CN102380226A - Acesulfame sugar water concentration method - Google Patents
Acesulfame sugar water concentration method Download PDFInfo
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- CN102380226A CN102380226A CN2011102638704A CN201110263870A CN102380226A CN 102380226 A CN102380226 A CN 102380226A CN 2011102638704 A CN2011102638704 A CN 2011102638704A CN 201110263870 A CN201110263870 A CN 201110263870A CN 102380226 A CN102380226 A CN 102380226A
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- sugar water
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Abstract
An acesulfame sugar water concentration method comprises following steps: a, a compressor is arranged at the top of a crystallizer, steam in acesulfame sugar water is extracted away, after the steam is compressed, the temperature of the steam is increased to 80 DEG C to 85 DEG C, then the steam enters a tube still heater, and the acesulfame sugar water flowing through a tube nest is heated to 75 DEG C from 60 DEG C or 70 DEG C; and b, a circulation pump is arranged at the bottom of the crystallizer and leads to the tube still heater, so that the acesulfame sugar water is evaporated circularly. The acesulfame sugar water concentration method has the advantages that cost is greatly reduced, in the acesulfame sugar water concentration method, concentration of one ton of sugar water consumes 40 KWh of electricity, steam quantity is low and can be ignored basically, and cost for the acesulfame sugar water concentration method is 20 yuan. In an original concentration method, one ton of sugar water needs one ton of steam, and cost for the original concentration method is 180 yuan. Compared with the original concentration method, the acesulfame sugar water concentration method saves 160 yuan, so that production cost is reduced, and the purpose of energy conservation and environmental protection is also achieved.
Description
Technical field:
The present invention relates in a kind of acesulfame potassium and back syrup condensation crystallization method.
Background technology:
The acesulfame potassium syrup concentrates and to take the single effect evaporation pattern in the prior art, and promptly syrup heats up in tube still heater, the material Natural Circulation, and water evaporates, gas phase is through condenser, the vacuum concentrated a kind of method that reduces pressure, and is as shown in Figure 1.Therefore, existing technology concentrates syrup, and steam consumption is big, and concentrating 1 ton of syrup needs 1 ton steam, about 180 yuan of 1 ton of steam cost, and the recirculated water use amount is big, so cost is higher.
Summary of the invention:
The object of the invention is exactly to solve that the steam consumption that exists in the prior art is big, the recirculated water use amount is big, defect of high cost, the method for concentration of a kind of acesulfame potassium syrup that provides.
Technical scheme of the present invention is following:
A kind of method for concentration of acesulfame potassium syrup is characterized in that may further comprise the steps:
A, the acesulfame potassium syrup is squeezed in the tube still heater with circulating pump, the acesulfame potassium syrup after heating gets into crystallizer;
B, be provided with compressor at the crystallizer top; Steam in the acesulfame potassium syrup in the crystallizer is taken away; Bring up to 80 ℃-85 ℃ through vapor (steam) temperature after the compressor compresses; This steam gets into tube still heater, will be heated to 75 ℃, formation condensate liquid entering condensate receiver behind the steam process tube still heater from 60-70 ℃ through the acesulfame potassium syrup of tubulation;
C, crystallizer bottom are provided with circulating pump and lead to tube still heater, make acesulfame potassium syrup circulating and evaporating.
Acesulfame potassium syrup method for concentration of the present invention comes down to utilize Lodz machine compression acesulfame potassium syrup indirect steam; Make full use of indirect steam latent heat; Through the indirect steam of overcompression, pressure increases, and temperature raises; Do the thermal source that concentrates syrup with this, facilitate with forced circulation pump that syrup circulates, heat exchange in heater.Only need syrup is heated to about 75 ℃ thereby reach, when concentrating, need not new steam and get involved the purpose that can concentrate.
The invention has the advantages that: the present invention's technology as compared with the past, cost significantly reduces, through adding up: method for concentration of the present invention, 1 ton of syrup concentrates consumes electric power 40 degree, and quantity of steam is low, ignores basically, counts 20 yuan.1 ton of syrup of former method for concentration needs 1 ton of steam, counts 180 yuan.Practice thrift 160 yuan relatively.Thereby reduce production costs, also reach the purpose of energy-conserving and environment-protective.
Description of drawings:
Fig. 1 is existing acesulfame potassium syrup concentration technology flow chart;
Fig. 2 is an acesulfame potassium syrup concentration technology flow chart of the present invention.
The specific embodiment:
As shown in Figure 2; The employed device of the method for concentration of a kind of acesulfame potassium syrup provided by the invention; Comprise tube still heater and crystallizer; The crystallizer bottom connects circulating pump through pipeline, and circulating-pump outlet connects the tubulation import in the tube still heater, and the tubulation outlet is connected in the crystallizer through pipeline.The crystallizer top connects compressor (Roots's machine) through pipeline, and compressor outlet connects the import of tube still heater housing heating chamber, and the outlet of tube still heater housing heating chamber connects condensate receiver.The crystallizer bottom also connects freezing kettle through pipeline.
The method for concentration of a kind of acesulfame potassium syrup provided by the invention is with T
170 ℃ acesulfame potassium syrup is squeezed into the tubulation import in the tube still heater, and the acesulfame potassium syrup that after heating, flows out from the tubulation outlet reaches T
275 ℃, behind the entering crystallizer, under compressor (Roots's machine) action of negative pressure, with the T in the acesulfame potassium syrup in the crystallizer
370-75 ℃ steam is taken away, and through after the compressor compresses, vapor (steam) temperature is brought up to T
480 ℃-85 ℃, this steam is through behind tube still heater, and acesulfame potassium syrup that will be through tubulation is from T
170 ℃ are heated to T
275 ℃, steam gets into condensate receiver through forming condensate liquid behind the tube still heater.Said process repeats, and is concentrated to until the acesulfame potassium syrup to meet the requirements.
Through adding up: method for concentration of the present invention, 1 ton of syrup concentrates consumes electric power 40 degree, and quantity of steam is low, ignores basically, counts 20 yuan.1 ton of syrup of former method for concentration needs 1 ton of steam, counts 180 yuan, practices thrift 160 yuan relatively.Thereby reduce production costs, also reach the purpose of energy-conserving and environment-protective.
Claims (1)
1. the method for concentration of an acesulfame potassium syrup is characterized in that may further comprise the steps:
A, the acesulfame potassium syrup is squeezed in the tube still heater with circulating pump, the acesulfame potassium syrup after heating gets into crystallizer;
B, be connected with compressor at the crystallizer top; Steam in the acesulfame potassium syrup in the crystallizer is taken away; Bring up to 80 ℃-85 ℃ through vapor (steam) temperature after the compressor compresses; This steam gets into tube still heater, will be heated to 75 ℃, formation condensate liquid entering condensate receiver behind the steam process tube still heater from 60-70 ℃ through the acesulfame potassium syrup of tubulation;
C, crystallizer bottom are provided with circulating pump and lead to tube still heater, make acesulfame potassium syrup circulating and evaporating.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2011102638704A CN102380226A (en) | 2011-09-07 | 2011-09-07 | Acesulfame sugar water concentration method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2011102638704A CN102380226A (en) | 2011-09-07 | 2011-09-07 | Acesulfame sugar water concentration method |
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| CN102380226A true CN102380226A (en) | 2012-03-21 |
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| CN2011102638704A Pending CN102380226A (en) | 2011-09-07 | 2011-09-07 | Acesulfame sugar water concentration method |
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Cited By (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103588728A (en) * | 2013-11-01 | 2014-02-19 | 安徽金禾实业股份有限公司 | Neutralization direct crystallization production technology of acesulfame potassium |
| CN104292181A (en) * | 2014-09-27 | 2015-01-21 | 安徽金禾实业股份有限公司 | Method for concentrating acesulfame potassium mother liquor by adopting MVR system |
| CN106262665A (en) * | 2016-08-12 | 2017-01-04 | 安徽维多食品配料有限公司 | A kind of direct employing film processes the method for equivalent dialysis |
| CN106496159A (en) * | 2016-09-20 | 2017-03-15 | 苏州浩波科技股份有限公司 | A kind of production technology of the big granularity crystal of acesulfame potassium |
| US10023546B2 (en) | 2016-09-21 | 2018-07-17 | Celanese International Corporation | Acesulfame potassium compositions and processes for producing same |
| US10030000B2 (en) | 2016-09-21 | 2018-07-24 | Celanese International Corporation | Acesulfame potassium compositions and processes for producing same |
| US10029998B2 (en) | 2016-09-21 | 2018-07-24 | Celanese International Corporation | Acesulfame potassium compositions and processes for producing same |
| US10029999B2 (en) | 2016-09-21 | 2018-07-24 | Celanese International Corporation | Acesulfame potassium compositions and processes for producing same |
| CN109045744A (en) * | 2018-08-30 | 2018-12-21 | 山东亚邦化工科技有限公司 | The method and apparatus for preparing acesulfame potassium crystallization of continuous-stable |
| CN109078359A (en) * | 2018-08-30 | 2018-12-25 | 山东亚邦化工科技有限公司 | A kind of technique and device for acesulfame potassium sulfonation hydrolysis liquid continuous extration |
| USRE48464E1 (en) | 2012-06-08 | 2021-03-16 | Celanese Sales Germany Gmbh | Process for producing acesulfame potassium |
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| CN85109641A (en) * | 1984-10-19 | 1986-06-10 | 武田药品工业株式会社 | Carry out the method and the device thereof of chemical dehydration reaction |
| CN101124981A (en) * | 2007-09-12 | 2008-02-20 | 安徽金禾实业股份有限公司 | Concentrating method and device in acesulfame potassium production |
| CN101392757A (en) * | 2008-10-31 | 2009-03-25 | 溧阳德维透平机械有限公司 | Centrifugal compressor and vapour recompression method utilizing the compressor |
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| CN85109641A (en) * | 1984-10-19 | 1986-06-10 | 武田药品工业株式会社 | Carry out the method and the device thereof of chemical dehydration reaction |
| CN101124981A (en) * | 2007-09-12 | 2008-02-20 | 安徽金禾实业股份有限公司 | Concentrating method and device in acesulfame potassium production |
| CN101392757A (en) * | 2008-10-31 | 2009-03-25 | 溧阳德维透平机械有限公司 | Centrifugal compressor and vapour recompression method utilizing the compressor |
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Cited By (36)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| USRE48464E1 (en) | 2012-06-08 | 2021-03-16 | Celanese Sales Germany Gmbh | Process for producing acesulfame potassium |
| CN103588728B (en) * | 2013-11-01 | 2016-06-22 | 安徽金禾实业股份有限公司 | With direct crystallization production technology in acesulfame potassium |
| CN103588728A (en) * | 2013-11-01 | 2014-02-19 | 安徽金禾实业股份有限公司 | Neutralization direct crystallization production technology of acesulfame potassium |
| CN104292181A (en) * | 2014-09-27 | 2015-01-21 | 安徽金禾实业股份有限公司 | Method for concentrating acesulfame potassium mother liquor by adopting MVR system |
| CN104292181B (en) * | 2014-09-27 | 2016-10-26 | 安徽金禾实业股份有限公司 | A kind of MVR system concentrates the method for acesulfame potassium mother solution |
| CN106262665A (en) * | 2016-08-12 | 2017-01-04 | 安徽维多食品配料有限公司 | A kind of direct employing film processes the method for equivalent dialysis |
| CN106496159B (en) * | 2016-09-20 | 2018-09-21 | 苏州浩波科技股份有限公司 | A kind of production technology of the big granularity crystal of acesulfame potassium |
| CN106496159A (en) * | 2016-09-20 | 2017-03-15 | 苏州浩波科技股份有限公司 | A kind of production technology of the big granularity crystal of acesulfame potassium |
| US10590098B2 (en) | 2016-09-21 | 2020-03-17 | Celanese International Corporation | Acesulfame potassium compositions and processes for producing same |
| US10759771B2 (en) | 2016-09-21 | 2020-09-01 | Celanese International Corporation | Acesulfame potassium compositions and processes for producing same |
| US10029998B2 (en) | 2016-09-21 | 2018-07-24 | Celanese International Corporation | Acesulfame potassium compositions and processes for producing same |
| US11731948B2 (en) | 2016-09-21 | 2023-08-22 | Celanese International Corporation | Acesulfame potassium compositions and processes for producing same |
| US11724994B2 (en) | 2016-09-21 | 2023-08-15 | Celanese International Corporation | Acesulfame potassium compositions and processes for producing same |
| US10208004B2 (en) | 2016-09-21 | 2019-02-19 | Celanese International Corporation | Acesulfame potassium compositions and processes for producing same |
| US10227316B2 (en) | 2016-09-21 | 2019-03-12 | Celanese International Corporation | Acesulfame potassium compositions and processes for producing same |
| US10233164B2 (en) | 2016-09-21 | 2019-03-19 | Celanese International Corporation | Acesulfame potassium compositions and processes for producing same |
| US10233163B2 (en) | 2016-09-21 | 2019-03-19 | Celanese International Corporation | Acesulfame potassium compositions and processes for producing same |
| US10590097B2 (en) | 2016-09-21 | 2020-03-17 | Celanese International Corporation | Acesulfame potassium compositions and processes for producing same |
| US10030000B2 (en) | 2016-09-21 | 2018-07-24 | Celanese International Corporation | Acesulfame potassium compositions and processes for producing same |
| US10590095B2 (en) | 2016-09-21 | 2020-03-17 | Celanese International Corporation | Acesulfame potassium compositions and processes for producing same |
| US10590096B2 (en) | 2016-09-21 | 2020-03-17 | Celenese International Corporation | Acesulfame potassium compositions and processes for producing same |
| US10029999B2 (en) | 2016-09-21 | 2018-07-24 | Celanese International Corporation | Acesulfame potassium compositions and processes for producing same |
| US10759770B2 (en) | 2016-09-21 | 2020-09-01 | Celanese International Corporation | Acesulfame potassium compositions and processes for producing same |
| US10781190B2 (en) | 2016-09-21 | 2020-09-22 | Celanese International Corporation | Acesulfame potassium compositions and processes for producing same |
| US10781191B2 (en) | 2016-09-21 | 2020-09-22 | Celanese International Corporation | Acesulfame potassium compositions and processes for producing same |
| US11724993B2 (en) | 2016-09-21 | 2023-08-15 | Celanese International Corporation | Acesulfame potassium compositions and processes for producing same |
| US10023546B2 (en) | 2016-09-21 | 2018-07-17 | Celanese International Corporation | Acesulfame potassium compositions and processes for producing same |
| US10954204B2 (en) | 2016-09-21 | 2021-03-23 | Celanese International Corporation | Acesulfame potassium compositions and processes for producing same |
| US10954203B2 (en) | 2016-09-21 | 2021-03-23 | Celanese International Corporation | Acesulfame potassium compositions and processes for producing same |
| US10961207B2 (en) | 2016-09-21 | 2021-03-30 | Celanese International Corporation | Acesulfame potassium compositions and processes for producing same |
| US10975047B2 (en) | 2016-09-21 | 2021-04-13 | Celanese International Corporation | Acesulfame potassium compositions and processes for producing same |
| US11718594B2 (en) | 2016-09-21 | 2023-08-08 | Celanese International Corporation | Acesulfame potassium compositions and processes for producing same |
| CN109045744B (en) * | 2018-08-30 | 2021-04-27 | 山东亚邦化工科技有限公司 | Method and device for continuously and stably preparing acesulfame potassium crystals |
| CN109078359B (en) * | 2018-08-30 | 2020-11-06 | 山东亚邦化工科技有限公司 | Process and device for continuous extraction of acesulfame potassium sulfonated hydrolysate |
| CN109078359A (en) * | 2018-08-30 | 2018-12-25 | 山东亚邦化工科技有限公司 | A kind of technique and device for acesulfame potassium sulfonation hydrolysis liquid continuous extration |
| CN109045744A (en) * | 2018-08-30 | 2018-12-21 | 山东亚邦化工科技有限公司 | The method and apparatus for preparing acesulfame potassium crystallization of continuous-stable |
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Application publication date: 20120321 |