CN112142602B - Continuous treatment method for acesulfame potassium waste acid - Google Patents
Continuous treatment method for acesulfame potassium waste acid Download PDFInfo
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Abstract
The invention belongs to the field of chemical production, and particularly provides a continuous treatment method of acesulfame potassium waste acid, which comprises the following steps: 1) Performing continuous neutralization reaction on ammonia gas or liquid ammonia and waste acid; 2) The neutralized waste acid enters a triethylamine dissociation tower, the waste acid is continuously dissociated in the tower, dissociated triethylamine-water is conveyed to a separator, an ammonium sulfate solution after triethylamine dissociation is pumped out from a dissociation tower kettle, and the liquid level of the tower kettle is maintained to be balanced; 3) And (3) feeding waste acid obtained after triethylamine dissociation into a continuous ammonia distillation tower, combining an ammonium sulfate solution obtained after ammonia distillation with a sulfuric acid absorption solution obtained after ammonia distillation, performing continuous pretreatment, and continuously evaporating to obtain a qualified ammonium sulfate byproduct. According to the invention, by accurately controlling the pH value of neutralization separation, triethylamine in waste acid is efficiently recovered, and the recovered triethylamine has high purity and economic value; the continuous integrated treatment of the acesulfame potassium waste acid is realized, the waste acid treatment efficiency is greatly improved, the treatment cost is reduced, and the safety and stability of the treatment process are ensured.
Description
Technical Field
The invention belongs to the field of chemical industry, and particularly relates to a continuous processing method of acesulfame potassium waste acid.
Background
Acesulfame potassium (acesulfame potassium) also known as acesulfame potassium: acesulfame potassium; 6-methyl-1,2, 3-oxaoxazin-4- (3H) -one-2, 2-dioxide; 6-methyl-1,2, 3-oxazin-4- (3H) -one-2, 2-dioxy potassium salt; 6-methyl-1,2, 3-oxooxazin-4- (3H) -one-2, 2-dioxopotassium salt; 6-methyl-2, 2-dioxo-1, 2, 3-oxysulfideAza; acesulfame potassium; 6-methyl-1,2, 3-oxazin-4- (3H) -one-2, 2-dioxypotassium salt; AK sugar english name: RARECHEM AM UC 0205; SWEET ONE; SUNETTE; POTASSIUM 6-METHYL-1,2,3-OXATHIAZIN-4 (3H) -ONE 2,2-DIOXIDE;6-methyl-3,4-dihydro-1,2,3-oxathiazin-4-one 2,2-dioxide; acesulfame; ACESULFAME K; ACESULFAME potatosium, appearance properties: white crystalline powder, readily soluble in water, slightly soluble in ethanol. CAS number 55589-62-3; the molecular formula is C4H4KNON4SK; the molecular weight is 201.2; melting point: 225 °; water solubility: 270g/Lat 20 ℃; density: 1.81; structural formula (la):
action and use: the product has strong sweet taste, sweetness about 130 times that of sucrose, and taste similar to saccharin. At high concentrations, the tea has a bitter taste. It has no moisture absorption, is stable at room temperature, and has good mixing property with sugar alcohol, sucrose, etc. As a non-nutritive sweetener, it can be widely used in various foods. According to the regulation of GB2760-90 in China, the product can be used for liquid, solid beverage, ice cream, cake, jam, pickles, sweetmeat, chewing gum and table sweetener, and the maximum use amount is 0.3g/kg.
The prior art treatment process comprises the following steps: the waste acid generated in the preparation process of the acesulfame potassium contains triethylamine sulfate, sulfuric acid, organic impurities, water and the like, and the COD and the acidity are too high, so that the direct discharge can harm the environment, and the triethylamine in the waste acid has certain economic value, so that the research on the method for treating the acesulfame potassium waste acid is of great significance. The existing acesulfame potassium waste acid treatment process is a batch gypsum process, calcium hydroxide aqueous solution and waste acid are adopted for neutralization, triethylamine in the waste water is recovered, and the obtained calcium sulfate is sold as a byproduct.
In the patent 'method for recovering triethylamine as a catalyst in acesulfame potassium production', stone powder (calcium carbonate) aqueous solution and waste acid are adopted for neutralizing and recovering triethylamine, a large amount of non-condensable gas carbon dioxide is generated in the neutralizing step of the process, more triethylamine is brought into system tail gas, the triethylamine recovery rate is low, and the process is an intermittent operation process;
in the patent of 'a process for recovering a catalyst used in the process of synthesizing acesulfame potassium', a calcium hydroxide aqueous solution is adopted for neutralizing and recovering triethylamine, so that the triethylamine recovery rate is low, the water content is high, the environmental pollution is high, the operation process is complicated, and the treatment capacity is low.
Disclosure of Invention
The invention aims to provide a method for continuously treating acesulfame potassium waste acid, which is characterized in that the waste acid generated in the process of preparing acesulfame potassium contains triethylamine sulfate, sulfuric acid, organic impurities, water and the like, the COD and acidity are too high, the environment can be harmed by direct discharge, and triethylamine in the waste acid has a certain economic value, so that the research on the method for continuously treating acesulfame potassium waste acid is of great significance.
The technical scheme of the invention is as follows:
a continuous processing method of acesulfame potassium waste acid comprises the following steps:
1) Firstly, ammonia gas or liquid ammonia and waste acid are subjected to continuous neutralization reaction in a continuous reactor, wherein the mass concentration of the sulfuric acid in the waste acid is 10-30%, the mass concentration of triethylamine sulfate is 5-20%, and the molar ratio n (ammonia): n (sulfuric acid) = 2-3, neutralization is carried out until the pH is 4-9, and the neutralization reaction pressure is 0-2 MPa (including the pressure of 0, when the range pressure is 0, the normal pressure is expressed)
2) And (2) feeding the neutralized waste acid into a triethylamine dissociation tower from the middle upper part of the tower, feeding ammonia gas or liquid ammonia into the triethylamine dissociation tower from the middle lower part of the tower, and continuously dissociating the waste acid in the tower, wherein the molar ratio of n (ammonia): n (triethylamine sulfate) = 2-3, dissociated triethylamine-water is conveyed to a separator, crude triethylamine on the upper layer is separated and then enters a rectification dehydration process, water on the lower layer flows back to a tower, the temperature of a tower kettle is controlled to be 75-110 ℃, the PH of a kettle liquid is more than or equal to 8, the pressure of a dissociation tower system is 0.1-2 MPa, an ammonium sulfate solution after triethylamine dissociation is pumped out of the dissociation tower kettle, the liquid level of the tower kettle is maintained to be balanced, and v (neutralization solution) = v (dissociation solution);
3) The waste acid after triethylamine dissociation is ammonium sulfate-containing solution, the ammonium sulfate-containing solution is pumped into a continuous ammonia still, the temperature of a tower kettle is controlled to be 100-110 ℃, the total reflux is carried out on the top of the tower, the evaporated ammonia is absorbed by sulfuric acid, the tower kettle liquid is pumped out, v (dissociation liquid) = v (solution after ammonia distillation) maintains the liquid level balance of the tower kettle, the PH of the tower kettle liquid is controlled to be 4-6, and the system pressure of the ammonia still is 0.1-2 MPa; the ammonium sulfate solution after ammonia distillation is combined with the sulfuric acid absorption liquid after ammonia distillation, and then the mixture is subjected to continuous pretreatment and continuous evaporation, and meanwhile, a qualified ammonium sulfate byproduct is prepared.
Further, the feeding temperature of the waste acid in the step 1) is 10-60 ℃, the retention time of neutralization is 5 s-3 h, and the discharging temperature of the neutralized waste acid is 65-95 ℃.
Further, the continuous reactor is a continuous flow reactor such as a kettle type continuous reactor, a tubular reactor, a tower type continuous reactor or a micro-channel reactor.
Further, after the crude triethylamine on the upper layer in the step 2) is separated, the crude triethylamine enters a rectification dehydration process, the recovery rate of the triethylamine reaches 95-98%, and the content of the triethylamine is 99.8-99.9%.
Further, the residence time of the continuous dissociation in the step 2) is 0.5 to 8 hours.
Further, the retention time of the continuous ammonia distillation in the step 3) is 0.5-8h,
furthermore, the feeding temperature of the waste acid in the step 1) is 30-60 ℃, the retention time of neutralization is 15 min-1.5 h, and the discharging temperature of the neutralized waste acid is 70-90 ℃.
Furthermore, the residence time of the continuous dissociation in the step 2) is 2 to 6 hours.
Furthermore, the retention time of the continuous ammonia distillation in the step 3) is 1-5 h.
The invention relates to a continuous processing method of acesulfame potassium waste acid, which comprises the following steps:
1) Firstly, ammonia gas or liquid ammonia with a certain flow rate and waste acid (in a continuous reactor) with a certain flow rate are subjected to continuous neutralization reaction, wherein the mass concentration of sulfuric acid in the waste acid is 10-30%, the mass concentration of triethylamine sulfate is 5-20%, and n (ammonia): n (sulfuric acid) = 2-3 (molar ratio), the feeding temperature of waste acid is 10-60 ℃, wherein the continuous reactor is a continuous flow reactor such as a kettle type continuous reactor, a tubular reactor, a tower type continuous reactor or a microchannel reactor, the neutralization is carried out until the pH is 4-9, the retention time of the neutralization is 5 s-3 h, the discharging temperature of the neutralized waste acid is 65-95 ℃, and the neutralization reaction pressure is 0-2 MPa;
2) And (2) feeding the neutralized waste acid into a triethylamine dissociation tower from the middle upper part of the tower at a certain flow rate, feeding ammonia gas or liquid ammonia into the triethylamine dissociation tower from the middle lower part of the tower at a certain flow rate, continuously dissociating the waste acid in the tower, and performing n (ammonia): n (triethylamine sulfate) = 2-3, dissociated triethylamine-water is conveyed to a separator, crude triethylamine in the upper layer is separated and then enters a rectification dehydration process, the recovery rate of the triethylamine reaches 95% -98%, the triethylamine content is 99.8-99.9%, lower layer water flows back to a tower, the temperature of a tower kettle is controlled to be 75-110 ℃, the PH of the kettle liquid is more than or equal to 8, the pressure of a dissociation tower system is 0.1-2 MPa, ammonium sulfate solution after dissociation of the triethylamine is pumped out from the dissociation tower kettle at a certain flow rate, the liquid level of the tower kettle is maintained to be balanced, v (neutralization solution) = v (dissociation solution), and the retention time of continuous dissociation is 0.5-8h;
3) The waste acid after triethylamine dissociation is ammonium sulfate-containing solution, the solution is pumped into a continuous ammonia distillation tower at a certain flow, the temperature of a tower kettle is controlled to be 100-110 ℃, the total reflux is carried out on the top of the tower, the evaporated ammonia is absorbed by sulfuric acid, the tower kettle liquid is pumped out at a certain flow, v (dissociation liquid) = v (solution after ammonia distillation) maintains the liquid level balance of the tower kettle, the PH of the tower kettle liquid is controlled to be 4-6, the retention time of continuous ammonia distillation is 0.5-8h, and the system pressure of the ammonia distillation tower is 0.1-2 MPa; the ammonium sulfate solution after ammonia distillation is combined with the sulfuric acid absorption liquid of the ammonia distillation, and then continuous pretreatment and continuous evaporation are carried out, and meanwhile, a qualified ammonium sulfate byproduct is prepared.
The invention relates to a plurality of 'certain flow rates', the following molar ratio or volume ratio determines the flow rate ratio range of two materials, the specific flow rate value is determined according to the residence time of the materials in a reactor and the volume of the reactor, and the volume of the reactor is determined according to the capacity.
The invention has the beneficial technical effects that:
1) The problems in the prior art are solved, the pH of the acesulfame potassium wastewater is neutralized and separated through accurate control, the triethylamine in the waste acid is efficiently recovered, and the recovered triethylamine has high purity and certain economic value;
2) Through the continuous ammonia distillation process, the free ammonia in the wastewater is effectively removed, and the free ammonia can be reduced to be less than 100 ppm. The ammonia nitrogen content of the treated wastewater is greatly reduced, the environmental-friendly discharge standard is reached, and the ecological environment protection is facilitated.
3) The by-product ammonium sulfate prepared by the method has the product quality reaching the high-grade quality, can be used as a nitrogen fertilizer, and promotes ecological development;
4) The invention realizes the continuous integrated treatment of the acesulfame potassium waste acid, greatly improves the waste acid treatment efficiency, improves the treatment capacity, reduces the treatment cost and ensures the safety and stability of the treatment process.
Drawings
FIG. 1 is a process flow diagram of a continuous treatment method of acesulfame potassium waste acid.
Detailed Description
The present invention is further illustrated below with reference to examples, which are understood by those skilled in the art to be illustrative only and not to constitute any limitation to the present invention.
Example 1
1) Firstly, ammonia gas or liquid ammonia with a certain flow rate and waste acid with a certain flow rate are subjected to continuous neutralization reaction, wherein the mass concentration of sulfuric acid in the waste acid is 10%, the mass concentration of triethylamine sulfate is 20%, and n (ammonia): n (sulfuric acid) =2, the feeding temperature of the waste acid is 30 ℃, wherein the continuous reactor is a tubular reactor, the neutralization is carried out until the PH is 4, the retention time of the neutralization is 15min, the discharging temperature of the neutralized waste acid is 70 ℃, and the neutralization reaction pressure is normal pressure;
2) And (2) feeding the neutralized waste acid into a triethylamine dissociation tower from the middle upper part of the tower at a certain flow rate, feeding ammonia gas or liquid ammonia into the triethylamine dissociation tower from the middle lower part of the tower at a certain flow rate, continuously dissociating the waste acid in the tower, and performing n (ammonia): n (triethylamine sulfate) =2, dissociated triethylamine-water is conveyed to a separator, crude triethylamine in the upper layer is separated and then enters a rectification dehydration process, the recovery rate of triethylamine reaches 95%, the triethylamine content is 99.8%, lower layer water flows back to a tower, the temperature of a tower kettle is controlled to be 75 ℃, the pH of a kettle liquid is more than or equal to 8, the pressure of a dissociation tower system is 0.1MPa, an ammonium sulfate solution after dissociation of triethylamine is ejected from the dissociation tower kettle at a certain flow rate, the liquid level of the tower kettle is maintained to be balanced, v (neutralization solution) = v (dissociation solution), and the retention time of continuous dissociation is 2 hours;
3) The waste acid after triethylamine dissociation is ammonium sulfate-containing solution, the solution is injected into a continuous ammonia still at a certain flow rate, the temperature of a tower kettle is controlled to be 100 ℃, the total reflux of the tower top is carried out, the evaporated ammonia is absorbed by sulfuric acid, tower kettle liquid is ejected at a certain flow rate, v (dissociation liquid) = v (solution after ammonia still) maintains the liquid level balance of the tower kettle, the PH of the tower kettle liquid is controlled to be 4, the retention time of continuous ammonia still is 1h, and the system pressure of the ammonia still is 0.1MPa; the ammonium sulfate solution after ammonia distillation is combined with the sulfuric acid absorption liquid after ammonia distillation, and then the mixture is subjected to continuous pretreatment and continuous evaporation, and meanwhile, a qualified ammonium sulfate byproduct is prepared.
Example 2
1) Firstly, ammonia gas or liquid ammonia with a certain flow rate and waste acid with a certain flow rate are subjected to continuous neutralization reaction, wherein the mass concentration of sulfuric acid in the waste acid is 20%, the mass concentration of triethylamine sulfate is 5%, and n (ammonia): n (sulfuric acid) =2.5, the feeding temperature of the waste acid is 45 ℃, wherein the continuous reactor is a kettle-type continuous reactor, the neutralization is carried out until the pH is 7, the retention time of the neutralization is 1h, the discharging temperature of the neutralized waste acid is 75 ℃, and the neutralization reaction pressure is 1MPa;
2) And (2) feeding the neutralized waste acid into a triethylamine dissociation tower from the middle upper part of the tower at a certain flow rate, feeding ammonia gas or liquid ammonia into the triethylamine dissociation tower from the middle lower part of the tower at a certain flow rate, continuously dissociating the waste acid in the tower, and performing n (ammonia): n (triethylamine sulfate) =2.5, dissociated triethylamine-water is conveyed to a separator, crude triethylamine in the upper layer is separated and then enters a rectification dehydration process, the recovery rate of the triethylamine reaches 97%, the triethylamine content is 99.9%, lower layer water flows back to a tower, the temperature of a tower kettle is controlled to be 100 ℃, the pH of a kettle liquid is not less than 8, the pressure of a dissociation tower system is 1MPa, an ammonium sulfate solution obtained after dissociation of the triethylamine is pumped out of the dissociation tower kettle at a certain flow rate, the liquid level of the tower kettle is maintained to be balanced, v (neutralizing liquid) = v (dissociation liquid), and the retention time of continuous dissociation is 4h;
3) The waste acid after triethylamine dissociation is ammonium sulfate-containing solution, the solution is injected into a continuous ammonia still at a certain flow rate, the temperature of a tower kettle is controlled to be 105 ℃, the total reflux of the tower top is carried out, the evaporated ammonia is absorbed by sulfuric acid, tower kettle liquid is ejected at a certain flow rate, v (dissociation liquid) = v (solution after ammonia still) maintains the liquid level balance of the tower kettle, the PH of the tower kettle liquid is controlled to be 5, the retention time of continuous ammonia still is 4 hours, and the system pressure of the ammonia still is 1MPa; the ammonium sulfate solution after ammonia distillation is combined with the sulfuric acid absorption liquid of the ammonia distillation, and then continuous pretreatment and continuous evaporation are carried out, and meanwhile, a qualified ammonium sulfate byproduct is prepared.
Example 3
1) Firstly, ammonia gas or liquid ammonia with a certain flow rate and waste acid with a certain flow rate are subjected to continuous neutralization reaction, wherein the mass concentration of sulfuric acid in the waste acid is 30%, the mass concentration of triethylamine sulfate is 5%, and n (ammonia): n (sulfuric acid) =3, the feeding temperature of the waste acid is 60 ℃, wherein the continuous reactor is a microchannel reactor, the neutralization is carried out until the PH is 9, the retention time of the neutralization is 1.5h, the discharging temperature of the neutralized waste acid is 90 ℃, and the neutralization reaction pressure is 2MPa;
2) And (2) feeding the neutralized waste acid into a triethylamine dissociation tower from the middle upper part of the tower at a certain flow rate, feeding ammonia gas or liquid ammonia into the triethylamine dissociation tower from the middle lower part of the tower at a certain flow rate, continuously dissociating the waste acid in the tower, and performing n (ammonia): n (triethylamine sulfate) =3, dissociated triethylamine-water is conveyed to a separator, crude triethylamine in the upper layer is separated and then enters a rectification dehydration process, the recovery rate of triethylamine reaches 98%, the triethylamine content is 99.9%, water in the lower layer flows back to a tower, the temperature of a tower kettle is controlled to be 110 ℃, the PH of a kettle liquid is more than or equal to 8, the pressure of a dissociation tower system is 2MPa, an ammonium sulfate solution after triethylamine dissociation is discharged from the dissociation tower kettle at a certain flow rate, the liquid level of the tower kettle is maintained to be balanced, v (neutralization solution) = v (dissociation solution), and the retention time of continuous dissociation is 6 hours;
3) The waste acid after triethylamine dissociation is ammonium sulfate-containing solution, the solution is pumped into a continuous ammonia distillation tower at a certain flow, the temperature of a tower kettle is controlled to be 110 ℃, the total reflux is carried out on the top of the tower, the evaporated ammonia is absorbed by sulfuric acid, the tower kettle liquid is pumped out at a certain flow, v (dissociation liquid) = v (solution after ammonia distillation) maintains the liquid level balance of the tower kettle, the PH of the tower kettle liquid is controlled to be 6, the retention time of continuous ammonia distillation is 5h, and the system pressure of the ammonia distillation tower is 2MPa; the ammonium sulfate solution after ammonia distillation is combined with the sulfuric acid absorption liquid of the ammonia distillation, and then continuous pretreatment and continuous evaporation are carried out, and meanwhile, a qualified ammonium sulfate byproduct is prepared.
The present invention has been disclosed in terms of preferred embodiments, but it is not intended to be limited thereto, and all technical solutions obtained by using equivalents or equivalent changes are within the scope of the present invention.
Claims (9)
1. A continuous processing method of acesulfame potassium waste acid is characterized by comprising the following steps:
1) Firstly, ammonia gas or liquid ammonia and waste acid are subjected to continuous neutralization reaction in a continuous reactor, wherein the mass concentration of the sulfuric acid in the waste acid is 10-30%, the mass concentration of triethylamine sulfate is 5-20%, and the molar ratio n (ammonia): n (sulfuric acid) = 2-3, and the neutralization is carried out until the PH is 4-9 and the neutralization reaction pressure is 0-2 MPa;
2) And (2) feeding the neutralized waste acid into a triethylamine dissociation tower from the middle upper part of the tower, feeding ammonia gas or liquid ammonia into the triethylamine dissociation tower from the middle lower part of the tower, and continuously dissociating the waste acid in the tower, wherein the molar ratio of n (ammonia): n (triethylamine sulfate) = 2-3, dissociated triethylamine-water is conveyed to a separator, crude triethylamine in the upper layer is separated and enters a rectification dehydration process, water in the lower layer flows back to a tower, the temperature of a tower kettle is controlled to be 75-110 ℃, the pH value of a kettle liquid is more than or equal to 8, the pressure of a dissociation tower system is 0.1-2 MPa, an ammonium sulfate solution after triethylamine dissociation is pumped out of the dissociation tower kettle, the liquid level of the tower kettle is maintained to be balanced, and v (neutralization solution) = v (dissociation solution);
3) The waste acid after triethylamine dissociation is ammonium sulfate-containing solution, the solution is pumped into a continuous ammonia still, the temperature of a tower kettle is controlled to be 100-110 ℃, the total reflux is carried out on the tower top, the evaporated ammonia is absorbed by sulfuric acid, tower kettle liquid is extracted, v (dissociation liquid) = v (solution after ammonia distillation) maintains the liquid level balance of the tower kettle, the PH of the tower kettle liquid is controlled to be 4-6, and the system pressure of the ammonia still is 0.1-2 MPa; the ammonium sulfate solution after ammonia distillation is combined with the sulfuric acid absorption liquid of ammonia distillation, and then continuous pretreatment and continuous evaporation are carried out, and meanwhile, an ammonium sulfate byproduct is prepared.
2. The continuous processing method of acesulfame potassium waste acid according to claim 1, wherein the feed temperature of the waste acid in step 1) is 10-60 ℃, the retention time of neutralization is 15 min-3 h, and the discharge temperature of the neutralized waste acid is 65-95 ℃.
3. The continuous treatment method of acesulfame potassium waste acid according to claim 1, wherein the continuous reactor is a tank type continuous reactor, a tower type continuous reactor or a microchannel reactor continuous flow reactor.
4. The continuous processing method of acesulfame potassium waste acid according to claim 1, wherein the crude triethylamine at the upper layer in step 2) is separated and then enters a rectification dehydration process, the recovery rate of triethylamine is 95% -98%, and the triethylamine content is 99.8-99.9%.
5. The continuous processing method of acesulfame potassium waste acid according to claim 1, wherein the residence time of the continuous dissociation in step 2) is 0.5-8h.
6. The continuous treatment method of acesulfame potassium waste acid according to claim 1, wherein the residence time of the continuous ammonia distillation in step 3) is 0.5-8h.
7. The continuous treatment method of acesulfame potassium waste acid according to claim 1, wherein the feed temperature of the waste acid in step 1) is 30-60 ℃, the retention time of neutralization is 15 min-1.5 h, and the discharge temperature of the neutralized waste acid is 70-90 ℃.
8. The continuous treatment method of acesulfame potassium waste acid according to claim 1, wherein the residence time of the continuous dissociation in step 2) is 2-6 h.
9. The continuous treatment method of acesulfame potassium waste acid according to claim 1, wherein step 3) is performed with continuous ammonia distillation in the ammonia distillation tower, and the retention time of the continuous ammonia distillation is 1-5 h.
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| CN1883790A (en) * | 2006-06-30 | 2006-12-27 | 张家港浩波化学品有限公司 | Process for reclaiming catalyst for use in synthesis of acesulfame potassium |
| CN101148300A (en) * | 2007-08-30 | 2008-03-26 | 北京维多化工有限责任公司 | Waste acid treatment method and treatment system for acesulfame preparation technique by sulphuric anhydride cyclization method |
| CN101157666A (en) * | 2007-09-12 | 2008-04-09 | 安徽金禾实业股份有限公司 | Triethylamine recovery processing method and device for production of acesulfame potassium |
| CN104193625A (en) * | 2014-09-27 | 2014-12-10 | 安徽金禾实业股份有限公司 | Recovery method of catalyst triethylamine in acesulfame potassium production |
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Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1883790A (en) * | 2006-06-30 | 2006-12-27 | 张家港浩波化学品有限公司 | Process for reclaiming catalyst for use in synthesis of acesulfame potassium |
| CN101148300A (en) * | 2007-08-30 | 2008-03-26 | 北京维多化工有限责任公司 | Waste acid treatment method and treatment system for acesulfame preparation technique by sulphuric anhydride cyclization method |
| CN101157666A (en) * | 2007-09-12 | 2008-04-09 | 安徽金禾实业股份有限公司 | Triethylamine recovery processing method and device for production of acesulfame potassium |
| CN104193625A (en) * | 2014-09-27 | 2014-12-10 | 安徽金禾实业股份有限公司 | Recovery method of catalyst triethylamine in acesulfame potassium production |
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