CN101224879A - Energy-saving method for chlorination reaction process - Google Patents
Energy-saving method for chlorination reaction process Download PDFInfo
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- CN101224879A CN101224879A CNA2008100522097A CN200810052209A CN101224879A CN 101224879 A CN101224879 A CN 101224879A CN A2008100522097 A CNA2008100522097 A CN A2008100522097A CN 200810052209 A CN200810052209 A CN 200810052209A CN 101224879 A CN101224879 A CN 101224879A
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
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Abstract
The invention discloses an energy-saving method during a chlorination reaction, which belongs to the energy-saving technology during the chlorination reaction. The process of the method includes: low temperature salt water from a refrigerating machine is transferred to a cryogenic heat exchanger to carry out heat exchange with the low boiling point material, and then the brine is transferred to a liquefied chlorine carburetor after being heated as the medium for the vaporization of the liquefied chlorine, which provides the heat needed by the vaporization of the liquefied chlorine and is cooled, then the cooled brine is transferred to the refrigerating machine. In this way, a recycle process of brine is formed from the refrigerating machine to the cryogenic heat, then to the liquefied chlorine carburetor exchanger for heat exchange and finally to the refrigerating machine. The invention has the advantages that the evaporation process and refrigeration system of the liquefied chlorine is linked, which saves the heating steam and reduces the energy consumption of the refrigerating machine; the process is simple and is easy to be realized.
Description
Technical field
The present invention relates to the power-economizing method in a kind of chlorination reaction process, belong to the power-saving technology of chlorination reaction process.
Background technology
Existing is in the direct chlorination reaction process of raw material with the liquid chlorine, comprises the vaporization of liquid chlorine substantially, the processes such as capture of chlorination reaction and lower boiling vaporized product.Wherein the liquid chlorine vaporescence is meant that liquid chlorine carries out heat exchange by vapourizing unit and thermal medium, obtains the process of chlorine steam, and the heating medium that is adopted on the engineering is generally water vapor at present, and minority adopts hot water or electrically heated.Chlorine after the vaporization enters use equipment after the surge tank voltage stabilizing.Thermal medium is lowered the temperature after heat exchange, but is not repeated to utilize, and consumed energy is higher.
A kind of efficient chlorine liquid carburetor is disclosed in patent CN125137A, having proposed use occurring in nature river, river, lake water, seawater replaces above-mentioned water vapour or hot water or electric energy equal energy source as heating medium, be a kind of method that reduces liquid chlorine vaporescence energy consumption preferably, realized the energy-conservation the first step.Yet after this patent did not relate to the liquid chlorine vaporization yet, the cold that heating medium absorbed used (being the energy utilization) problem.
Meanwhile, for low-boiling-point substance and the material of avoiding reacting generation leaves reactor with the steam state form, need capture as cold medium in the chlorination reaction process with hypothermic saline.Industrial general using refrigerator (being refrigeration system) obtains the suitable chilled brine of temperature as heat-eliminating medium.At present, the salt solution after heat exchange heats up returns the cooled or cooling of refrigerator and is hypothermic saline.Salt solution is only done circulation between refrigerator → interchanger → refrigerator, the process of intensification of just experience cooling → intensifications of salt solution → lower the temperature again → again, and the energy that intensification salt solution is had is not fully used.
Therefore, comprise in the whole chlorination reaction process need with the chlorination vaporizer of thermal medium heat exchange and need with the cryogenic heat exchanger of cold medium heat exchange, the two each Xingqi thing, the energy consumption height has been wasted the energy.
Summary of the invention
The object of the present invention is to provide the power-economizing method in a kind of chlorination reaction process, this method is utilized chilled brine to recycle to reach purpose of energy saving.
The present invention is realized by following technical proposals, a kind of power-economizing method of chlorination reaction process, described chlorination reaction process, the device that adopts comprises chlorination reactor, the chlorine feed that participates in reaction comes from the chlorine steam that chlorine liquid carburetor provides, need capture reaction mass and low-boiling products by cryogenic heat exchanger during chlorination reaction, in order to avoid leave reactor with hydrogen chloride gas, the heat-eliminating medium of this interchanger derives from the chilled brine that refrigerator provides, realize the energy-conservation of this chlorination reaction process, it is characterized in that comprising following process: the hypothermic saline that will come from refrigerator delivers to cryogenic heat exchanger and the lower boiling material carries out heat exchange, salt solution after the intensification is delivered to the medium of chlorine liquid carburetor as liquid chlorine vaporization heating, the required heat of liquid chlorine vaporization is provided and is lowered the temperature, salt solution after the cooling is delivered to refrigerator again and further is cooled to hypothermic saline, proceed to cryogenic heat exchanger so form salt solution by refrigerator, carry out heat exchange to chlorine liquid carburetor again, get back to the process that recycles of refrigerator at last, realize that salt solution is by low temperature → intensification → cooling → cryogenic temperature changing process, thereby reduce brine temp by the latent heat that utilizes the liquid chlorine vaporization to be absorbed, save the power consumption of refrigerator, reached the energy-conservation purpose of chlorination reaction process.
The invention has the advantages that, the evaporative process and the refrigeration system of liquid chlorine are got up by the circulating brine series combination, utilize intensification salt solution that liquid chlorine is vaporized, realized the cascade utilization of energy, saved the energy consumption of heating steam; Liquid chlorine vaporization simultaneously will absorb intensification brinish energy, makes its cooling, reaches the purpose that reduces the refrigerator energy consumption.This process is simple, is easy to realize.
Description of drawings
Fig. 1 is for realizing process flow diagram of the present invention.
Among the figure: 1-chlorine liquid carburetor, 2-chlorination reactor, 3-cryogenic heat exchanger, 4-refrigerator.
Embodiment
Embodiment
Below in conjunction with Fig. 1 the present invention is specified :-14 ℃～-15 ℃ chilled brine to cryogenic heat exchanger 3 and the gas material that chlorination reaction produces that comes out from refrigerator 4 carries out heat exchange, the salt solution that is come out by interchanger 3 is warming up to-6 ℃～-7 ℃, salt solution after should heating up then to chlorine liquid carburetor 1 as heating medium, carry out heat exchange with liquid chlorine, the chlorine that produces is to the raw material of chlorination reactor 2 as chlorination reaction, salt solution obtains to be cooled to-9 ℃～-10 ℃, and the salt solution after this cooling is back to refrigerator 4 to carry out further refrigeration cool-down and reach-14 ℃～-15 ℃.Salt solution is so recycled by refrigerator 4 → cryogenic heat exchanger 3 → chlorine liquid carburetor 1 → refrigerator 4, and in working cycle, salt solution has utilized the latent heat of vaporization of liquid chlorine, has saved the power consumption of refrigerator, has saved the liquid chlorine needed heat of vaporizing simultaneously.
Producing Mono Chloro Acetic Acid with certain enterprise is example, and this installs average chlorine dosage is 691kg/h, and the thermal load of the cryogenic heat exchanger of conversion unit (water cooler) is 70,000 kilocalories/h.
Salt solution is all by refrigerator refrigeration, refrigerator day power consumption 840KWh before transforming.The liquid chlorine vaporization is all by steam heating, and steam consumption is 95kg/h.After changing technological process into technical process of the present invention, a refrigerator refrigeration day power consumption 571KWh, the liquid chlorine vaporization does not need steam heating.This technical process institute consumed energy is compared every day refrigerator refrigeration and can be economized on electricity approximately 1/3 with former flow process, do not consume steam in addition.
Claims (1)
1. the power-economizing method of a chlorination reaction process, described chlorination reaction process, the device that adopts comprises chlorination reactor, the chlorine feed that participates in reaction comes from the chlorine steam that chlorine liquid carburetor provides, need capture reaction mass and low-boiling products by cryogenic heat exchanger during chlorination reaction, in order to avoid leave reactor with hydrogen chloride gas, the heat-eliminating medium of this interchanger derives from the chilled brine that refrigerator provides, realize the energy-conservation of this chlorination reaction process, it is characterized in that comprising following process: the hypothermic saline that will come from refrigerator delivers to cryogenic heat exchanger and the lower boiling material carries out heat exchange, salt solution after the intensification is delivered to the medium of chlorine liquid carburetor as liquid chlorine vaporization heating, the required heat of liquid chlorine vaporization is provided and is lowered the temperature, salt solution after the cooling is delivered to refrigerator again and further is cooled to hypothermic saline, proceed to cryogenic heat exchanger so form salt solution by refrigerator, carry out heat exchange to chlorine liquid carburetor again, get back to the process that recycles of refrigerator at last, realize that salt solution is by low temperature → intensification → cooling → cryogenic temperature changing process, thereby reduce brine temp by the latent heat that utilizes the liquid chlorine vaporization to be absorbed, save the power consumption of refrigerator, reached the energy-conservation purpose of chlorination reaction process.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2008100522097A CN101224879B (en) | 2008-01-30 | 2008-01-30 | Energy-saving method for chlorination reaction process |
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| Application Number | Priority Date | Filing Date | Title |
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| CN2008100522097A CN101224879B (en) | 2008-01-30 | 2008-01-30 | Energy-saving method for chlorination reaction process |
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| Publication Number | Publication Date |
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| CN101224879A true CN101224879A (en) | 2008-07-23 |
| CN101224879B CN101224879B (en) | 2010-09-08 |
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| CN2008100522097A Expired - Fee Related CN101224879B (en) | 2008-01-30 | 2008-01-30 | Energy-saving method for chlorination reaction process |
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Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107930546A (en) * | 2017-11-30 | 2018-04-20 | 山东凯盛新材料股份有限公司 | Produce the cold utilization process of thionyl chloride |
| CN108036667A (en) * | 2017-11-30 | 2018-05-15 | 山东凯盛新材料股份有限公司 | Produce the raw material cryogenic energy utilization technique of thionyl chloride |
| CN108467017A (en) * | 2018-06-05 | 2018-08-31 | 中国天辰工程有限公司 | A kind of sulfur dioxide gasification process for thionyl chloride production |
| CN109879251A (en) * | 2019-03-07 | 2019-06-14 | 南京工程学院 | A kind of hydrogen chloride synthesis system based on total energy approach |
| CN112299474A (en) * | 2020-11-13 | 2021-02-02 | 云南国钛金属股份有限公司 | Method for refining titanium tetrachloride and removing vanadium |
| CN115349574A (en) * | 2022-09-07 | 2022-11-18 | 杭州佰倍优生物科技有限公司 | Albumin polypeptide ultrafiltration system and device for inhibiting hydrolysis and removing bitter taste |
-
2008
- 2008-01-30 CN CN2008100522097A patent/CN101224879B/en not_active Expired - Fee Related
Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107930546A (en) * | 2017-11-30 | 2018-04-20 | 山东凯盛新材料股份有限公司 | Produce the cold utilization process of thionyl chloride |
| CN108036667A (en) * | 2017-11-30 | 2018-05-15 | 山东凯盛新材料股份有限公司 | Produce the raw material cryogenic energy utilization technique of thionyl chloride |
| CN108467017A (en) * | 2018-06-05 | 2018-08-31 | 中国天辰工程有限公司 | A kind of sulfur dioxide gasification process for thionyl chloride production |
| CN109879251A (en) * | 2019-03-07 | 2019-06-14 | 南京工程学院 | A kind of hydrogen chloride synthesis system based on total energy approach |
| CN109879251B (en) * | 2019-03-07 | 2024-05-03 | 南京工程学院 | Hydrogen chloride synthesis system based on energy comprehensive utilization |
| CN112299474A (en) * | 2020-11-13 | 2021-02-02 | 云南国钛金属股份有限公司 | Method for refining titanium tetrachloride and removing vanadium |
| CN115349574A (en) * | 2022-09-07 | 2022-11-18 | 杭州佰倍优生物科技有限公司 | Albumin polypeptide ultrafiltration system and device for inhibiting hydrolysis and removing bitter taste |
| CN115349574B (en) * | 2022-09-07 | 2023-08-18 | 杭州佰倍优生物科技有限公司 | Albumin polypeptide ultrafiltration system and device for inhibiting hydrolysis and removing bitter taste |
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|---|---|
| CN101224879B (en) | 2010-09-08 |
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