CN210457558U - Sour hot enrichment facility in dirty acid - Google Patents
Sour hot enrichment facility in dirty acid Download PDFInfo
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- CN210457558U CN210457558U CN201921023175.9U CN201921023175U CN210457558U CN 210457558 U CN210457558 U CN 210457558U CN 201921023175 U CN201921023175 U CN 201921023175U CN 210457558 U CN210457558 U CN 210457558U
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Abstract
The utility model discloses a waste acid medium-acid heat concentration device, which comprises at least two stages of evaporation concentration components which are arranged in sequence, wherein each stage of evaporation concentration component comprises a separation chamber, a heater and a circulating pump, two ends of the circulating pump are communicated with different positions of the separation chamber so as to circulate the dirty acid in the separation chamber, the heater is arranged on a circulating pipeline connected with the circulating pump and the separation chamber, a dirty acid inlet is arranged on the circulating pipeline of the first-stage evaporation concentration component, a steam inlet used for introducing fresh steam is arranged on the heater, the steam inlets of the heaters of other evaporation concentration components are communicated with the steam outlet of the separation chamber of the previous evaporation concentration component through a pipeline, and dirty acid inlets on the circulating pipelines of other evaporation concentration assemblies are communicated with an evaporation concentrated liquid outlet of the separation chamber of the previous evaporation concentration assembly through a pipeline. The utility model has the characteristics of resource recovery utilization rate is high, with low costs, no secondary pollution etc.
Description
Technical Field
The utility model belongs to the technical field of metallurgical environmental protection, especially, relate to a sour hot enrichment facility in sour.
Background
A large amount of flue gas containing high concentration of SO is generated in the non-ferrous metal smelting process2And some harmful metal components, the smelting plant realizes the recovery of smoke dust and SO2A large amount of strong acid wastewater containing heavy metals, namely waste acid wastewater, can be generated in the process of preparing acid from flue gas. The waste acid water has strong acidity, complex water quality, high content of toxic and harmful elements, and contains fluorinion, chloride ion and the like, and is mixed acid containing sulfuric acid, hydrofluoric acid, hydrochloric acid and the like.
The current common methods for treating waste acid and wastewater mainly comprise a vulcanization-neutralization method, a coagulating sedimentation method, an ion exchange method, an electrodialysis method and the like. The sulfuration-neutralization method has the advantages of wide application, mature process and low cost, but the resources in the process can not be effectively recovered, the treatment cost of the produced water treatment slag is high, and secondary pollution is easy to produce. In order to meet the requirements of water resource recycling and valuable resource recycling, the waste acid wastewater is treated by an evaporation concentration method, so that the resources can be effectively recycled, the treatment cost is reduced, and certain economic benefit can be obtained.
The thermal evaporation concentration method is a method of heating a part of a solvent in a solution to increase the concentration of the solution or concentrating the solution to saturation to precipitate a solute. The evaporation concentration method is widely applied to treatment of high-concentration organic wastewater, radioactive wastewater and landfill leachate due to the advantages of mature technology, simple process and the like, but the device for performing acid-heat concentration on waste acid by adopting the thermal evaporation concentration method in the prior art still has the problems of low treatment cost, poor concentration effect, high production energy consumption and the like.
SUMMERY OF THE UTILITY MODEL
The present application is directed to solving at least one of the problems in the prior art. Therefore, one of the purposes of the present invention is to provide an energy-saving and effective concentration device for acid-in-waste acid.
In order to solve the technical problem, the following technical scheme is adopted in the application:
the utility model provides a sour hot enrichment facility in dirty sour, includes the at least two-stage evaporation concentration subassembly that sets gradually, every level evaporation concentration subassembly includes separator, heater and circulating pump, the both ends of circulating pump communicate in the different positions of separator are in order to be used for making dirty sour circulation in the separator flows, the heater sets up the circulating pump with on the circulating line that the separator links to each other, be equipped with on the circulating line of first order evaporation concentration subassembly dirty sour entry and its heater and be equipped with the steam inlet who is used for letting in fresh steam, the steam inlet of the heater of other evaporation concentration subassemblies passes through the steam outlet intercommunication of pipeline and the separator of last one-level evaporation concentration subassembly, and dirty sour entry on the circulating line of other evaporation concentration subassemblies passes through the evaporation concentrate export intercommunication of pipeline and the separator of last one-level evaporation concentration subassembly.
Further, still include one-level preheater and second grade preheater, wait to evaporate dirty acid and pass through in proper order one-level preheater and second grade preheater preheat the back and get into the dirty acid entry of first order evaporation concentration subassembly.
Furthermore, the evaporation concentration assembly is divided into three stages, a steam outlet of a heater of the first-stage evaporation concentration assembly is communicated with a steam inlet of the second-stage preheater, and a steam outlet of a heater of the second-stage evaporation concentration assembly is communicated with a steam inlet of the first-stage preheater.
Furthermore, a gas-liquid separator is arranged on a steam outlet at the top of the separation chamber.
Further, the vapor outlet of the separation chamber of the last stage concentration assembly is connected to the condenser.
Furthermore, a graphite coating and a tetrafluoro coating are sequentially arranged on the inner wall of the heater from inside to outside.
Furthermore, the separation chamber is made of a steel lining PTFE material.
Furthermore, control valves are arranged on an evaporation concentrated liquid outlet of the separation chamber and the circulating pipeline.
Compared with the prior art, the utility model adopts the multi-stage evaporation concentration component to carry out evaporation concentration on the waste acid, no medicament is required to be added in the whole process, and the generated distillate has lower fluorine and chlorine content and can be recycled; the secondary steam can be effectively used as a heating source, the heat energy loss is reduced, and the method has the characteristics of high resource recovery rate, low cost, no secondary pollution and the like.
Drawings
Fig. 1 is a schematic structural diagram of the present invention.
Detailed Description
The technical solutions in the embodiments of the present invention will be described clearly and completely with reference to the accompanying drawings in the embodiments of the present invention, and it is obvious that the described embodiments are only some embodiments of the present invention, not all embodiments. Based on the embodiments in the present invention, all other embodiments obtained by a person skilled in the art without creative efforts belong to the protection scope of the present invention.
Referring to fig. 1, sour hot enrichment facility in sour, including the first order evaporative concentration subassembly, second level evaporative concentration subassembly and the third level evaporative concentration subassembly that set gradually, first order evaporative concentration subassembly includes that an effect separator 1, an effect heater 2 and an effect circulating pump 3, and second level evaporative concentration subassembly includes that two effect separator 4, two effect heater 5 and two effect circulating pump 6, and third level evaporative concentration subassembly includes that three effect separator 7, three effect heater 8 and three effect circulating pump 9. Two ends of each circulating pump are respectively communicated with the circulating outlet at the bottom part and the circulating inlet at the side part of the corresponding separating chamber so as to enable the waste acid in the separating chamber to circularly flow, and each heater is arranged on the circulating pipeline connected with the corresponding circulating pump and the separating chamber so as to heat the circularly flowing waste acid and enable the waste acid to be evaporated and concentrated; the top of each separation chamber is provided with a steam outlet, the steam outlet is provided with a gas-liquid separator 10, and a packing layer in the gas-liquid separator adopts high-temperature-resistant and corrosion-resistant packing.
The circulating pipeline of the first-stage evaporation concentration assembly is provided with a waste acid inlet, the effective heater 2 of the first-stage evaporation concentration assembly is provided with a steam inlet 11 for introducing fresh steam, the steam inlet of the second-stage evaporation concentration assembly of the second-stage heater 5 is communicated with a gas-liquid separator 10 on a steam outlet of the first-stage evaporation concentration assembly, and the waste acid inlet on the circulating pipeline of the second-stage evaporation concentration assembly is communicated with an evaporation concentrated solution outlet of the first-stage evaporation concentration assembly of the first-stage.
The steam inlet of the triple-effect heater 8 of the third-stage evaporation concentration assembly is communicated with the gas-liquid separator 10 on the steam outlet of the second-stage evaporation concentration chamber 4 in the second-stage evaporation concentration assembly through a pipeline, the dirty acid inlet on the circulating pipeline of the third-stage evaporation concentration assembly is communicated with the evaporation concentrated liquid outlet of the second-stage evaporation concentration chamber 4 of the second-stage evaporation concentration assembly through a pipeline, control valves are arranged on the evaporation concentrated liquid outlet and the circulating pipeline of the separation chamber in each stage of evaporation concentration assembly, the stability of the liquid level in the separation chamber is maintained by adjusting the introduction amount of dirty acid at the dirty acid inlet and the opening degree of each control valve, and the gas-liquid separator 10 on the triple-effect separation chamber 7 of the third-stage evaporation concentration assembly is connected.
Referring to fig. 1, in an embodiment, the concentration device further includes a first-stage preheater 13 and a second-stage preheater 14, a steam outlet of the first-stage evaporative concentration assembly first-effect heater 2 is communicated with a steam inlet of the second-stage preheater 14, a steam outlet of the second-stage evaporative concentration assembly second-effect heater 5 is communicated with a steam inlet of the first-stage preheater 13, and waste acid to be evaporated enters a waste acid inlet of the first-stage evaporative concentration assembly after being preheated by the first-stage preheater 13 and the second-stage preheater 14 in sequence. The first-stage preheater 13 and the second-stage preheater 14 preheat the inlet liquid by using the steam waste heat of the heaters, and the heat utilization rate is high.
It can be understood that because the waste acid has strong corrosivity, in order to prolong the service life of each part, the inner walls of the two-effect heater 5 and the three-effect heater 8 are sequentially provided with a graphite coating and a tetrafluoro coating from inside to outside, and each separation chamber can be made of steel lining tetrafluoro material.
The working process of the embodiment is as follows:
dirty acid with acidity of 10 percent and fluorine content of 3000mg/L and chlorine content of 3000mg/L flows through a first-stage preheater 13 and a second-stage preheater 14 through an evaporation liquid inlet and enters a first-stage evaporation concentration component;
high-temperature steam entering from a steam inlet 11 heats dirty acid in the primary-effect heater 2, after the dirty acid is heated by primary-effect forced circulation, gas phase is subjected to gas-liquid separation through a gas-liquid separator 10 at the upper end of the primary-effect separation chamber 1, an outlet of the gas-liquid separator 10 is connected with the secondary-effect heater 5, primary-effect evaporation concentrated solution overflows to the lower end of the secondary-effect separation chamber 4 and is subjected to secondary-effect evaporation concentration, and the secondary-effect evaporation concentration process is the same as the primary-effect concentration process;
the outlet of the triple-effect separation chamber 7 is connected with a condenser 12, so that triple-effect gas phase is condensed to form liquid, and the condenser 12 is connected with a vacuum unit 15;
after triple effect evaporation, the acidity of the concentrated solution is about 30 percent, and the concentrated solution is discharged and collected through an evaporation concentrated solution outlet of the triple effect separation chamber 7; the steam is condensed by the first-stage preheater 13, the second-stage preheater 14 and the condenser 12 to form distillate, and the distillate has low fluorine and chlorine content and can be recycled.
In the embodiment, the polluted acid is evaporated and concentrated by adopting the multi-stage evaporation and concentration assembly, no medicament is required to be added in the whole process, and the generated distillate has low fluorine and chlorine content and can be recycled; the secondary steam can be effectively used as a heating source, the heat energy loss is reduced, and the method has the characteristics of high resource recovery rate, low cost, no secondary pollution and the like.
The heater, the gas-liquid separator 10, the condenser 12, the primary preheater 13 and the secondary preheater 14 in this embodiment are all of the existing structure, and those skilled in the art can select the heater adaptively according to the actual concentration requirement.
The above examples are merely illustrative of the present invention clearly and are not intended to limit the embodiments. Other variations and modifications will be apparent to persons skilled in the art in light of the above description. Nor is it intended to be exhaustive of all embodiments. And obvious changes and modifications may be made without departing from the scope of the present invention.
Claims (8)
1. The utility model provides a sour hot enrichment facility in dirty acid which characterized in that: the device comprises at least two stages of evaporation concentration components which are arranged in sequence, wherein each stage of evaporation concentration component comprises a separation chamber, a heater and a circulating pump;
two ends of the circulating pump are communicated with different positions of the separation chamber so as to enable waste acid in the separation chamber to circularly flow, and the heater is arranged on a circulating pipeline connected with the circulating pump and the separation chamber;
the circulating pipeline of the first-stage evaporation concentration assembly is provided with a dirty acid inlet, the heater of the first-stage evaporation concentration assembly is provided with a steam inlet for introducing fresh steam, the steam inlets of the heaters of other evaporation concentration assemblies are communicated with the steam outlet of the separation chamber of the last-stage evaporation concentration assembly through pipelines, and the dirty acid inlets of the circulating pipeline of other evaporation concentration assemblies are communicated with the evaporation concentrated solution outlet of the separation chamber of the last-stage evaporation concentration assembly through pipelines.
2. The apparatus of claim 1, wherein: still include one-level preheater and second grade preheater, wait to evaporate dirty acid and pass through in proper order one-level preheater and second grade preheater preheat the back and get into the dirty acid entry of first order evaporation concentration subassembly.
3. The apparatus of claim 2, wherein: the number of stages of the evaporation concentration components is three, a steam outlet of a heater of the first-stage evaporation concentration component is communicated with a steam inlet of the second-stage preheater, and a steam outlet of a heater of the second-stage evaporation concentration component is communicated with a steam inlet of the first-stage preheater.
4. The apparatus of claim 1, wherein: and a gas-liquid separator is arranged on a steam outlet at the top of the separation chamber.
5. The apparatus of claim 1, wherein: the steam outlet of the separation chamber of the last stage concentration assembly is connected to the condenser.
6. The apparatus of claim 1, wherein: and the inner wall of the heater is sequentially provided with a graphite coating and a tetrafluoro coating from inside to outside.
7. The apparatus of claim 1, wherein: the separation chamber is made of a steel lining PTFE material.
8. The apparatus of claim 1, wherein: and control valves are arranged on the evaporation concentrated liquid outlet of the separation chamber and the circulating pipeline.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201921023175.9U CN210457558U (en) | 2019-07-02 | 2019-07-02 | Sour hot enrichment facility in dirty acid |
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| Application Number | Priority Date | Filing Date | Title |
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| CN201921023175.9U CN210457558U (en) | 2019-07-02 | 2019-07-02 | Sour hot enrichment facility in dirty acid |
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| CN210457558U true CN210457558U (en) | 2020-05-05 |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113476874A (en) * | 2021-07-29 | 2021-10-08 | 上海神农节能环保科技股份有限公司 | Multiple-effect evaporation crystallizer suitable for viscose fiber acid bath concentration crystallization |
| CN113476873A (en) * | 2021-07-29 | 2021-10-08 | 上海神农节能环保科技股份有限公司 | Multi-effect evaporator suitable for viscose fiber spinning scouring water concentration |
-
2019
- 2019-07-02 CN CN201921023175.9U patent/CN210457558U/en active Active
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113476874A (en) * | 2021-07-29 | 2021-10-08 | 上海神农节能环保科技股份有限公司 | Multiple-effect evaporation crystallizer suitable for viscose fiber acid bath concentration crystallization |
| CN113476873A (en) * | 2021-07-29 | 2021-10-08 | 上海神农节能环保科技股份有限公司 | Multi-effect evaporator suitable for viscose fiber spinning scouring water concentration |
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