CN101745241A - Method and device for producing calcium chloride solution through concentration - Google Patents
Method and device for producing calcium chloride solution through concentration Download PDFInfo
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- CN101745241A CN101745241A CN200910264164A CN200910264164A CN101745241A CN 101745241 A CN101745241 A CN 101745241A CN 200910264164 A CN200910264164 A CN 200910264164A CN 200910264164 A CN200910264164 A CN 200910264164A CN 101745241 A CN101745241 A CN 101745241A
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Abstract
The invention relates to a method and a device for producing calcium chloride solution through concentration, which belongs to the technical field of calcium chloride solution concentration. The method comprises the following steps: firstly, two sections of coordination methods that a mechanical steam recompression evaporator and a triple effect evaporator with a steam jet pump are combined are adopted for concentrating the calcium chloride solution; secondly, the method for the mechanical vapor recompression evaporator adopted at the first section comprises the following steps: the raw materials enter into the first section of the evaporator (3) to be heated and vaporized, the generated secondary steam carried with a small part of calcium chloride solution enters into a separator (4) for separation, then the separated secondary steam enters into a compressor (5) for compression, the compressed secondary steam is introduced into a shell side of the first section of the evaporator (3) after temperature rise and pressure increase, then the calcium chloride solution in the tube side is heated, and after the separated calcium chloride solution is mixed with unevaporated calcium chloride solution, the mixed solution is delivered to a second section of process pump from a first section of process pump (6). By adopting the method and the device, both the energy resources and the investment are saved, and the running cost is reduced.
Description
Technical field
The present invention is that a kind of calcium chloride solution concentrates production production method and production equipment, is applied to concentrate calcium chloride solution, can reduce the energy consumption in the industrial production, belongs to energy-saving field.
Background technology
At present, concentrated multiple-effect evaporation methods that adopt of known calcium chloride solution more.As shown in Figure 1, be a triple effect evaporation flow chart commonly used.In this mode, living steam enters first single-effect evaporator and adds thermal material, the indirect steam that the material explosive evaporation goes out enters the material in second single-effect evaporator heating, two effects, second indirect steam of imitating the material generation enters third effect evaporator again and adds thermal material, and the indirect steam that is produced enters condenser condenses and discharges.This shows that this mode need constantly provide a large amount of living steam, has increased running cost, has increased energy consumption; In addition, this mode will reach the required evaporimeter effect number of end of a period concentration requirement and increase, and investment increases, and equipment is huge, complicated operation.Now, along with day being becoming tight of energy situation, energy-conservationly more and more paid close attention to by society, government, enterprise, some energy policies are put into effect in succession.In order better to adapt to energy policy, to develop and promote, power-saving technology or technology have been imperative.
Summary of the invention
The purpose of this invention is to provide the calcium chloride solution that a kind of steam consumption is few, easy to operate, energy-efficient, operating cost is low and concentrate production method and production equipment.
A kind of calcium chloride solution concentrates production method, it is characterized in that may further comprise the steps:
Two sections coordination approach that the triple effect evaporation of adopting steam machinery to recompress evaporation and carrying vapour jet pump combines concentrate calcium chloride solution;
The method detailed process of the steam machinery recompression of above-mentioned first section employing is: raw material enters first section evaporimeter and is subjected to thermal evaporation, the indirect steam that produces is carried the small part calcium chloride solution secretly and is entered the separator separation, isolated indirect steam advances compressor and contracts and import calcium chloride solution in first section evaporimeter shell side heating tube journey after the increasing temperature and pressure, and isolated calcium chloride solution mixes with the calcium chloride solution that not have to evaporate and then is pumped into second section by first section process.
A kind of calcium chloride solution concentrates production equipment, it is characterized in that:
Head tank links to each other with first section evaporimeter upper cover through feed pump, and the low head of first section evaporimeter is divided into two branch roads, and a branch road links to each other with first section evaporimeter shell through first section separator and vapour compression machine; Another branch road with link to each other with the upper cover of 1st effective evaporator through first section process pump after the bottom of first section separator is converged;
Above-mentioned 1st effective evaporator is divided into two branch roads, and a branch road links to each other with the 1st effective evaporator shell through an effect separator and steam jet pump; Imitating the process pump through one after the bottom that another branch road and is imitated separator is converged links to each other with the upper cover of 2nd effect evaporator;
Above-mentioned 2nd effect evaporator is divided into two branch roads, and a branch road is imitated separator through two and linked to each other with the triple effect evaporator shell; Imitating the process pumps through two after the bottoms that another branch road and two is imitated separators are converged links to each other with the upper cover of triple effect evaporator;
Above-mentioned triple effect evaporator is divided into two branch roads, and a branch road links to each other with the condenser shell through the triple effect separator; After converging, the bottom of another branch road and triple effect separator gets through discharging pump; Condenser links to each other with vavuum pump.
Above-mentioned first section separator shell condensate outlet, 1st effective evaporator shell condensate outlet, 2nd effect evaporator shell condensate outlet, triple effect evaporator shell condensate outlet, condenser shell condensate outlet all link to each other with drainer;
Two sections coordination approach that the present invention adopts the triple effect evaporation of recompression evaporation of steam machinery and carrying vapour jet pump to combine concentrate calcium chloride solution, first section is adopted steam machinery recompression method, indirect steam after compression also will be compressed by the isolated indirect steam of separator uses as giving birth to steam, and such first section just need not extra heating steam.Adopt the triple effect evaporation method of carrying vapour jet pump in second section, only need a spot of heating steam.Whole like this technology only needs a spot of electric energy and heating steam just can reach good evaporation effect, has saved the energy, has reduced operating cost.Reached the purpose that steam consumption is few, easy to operate, energy-efficient, operating cost is low.
Description of drawings
Fig. 1 is a process chart of the present invention.
Fig. 2 is existing triple effect evaporation flow chart.
Fig. 3 is the relation of system's total operation expense with first section discharging change in concentration.
Fig. 1, comprise in 2 that label name is called: 1, head tank 2, feed pump 3, first section evaporimeter 4, first section separator 5, vapour compression machine 6, first section process pump 7, steam jet pump machine 8,1st effective evaporator 9, one imitates separator 10, one imitates process pump 11,2nd effect evaporator 12, two imitate separator 13, two imitate process pump 14, triple effect evaporator 15, triple effect separator 16, discharging pump 17, condenser 18, vavuum pump 19, condensation water pot 20, vapour coagulates jar 21, head tank 22, feed pump 23,1st effective evaporator 24, one imitates separator 25, one imitates process pump 26,2nd effect evaporator 27, two imitate separator 28, two imitate process pump 29, triple effect evaporator 30, three school separators 31, discharging pump 32, condenser 33, coagulate water pot 34, condensate pump 35, vavuum pump.Triple effect evaporation D, the water for industrial use E of A, raw material B, first section steam machinery recompression evaporation C, second section carrying vapour jet pump, finish liquid F, condensed water
The specific embodiment
Process of the present invention is:
As shown in Figure 1, the raw material in the head tank 1 pumps into evaporimeter 3 through feed pump 2, heat absorption boiling, and the part that contains indirect steam enters mixes with the feed liquid that does not contain gas after separator 4 is isolated indirect steam, in second section of MVR process pump 6 pump people; Isolated indirect steam after vapour compression machine 5 compressions, imports the evaporimeter heating and concentrates raw material, and the heat release condensation enters chilled water tank 19 after coagulate water pipe;
In second section, enter the tube side of 1st effective evaporator 8 by first section pump people's feed liquid, the explosive evaporation of heat absorption falling liquid film, low head at evaporimeter, the part that contains indirect steam enters mixes with the feed liquid that does not contain gas that flows out straight after an effect separator 9 is isolated indirect steam, imitate process pump 10 pump people second single-effect evaporator 11 tube sides through one, the explosive evaporation of heat absorption falling liquid film, the part that contains indirect steam enters two and imitates separator 12, mix with the feed liquid that does not contain gas that flows out straight after isolating indirect steam, imitate process pump 13 pump people third effect evaporators 14 tube sides through two, the explosive evaporation of heat absorption falling liquid film, the part that contains indirect steam enters triple effect separator 15, isolates behind the indirect steam and mixes with the feed liquid that does not contain gas that flows out straight, pumps through discharging pump 16.One imitates isolated indirect steam, and a part is introduced into steam jet pump 7 and combines with giving birth to steam, and the shell side heating that the back of boosting imports first section evaporimeter concentrates raw material, and the heat release condensation enters chilled water tank after coagulate water pipe; The shell side heating that another part imports second single-effect evaporator 11 concentrates raw material.Second imitates the shell side heating that produces indirect steam importing third effect evaporator 14 concentrates raw material, and the heat release condensation enters chilled water tank after coagulate water pipe, and the shell side of the indirect steam importing condenser 17 that triple effect produces enters water pot with fixed attention after the condensation.
First section concentrated discharge concentration is one of key factor that influences system power dissipation.If the concentration of first section discharging is low, second section evaporation treatment capacity increases, and the total operation expense of system increases; Otherwise first section concentrate excessive concentration, first section compressor power consumption that needs are bigger then, the operating cost of system also can increase.Therefore, when system moves, an optimum value is arranged.
The calculating formula of the total operation expense of system is: C=C
1+ C
2+ C
3
C in the formula
1---the electric energy expense (ten thousand yuan/year) of compressor consumption
C
2--the living steam expense (ten thousand yuan/year) of heat spray pump consumption
C
3--cooling water expense (ten thousand yuan/year)
A--working time wherein, hour
b
1, b
2, b
3--electricity price, unit; Give birth to the steam price, unit; The cooling water price, unit.
The power consumption of E--compressor, kwh.
The F--inlet amount, kg/h.
X
1, X
2, X
3--material concentration, %; Discharge concentration, % for first section; End of a period concentration, %.
The latent heat of the indirect steam that triple effect produces among second section of the r--, kJ/kg.
C
p--cooling water specific heat capacity, kJ/kgK.
Δ T--cooling range, ℃.
Work as X
2When getting different value respectively, the total cost situation of change of the system that is obtained by following formula as shown in Figure 3.Wherein, the input concentration of rare calcium chloride solution is 7%, and end of a period concentration is 43%; A=7200 hour, b
1=0.6 yuan, b
2=180 yuan, b
3=0.4 yuan, Δ T=6 ℃.Therefrom we when first section discharge concentration was 23%-25%, the total operation expense of system had minimum of a value as can be seen.In addition, we also are not difficult to find out from figure, and when also the whole operation process had only second section to finish when first section discharge concentration is 0, needed total cost was a lot of in the time of will exceeding two-section joint; In like manner, to discharge concentration be 43% also to be whole process when having only first section to finish when first section, the total cost when needed total cost is greater than two-section joint, but be less than total cost when having only second section work.Therefore, energy-saving effect of the present invention is remarkable, for reduce cost in the calcium chloride concentration process, energy savings opened up a new way.
The present invention specifically is embodiment: temperature is 80 ℃, and concentration is that rare calcium chloride solution of 7% enters first section evaporimeter, and the evaporation and concentration of being heated to concentration is 24% to enter in second section; The temperature that the solution evaporation is produced is to enter compressor after 73.9 ℃ indirect steam separates through first section separator, and compressed being warming up to enters first section evaporimeter heating calcium chloride solution wherein after 87 ℃.Concentration be 24% calcium chloride solution successively through second section one imitate, two imitate, the triple effect evaporator heating concentrates, be concentrated into 43% after discharging pump discharge; The indirect steam that 1st effective evaporator produces in second section is imitated separator through one, and to separate that a back part extracted through pressure by heat spray pump be that the livings steam of 6MPa promotes the back and heats calcium chloride solution in the 1st effective evaporator, and another part enters two effects and evaporates and wherein heat calcium chloride solution; The indirect steam that 2nd effect evaporator produces is imitated through two and is entered triple effect evaporator heating calcium chloride solution after separator separates, and the indirect steam that produces in the triple effect evaporator enters in the condenser, enters water pot with fixed attention after the condensation.In first section evaporimeter and second section one imitate, two imitate, the triple effect evaporation water that coagulates wherein also enters water pot with fixed attention through coagulating water pipe.
Claims (3)
1. a calcium chloride solution concentrates production method, it is characterized in that may further comprise the steps:
(1), two sections coordination approach that adopt the mechanical triple effect evaporation that recompresses evaporation and carrying vapour jet pump of steam to combine concentrate calcium chloride solution;
(2), the method detailed process of the steam of above-mentioned first section employing machinery recompression is: raw material enters first section evaporimeter
(3) be subjected to thermal evaporation, the indirect steam that produces is carried the small part calcium chloride solution secretly and is entered separator (4) separation, isolated indirect steam advances compressor (5) and contracts and import calcium chloride solution in first section evaporimeter (3) shell side heating tube side after the increasing temperature and pressure, isolated calcium chloride solution with send into second section by first section process pump (6) after the calcium chloride solution that not have to evaporate mixes.
2. concentrate production method according to the described calcium chloride solution of claim 1, it is characterized in that may further comprise the steps: first section evaporimeter (3) outlet calcium chloride solution concentration is controlled in the 23%-25% scope in the method for the steam machinery recompression of first section employing.
3. a calcium chloride solution concentrates production equipment, it is characterized in that:
Head tank (1) links to each other with first section evaporimeter (3) upper cover through feed pump (2), the low head of first section evaporimeter (3) is divided into two branch roads, and a branch road links to each other with first section evaporimeter (3) shell through first section separator (4) and vapour compression machine (5); Another branch road with link to each other through the upper cover of first section process pump (6) after the bottom of first section separator (4) is converged with 1st effective evaporator (8);
Above-mentioned 1st effective evaporator (8) is divided into two branch roads, and a branch road links to each other with 1st effective evaporator (8) shell through an effect separator (9) and steam jet pump (7); Imitating process pump (10) through one after the bottom that another branch road and is imitated separator (9) is converged links to each other with the upper cover of 2nd effect evaporator (11);
Above-mentioned 2nd effect evaporator (11) is divided into two branch roads, and a branch road is imitated separator (12) through two and linked to each other with triple effect evaporator (14) shell; Imitating process pumps (13) through two after the bottoms that another branch road and two is imitated separators (12) are converged links to each other with the upper cover of triple effect evaporator (14);
Above-mentioned triple effect evaporator (14) is divided into two branch roads, and a branch road links to each other with condenser (17) shell through triple effect separator (15); After converging, the bottom of another branch road and triple effect separator (15) gets through discharging pump (16); Condenser (17) links to each other with vavuum pump (18);
Above-mentioned first section separator (4) shell condensate outlet, 1st effective evaporator (8) shell condensate outlet, 2nd effect evaporator (11) shell condensate outlet, triple effect evaporator (14) shell condensate outlet, condenser (17) shell condensate outlet all link to each other with drainer (20).
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Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102641603A (en) * | 2012-03-11 | 2012-08-22 | 甘肃蓝科石化高新装备股份有限公司 | Plate-type evaporator device with mechanical vapor compressor |
| CN103833092A (en) * | 2014-03-19 | 2014-06-04 | 江苏星瑞化工工程科技有限公司 | Method for concentrating salt-containing wastewater |
| CN105999750A (en) * | 2016-06-23 | 2016-10-12 | 广州中科鑫洲科技有限公司 | Evaporating system capable of conducting online descaling and working continuously and evaporating process |
| CN108176066A (en) * | 2017-12-11 | 2018-06-19 | 山东省科学院能源研究所 | Alcohol method prepares the device and technique of syrup evaporation recycling ethyl alcohol during protein concentrate |
| CN108245912A (en) * | 2018-01-04 | 2018-07-06 | 中石化上海工程有限公司 | The process that multiple-effect evaporation and MVR systems mutually switch |
| CN110183017A (en) * | 2019-05-10 | 2019-08-30 | 江苏华晖环保科技有限公司 | A kind of multiple-effect evaporation technique of strong brine zero-emission |
| CN111544909A (en) * | 2020-04-27 | 2020-08-18 | 广东中科光年数智科技有限公司 | Evaporation concentration system |
-
2009
- 2009-12-31 CN CN2009102641644A patent/CN101745241B/en active Active
Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102641603A (en) * | 2012-03-11 | 2012-08-22 | 甘肃蓝科石化高新装备股份有限公司 | Plate-type evaporator device with mechanical vapor compressor |
| CN103833092A (en) * | 2014-03-19 | 2014-06-04 | 江苏星瑞化工工程科技有限公司 | Method for concentrating salt-containing wastewater |
| CN103833092B (en) * | 2014-03-19 | 2016-01-20 | 江苏星瑞化工工程科技有限公司 | A kind of concentration method of brine waste |
| CN105999750A (en) * | 2016-06-23 | 2016-10-12 | 广州中科鑫洲科技有限公司 | Evaporating system capable of conducting online descaling and working continuously and evaporating process |
| CN108176066A (en) * | 2017-12-11 | 2018-06-19 | 山东省科学院能源研究所 | Alcohol method prepares the device and technique of syrup evaporation recycling ethyl alcohol during protein concentrate |
| CN108176066B (en) * | 2017-12-11 | 2024-03-08 | 山东省科学院能源研究所 | Device and process for recovering ethanol by evaporating syrup in process of preparing concentrated protein by alcohol method |
| CN108245912A (en) * | 2018-01-04 | 2018-07-06 | 中石化上海工程有限公司 | The process that multiple-effect evaporation and MVR systems mutually switch |
| CN110183017A (en) * | 2019-05-10 | 2019-08-30 | 江苏华晖环保科技有限公司 | A kind of multiple-effect evaporation technique of strong brine zero-emission |
| CN111544909A (en) * | 2020-04-27 | 2020-08-18 | 广东中科光年数智科技有限公司 | Evaporation concentration system |
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| CN101745241B (en) | 2011-08-24 |
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Owner name: JIANGSU LEKE THERMAL TECHNOLOGY CO., LTD. Free format text: FORMER OWNER: NANJING UNIVERSITY OF AERONAUTICS AND ASTRONAUTICS Effective date: 20131031 Free format text: FORMER OWNER: HOT ENGINEERING EQUIPMENT CO., LTD. OF THE YUE S OF JIANGSU Effective date: 20131031 |
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Inventor after: Han Dong Inventor after: Ye Li Inventor after: Gu Ang Inventor after: Yao Junlei Inventor after: Peng Tao Inventor after: Xia Junjun Inventor after: Liang Lin Inventor after: Xia Jun Inventor after: Zhou Wensheng Inventor after: Bai Zhongkai Inventor after: Mao Jing Inventor after: Dan Huawei Inventor before: Han Dong Inventor before: Gu Ang Inventor before: Yao Junlei Inventor before: Liang Lin Inventor before: Peng Tao Inventor before: Xia Jun Inventor before: Zhou Wensheng Inventor before: Bai Zhongkai Inventor before: Mao Jing Inventor before: Dan Huawei Inventor before: Ye Li |
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Free format text: CORRECT: ADDRESS; FROM: 210016 NANJING, JIANGSU PROVINCE TO: 214500 TAIZHOU, JIANGSU PROVINCE Free format text: CORRECT: INVENTOR; FROM: HAN DONG LIANG LIN PENG TAO XIA JUN ZHOU WENSHENG BAI ZHONGKAI MAO JING DAN HUAWEI YE LI GU ANG YAO JUNLEI TO: HAN DONG PENG TAO XIA JUNJUN LIANG LIN XIA JUN ZHOU WENSHENG BAI ZHONGKAI MAO JING DAN HUAWEI YE LI GU ANG YAO JUNLEI |
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Effective date of registration: 20131031 Address after: 214500 Jingjiang City, Jiangsu province Huaxiang Road Development Zone No. 18 Building 2 Patentee after: Jiangsu Leke Thermal Technology Co., Ltd. Address before: Yudaojie Baixia District of Nanjing City, Jiangsu Province, No. 29 210016 Patentee before: Nanjing University of Aeronautics and Astronautics Patentee before: Hot engineering equipment Co., Ltd. of the Yue 's of Jiangsu |