25 | 2013-03-06 | 贵州省惠水磷酸盐厂 | Sodium pyrophosphate preparation technology |
| CN105329871B (en) * | 2015-11-02 | 2017-11-07 | 湖北兴发化工集团股份有限公司 | A kind of production method of Instant calgon |
| CN106348272B (en) * | 2016-09-23 | 2018-06-08 | 武汉工程大学 | The technique that a kind of solid phosphoric acid potassium dihydrogen melting arsenic removal prepares food-grade potassium metaphosphate |
| CN111302321A (en) * | 2020-04-10 | 2020-06-19 | 上海太洋科技有限公司 | Preparation method of optical-grade sodium metaphosphate |
| CN112978699B (en) * | 2021-02-22 | 2022-09-02 | 徐州恒世食品有限公司 | Low-energy-consumption production system and production method suitable for various phosphates |
| CN113173568B (en) * | 2021-05-07 | 2023-03-14 | 云南莱德福科技有限公司 | Trisodium pyrophosphate anhydride and preparation method and application thereof |
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Granted publication date: 20040623 |