CN210078872U - Dilute sulfuric acid concentration device - Google Patents
Dilute sulfuric acid concentration device Download PDFInfo
- Publication number
- CN210078872U CN210078872U CN201920757156.2U CN201920757156U CN210078872U CN 210078872 U CN210078872 U CN 210078872U CN 201920757156 U CN201920757156 U CN 201920757156U CN 210078872 U CN210078872 U CN 210078872U
- Authority
- CN
- China
- Prior art keywords
- sulfuric acid
- dilute sulfuric
- concentrated
- heating
- cauldron
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
Images
Landscapes
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Abstract
The utility model relates to a concentrated technical field of dilute sulfuric acid especially relates to a dilute sulfuric acid concentration device, including concentrated cauldron, the inside top-down of concentrated cauldron is equipped with the circulation passageway, and the top of concentrated cauldron is equipped with inlet and gas outlet, and the bottom of concentrated cauldron is equipped with the liquid outlet, and the bottom of circulation passageway is equipped with heating element. The utility model discloses dilute sulfuric acid is heated up constantly at the flow in-process, and moisture is constantly gasified, and the gaseous phase material upwards moves along the circulation passageway and carries out the heat and mass exchange with the dilute sulfuric acid contact of downward operation, and the concentrated cauldron is taken back to gasified sulfuric acid and the SO3 absorption band that decomposes out to the liquid phase commodity circulation of downward flow, and dilute sulfuric acid in the concentrated cauldron constantly risees at the removal process concentration, and final concentrated sulfuric acid flows from the liquid outlet of concentrated cauldron bottom. The utility model discloses form the gradient warm area and heat dilute sulfuric acid in concentrated cauldron, the further heat exchange of gasified moisture and dilute sulfuric acid in the dilute sulfuric acid has improved the concentrated effect and the concentration efficiency of dilute sulfuric acid, and has reduced the required energy resource consumption of heating.
Description
Technical Field
The utility model relates to a dilute sulfuric acid concentration technical field especially relates to a dilute sulfuric acid concentration device.
Background
At present, sulfuric acid is an important basic chemical raw material, is widely applied to the industries of chemical engineering, steel and the like, and is commonly used as a dehydrating agent, a reaction intermediate, a cleaning agent, a catalyst and the like in the industry. The concentration of the used sulfuric acid is usually reduced, or the used sulfuric acid becomes dilute sulfuric acid containing impurities and cannot be continuously used for production, and the sulfuric acid used in a plurality of industrial processes is finally treated in a waste acid mode or is simply treated and then discharged, so that the problems of serious resource waste and environmental pollution are caused.
In a chemical process system, the concentration and recovery of waste sulfuric acid are one of the problems to be solved urgently by many enterprises, and on one hand, the waste sulfuric acid must be treated for ensuring production; on the other hand, the problems of environmental pollution and protection caused by the pollution are solved. With the development of industrial technology and the demand for environmental protection, dilute sulfuric acid is generally concentrated, recovered and recycled, such as pot-type concentration, combustion concentration, high-temperature concentration, low-temperature concentration and the like, but due to the strong corrosivity of sulfuric acid, the high-temperature concentration process is often not feasible, the equipment is severely corroded, the operation period and the service life are short, the treatment efficiency of the equipment is low, and due to the high energy consumption of sulfuric acid concentration, the recovery value is not high, so that most users prefer to treat the dilute sulfuric acid as waste, and some enterprises even untreated directly discharge the dilute sulfuric acid, thereby polluting the environment.
SUMMERY OF THE UTILITY MODEL
Technical problem to be solved
The to-be-solved technical problem of the utility model is that the current dilute sulphuric acid enrichment facility consumes energy seriously, and the concentration effect is not good, problem that concentration efficiency is low.
(II) technical scheme
In order to solve the technical problem, the utility model provides a dilute sulfuric acid concentration device, including concentrated cauldron, the inside top-down of concentrated cauldron is equipped with the circulation passageway, the top of concentrated cauldron is equipped with inlet and gas outlet, the bottom of concentrated cauldron is equipped with the liquid outlet, the inlet with the gas outlet passes through the circulation passageway with the liquid outlet intercommunication, the bottom of circulation passageway is equipped with heating element.
Wherein, concentrated cauldron includes the concentrated subassembly of rectification and the concentrated subassembly of heating that top-down set gradually, the concentrated subassembly of rectification with the concentrated subassembly intercommunication of heating and internal structure play the circulation passageway, heating element set up in the concentrated subassembly of heating.
Wherein, the concentrated subassembly of rectification includes the tower body and packs the bed, pack the bed fill in the tower body the middle part of circulation passageway, the inlet with the gas outlet sets up the top of tower body, the bottom of tower body with the concentrated subassembly intercommunication of heating.
Wherein, be equipped with liquid distributor in the tower body, liquid distributor with the inlet is connected.
Wherein, be equipped with the gas phase collector in the tower body, the gas phase collector with the gas outlet is connected.
Wherein, the concentrated subassembly of heating includes the barrel, the axial of barrel with the axial vertical setting of tower body, the open-top of barrel with flange joint is passed through to the bottom of tower body, heating element set up in the inside bottom of barrel, the bottom of barrel is equipped with the liquid outlet.
Wherein, heating element includes heating tube bank, heating tube bank follows in the barrel the extending direction setting of circulation passageway.
Wherein the arrangement density of the heating tube bundle is gradually increased along the flow direction of the dilute sulfuric acid in the cylinder body.
Wherein, be equipped with on the concentrated cauldron and detect the temperature detector of different position temperature in the circulation passageway.
Wherein, still include evacuation subassembly, evacuation subassembly with concentrated cauldron is connected.
(III) advantageous effects
The above technical scheme of the utility model has following advantage: the utility model discloses a dilute sulfuric acid enrichment facility, dilute sulfuric acid is in the inside circulation passageway of concentrated cauldron by the inlet inflow of concentrated cauldron, and top-down flows in the circulation passageway, the bottom of circulation passageway has heating element, heating element heaies up for the circulation passageway, provide the heat for the evaporation of water in the dilute sulfuric acid, dilute sulfuric acid is constantly heated up at the in-process that flows, moisture constantly gasifies, the gas phase material is along circulation passageway upward movement, carry out the heat exchange with the dilute sulfuric acid contact of downward operation, the liquid phase commodity circulation of downward flow is with the sulphuric acid of gasification and the SO that decomposes out3The absorption band returns concentrated cauldron, and the dilute sulphuric acid in the concentrated cauldron constantly risees at the removal process concentration, and the concentrated sulfuric acid that finally reaches the required concentration flows from the liquid outlet of concentrated cauldron bottom, and gaseous phase material is after carrying out the heat exchange with dilute sulphuric acid, and remaining steam is discharged by the gas outlet at concentrated cauldron top. The utility model discloses form the gradient warm area and heat dilute sulfuric acid in concentrated cauldron, the further heat exchange of gasified moisture and dilute sulfuric acid in the dilute sulfuric acid, supplementary dilute sulfuric acid heating heaies up, has reduced the heating load of concentrated cauldron, has improved the concentrated effect and the concentrated efficiency of dilute sulfuric acid, and has reduced the required energy resource consumption of heating.
In addition to the technical problems addressed by the present invention, the technical features of the constituent technical solutions, and the advantages brought by the technical features of these technical solutions, which are described above, other technical features of the present invention and the advantages brought by these technical features will be further explained with reference to the accompanying drawings.
Drawings
FIG. 1 is a schematic structural diagram of a concentration kettle of a dilute sulfuric acid concentration device according to an embodiment of the present invention.
In the figure: 1: a flow-through channel; 2: a heating assembly; 3: a rectification concentration component; 4: heating the concentration assembly; 5: a flange; 6: a temperature detector; 11: a liquid inlet; 12: an air outlet; 13: a liquid outlet; 21: a heating tube bundle; 31: a tower body; 32: a packing bed layer; 33: a liquid distributor; 34: a gas phase collector; 41: and (4) a cylinder body.
Detailed Description
In order to make the objects, technical solutions and advantages of the embodiments of the present invention clearer, the technical solutions in the embodiments of the present invention will be clearly and completely described below with reference to the accompanying drawings in the embodiments of the present invention, and it is obvious that the described embodiments are some, but not all embodiments of the present invention. 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.
In the description of the present invention, it is to be noted that, unless otherwise explicitly specified or limited, the terms "mounted," "connected," and "connected" are to be construed broadly, and may be, for example, fixedly connected, detachably connected, or integrally connected; can be mechanically or electrically connected; they may be connected directly or indirectly through intervening media, or they may be interconnected between two elements. The specific meaning of the above terms in the present invention can be understood in specific cases to those skilled in the art.
In the description of the present invention, unless otherwise specified, "plurality", and "plural" mean two or more, and "several", and "several groups" mean one or more.
As shown in fig. 1, the embodiment of the utility model provides a dilute sulfuric acid concentration device, including concentrated cauldron, the inside top-down of concentrated cauldron is equipped with circulation passageway 1, and the top of concentrated cauldron is equipped with inlet 11 and gas outlet 12, and the bottom of concentrated cauldron is equipped with liquid outlet 13, and inlet 11 and gas outlet 12 are through circulation passageway 1 and liquid outlet 13 intercommunication, and the bottom of circulation passageway 1 is equipped with heating element 2.
In the dilute sulfuric acid concentration device of the utility model, dilute sulfuric acid flows into the circulation channel inside the concentration kettle from the liquid inlet of the concentration kettle and flows from top to bottom in the circulation channel, the bottom of the circulation channel is provided with a heating component,the heating assembly heats the circulation channel to provide heat for the evaporation of water in the dilute sulfuric acid, the dilute sulfuric acid is heated continuously in the flowing process, the water is gasified continuously, the gas-phase material moves upwards along the circulation channel and contacts with the dilute sulfuric acid moving downwards to perform heat and mass exchange, and the liquid-phase material flow flowing downwards is used for gasifying the sulfuric acid and the decomposed SO3The absorption band returns concentrated cauldron, and the dilute sulphuric acid in the concentrated cauldron constantly risees at the removal process concentration, and the concentrated sulfuric acid that finally reaches the required concentration flows from the liquid outlet of concentrated cauldron bottom, and gaseous phase material is after carrying out the heat exchange with dilute sulphuric acid, and remaining steam is discharged by the gas outlet at concentrated cauldron top. The utility model discloses form the gradient warm area and heat dilute sulfuric acid in concentrated cauldron, the further heat exchange of gasified moisture and dilute sulfuric acid in the dilute sulfuric acid, supplementary dilute sulfuric acid heating heaies up, has reduced the heating load of concentrated cauldron, has improved the concentrated effect and the concentrated efficiency of dilute sulfuric acid, and has reduced the required energy resource consumption of heating.
In one embodiment, the concentration kettle comprises a rectification concentration component 3 and a heating concentration component 4 which are sequentially arranged from top to bottom, the rectification concentration component 3 is communicated with the heating concentration component 4, a circulation channel 1 is formed in the rectification concentration component 3, and the heating component 2 is arranged in the heating concentration component 4. The rectification concentration component is communicated with the heating concentration component, the inner space of the rectification concentration component forms a circulation channel, the rectification concentration component and dilute sulfuric acid enter the upper part of the concentration kettle through a liquid inlet and flow to the heating concentration component at the lower part of the concentration kettle along the rectification concentration component, the dilute sulfuric acid is continuously heated and heated in the flowing process of the heating concentration component, the moisture is continuously gasified, the gas-phase material moves upwards along the rectification concentration component and is contacted with the dilute sulfuric acid which moves downwards in the rectification concentration component to carry out heat-mass exchange, and the gasified sulfuric acid and the decomposed SO are subjected to liquid-phase material flow by the liquid-phase material flow which flows downwards3The concentrated section of absorption band back heating, the sulphuric acid in the concentration cauldron constantly risees at removal process concentration, finally reaches the concentrated sulfuric acid of required concentration and flows out from the liquid outlet of heating concentration subassembly.
In one embodiment, the distillation concentration assembly 3 comprises a tower body 31 and a packing bed layer 32, the packing bed layer 32 is filled in the middle of the flow channel 1 in the tower body 31, the liquid inlet 11 and the gas outlet 12 are arranged at the top of the tower body 31, and the bottom of the tower body 31 is communicated with the heating concentration assembly 4. The dilute sulfuric acid enters the flow channel from the liquid inlet of the tower body after being preheated, the middle part of the flow channel of the tower body is a filling section for filling a filling bed layer, the filling bed layer is positioned below the liquid inlet, the dilute sulfuric acid moves downwards along the filling bed layer, the concentration kettle keeps negative pressure operation by a water ring vacuum pump, under the action of vacuum, part of moisture is gasified and enters the condensation system, liquid-phase materials flow downwards along the filling bed layer and enter the heating concentration assembly, the dilute sulfuric acid is heated and heated continuously while moving in the heating concentration assembly, the moisture is gasified continuously, and gas-phase materials enter the tower body and move upwards along the filling bed layer and are in retrograde contact with the liquid-phase materials in the filling bed layer.
In the embodiment, the rectification concentration assembly is a vertical tower body, the height-diameter ratio is 2-6: 1, the filler bed layers can be single-layer or multi-layer, single-layer fillers are arranged if the concentration range of dilute sulfuric acid is not large, multi-layer fillers are arranged if the concentration range is large, and a liquid collecting and redistributing disc is arranged between every two adjacent filler bed layers, so that the dilute sulfuric acid flowing into the filler bed layers can be uniformly dispersed, the sufficient mass transfer and heat transfer of the dilute sulfuric acid and evaporated gas-phase materials are realized, the sulfuric acid concentration effect is ensured, and the acid amount brought by evaporated water vapor is reduced as much as possible. In the embodiment, the size of the tower body is phi 500 multiplied by 1000mm, the circulating channel of the tower body is filled with scattered ceramic filler with the height of 600mm as a filler bed layer, and the air outlet is positioned above the liquid inlet.
In one embodiment, a liquid distributor 33 is provided in the column body 31, the liquid distributor 33 being connected to the liquid inlet 11. The dilute sulfuric acid enters the liquid distributor from the liquid inlet of the tower body and is uniformly sprayed to the upper surface of the packed bed layer from the liquid distributor. In the embodiment, the liquid distributor is conical, a bottom plate of the liquid distributor is a circular plate with holes and having a certain opening rate, the upper part of the bottom plate is a conical cylinder, one third part of the lower part of the conical cylinder is provided with holes, and the opening rate of the liquid distributor is set to be 5-8: 1. The bottom plate and the cylinder are arranged at a fixed angle, so that liquid is uniformly sprayed out from the distributor without bias flow, and the liquid is uniformly dispersed on the surface of the lower packed bed layer. The space distance between the liquid distributor and the top of the packing bed layer is controlled to be 150-450 mm, and preferably 200-300 mm.
In one embodiment, a gas phase collector 34 is arranged in the tower body 31, and the gas phase collector 34 is connected with the gas outlet 12. The top air outlet of the tower body is provided with the gas phase collector, gas phase materials are discharged to the outside of the tower body through the gas phase collector after being subjected to mass heat exchange with liquid phase materials through the filler bed layer, and the gas phase collector more fully collects steam at the air outlet of the tower body and sends the steam out, so that water vapor in the tower body is reduced.
In one embodiment, the heating concentration assembly 4 comprises a cylinder 41, the axial direction of the cylinder 41 is perpendicular to the axial direction of the tower body 31, the top opening of the cylinder 41 is connected with the bottom of the tower body 31 through a flange 5, the heating assembly 2 is arranged at the inner bottom of the cylinder 41, and the bottom of the cylinder 41 is provided with a liquid outlet 13. The barrel of the concentrated subassembly of heating is horizontal barrel, barrel axial sets up with tower body axial vertical, be equipped with the opening directly over barrel one end, the opening just right just passes through flange interconnect with the lower extreme opening of the concentrated subassembly tower body of rectification, set up the liquid outlet under the other end of barrel, dilute sulfuric acid flows into in the barrel of the concentrated subassembly of heating by the opening behind the concentrated subassembly of rectification, and flow along the barrel, heating element sets up in the barrel, dilute sulfuric acid is constantly heated at the flow process, the gaseous phase material is got back to in the concentrated subassembly of rectification through the opening, the liquid phase material then forms concentrated sulfuric acid and flows out by the liquid outlet. In the embodiment, the length-diameter ratio of the cylinder is 2-6: 1, and the preferable size is phi 1000 multiplied by 2400 mm.
In one embodiment, the heating assembly 2 comprises a heating tube bundle 21, the heating tube bundle 21 being arranged along the extension of the flow channel 1 within the cylinder 41. The heating tube bundle is arranged at the middle lower part in the cylinder body along the axial direction of the cylinder body, and provides concentrated heat for the dilute sulfuric acid in the flowing process in the flow channel of the cylinder body, so that the water is continuously evaporated in the moving process of the dilute sulfuric acid, the concentration is continuously increased, and finally the concentrated sulfuric acid reaching the required concentration flows out from the liquid outlet of the cylinder body. The heating power of the heating tube bundle in the embodiment is 120kW, and the heating tube bundle can be an electric heating tube bundle or a high-temperature heat conducting oil heating tube bundle.
In one embodiment, the heating tube bundle 21 is arranged at a density that gradually increases in the direction of flow of the dilute sulfuric acid within the cylinder 41. The arrangement density of the heating tube bundles is gradually increased along with the flow direction of the liquid-phase material in the cylinder, the temperature of the liquid-phase material provided for the liquid-phase material by the heating concentration assembly in the moving process of the liquid-phase material is gradually increased, and the concentration efficiency and effect of the dilute sulfuric acid are improved.
In one embodiment, the concentration tank is provided with temperature detectors 6 for detecting temperatures at different positions in the flow channel 1. The key part of the rectification concentration component is provided with a temperature detector for controlling the rectification effect of the dilute sulfuric acid in the internal circulation channel. In this embodiment, temperature detectors are disposed in the tower body above the packing bed, in the packing bed, and below the packing bed at the flow channels. The key part of the heating concentration component is provided with a temperature detector for controlling the concentration effect and safety monitoring of the dilute sulfuric acid in the internal circulation channel. In this embodiment, a plurality of temperature detectors are sequentially provided in the cylinder along the extending direction of the flow channel.
In one embodiment, the dilute sulfuric acid concentration device further comprises a vacuum pumping assembly, and the vacuum pumping assembly is connected with the concentration kettle. The vacuum condition of the concentration kettle is provided by the matched vacuumizing assembly, the vacuumizing assembly can enable the concentration kettle to keep negative pressure operation, the boiling point of water in the dilute sulfuric acid can be effectively reduced under the vacuum state, and therefore the heating temperature of the concentration kettle is reduced, energy is saved, the equipment is protected, the service life of the extender is prolonged, and meanwhile the concentrating effect of the dilute sulfuric acid can be guaranteed. In the embodiment, the vacuum pumping assembly adopts a liquid ring vacuum pump, so that the pressure in the concentration kettle is 2-50 kPa, preferably 5-20 kPa.
When in use, the dilute sulphuric acid concentration device of the utility model can adopt different matching processes to concentrate the dilute sulphuric acid concentration from 10 percent to 96 percent, preferably from 60 percent to 92 percent. The method can be used in the fields of chemical industry, steel industry, medicine industry, printing and dyeing industry and the like, adopts different pretreatment measures for different impurities contained in dilute sulfuric acid generated under different working conditions, has obvious concentration effect, and can be used by connecting two or more concentration kettles in series or in parallel according to process requirements. A certain chlor-alkali device is used for the useless dilute sulfuric acid after the chlorine is dry, flow 500kg/h, sulfuric acid concentration 75%, through the utility model discloses after the dilute sulfuric acid enrichment facility concentration, concentrated sulfuric acid concentration is greater than 92%.
To sum up, the utility model discloses a dilute sulfuric acid enrichment facility, dilute sulfuric acid flows into in the inside circulation passageway of concentrated cauldron by the inlet of concentrated cauldron, and top-down flows in the circulation passageway, the bottom of circulation passageway has heating element, heating element heaies up for the circulation passageway, provide the heat for the evaporation of water in the dilute sulfuric acid, dilute sulfuric acid is by constantly heating up at the in-process that flows, moisture constantly gasifies, the gaseous phase material upwards moves along the circulation passageway, carry out the heat mass exchange with the dilute sulfuric acid contact of downwards moving, the liquid phase commodity circulation of downwards flowing is with the sulphuric acid of gasification and the SO that decomposes out3The absorption band returns concentrated cauldron, and the dilute sulphuric acid in the concentrated cauldron constantly risees at the removal process concentration, and the concentrated sulfuric acid that finally reaches the required concentration flows from the liquid outlet of concentrated cauldron bottom, and gaseous phase material is after carrying out the heat exchange with dilute sulphuric acid, and remaining steam is discharged by the gas outlet at concentrated cauldron top. The utility model discloses form the gradient warm area and heat dilute sulfuric acid in concentrated cauldron, the further heat exchange of gasified moisture and dilute sulfuric acid in the dilute sulfuric acid, supplementary dilute sulfuric acid heating heaies up, has reduced the heating load of concentrated cauldron, has improved the concentrated effect and the concentrated efficiency of dilute sulfuric acid, and has reduced the required energy resource consumption of heating.
Finally, it should be noted that: the above embodiments are only used to illustrate the technical solution of the present invention, and not to limit it; although the present invention has been described in detail with reference to the foregoing embodiments, it should be understood by those skilled in the art that: the technical solutions described in the foregoing embodiments may still be modified, or some technical features may be equivalently replaced; such modifications and substitutions do not depart from the spirit and scope of the present invention in its corresponding aspects.
Claims (10)
1. A dilute sulfuric acid concentration device is characterized in that: including concentrated cauldron, the inside top-down of concentrated cauldron is equipped with the circulation passageway, the top of concentrated cauldron is equipped with inlet and gas outlet, the bottom of concentrated cauldron is equipped with the liquid outlet, the inlet with the gas outlet passes through the circulation passageway with the liquid outlet intercommunication, the bottom of circulation passageway is equipped with heating element.
2. The dilute sulfuric acid concentration device according to claim 1, wherein: the concentrated cauldron includes the concentrated subassembly of rectification and the concentrated subassembly of heating that top-down set gradually, the concentrated subassembly of rectification with the concentrated subassembly intercommunication of heating and internal structure play the circulation passageway, heating element set up in the concentrated subassembly of heating.
3. The dilute sulfuric acid concentration device according to claim 2, wherein: the concentrated subassembly of rectification includes the tower body and packs the bed, pack the bed fill in the tower body the middle part of circulation passageway, the inlet with the gas outlet sets up the top of tower body, the bottom of tower body with the concentrated subassembly intercommunication of heating.
4. The dilute sulfuric acid concentration device according to claim 3, wherein: the tower body is internally provided with a liquid distributor, and the liquid distributor is connected with the liquid inlet.
5. The dilute sulfuric acid concentration device according to claim 3, wherein: and a gas phase collector is arranged in the tower body and is connected with the gas outlet.
6. The dilute sulfuric acid concentration device according to claim 3, wherein: the concentrated subassembly of heating includes the barrel, the axial of barrel with the axial vertical setting of tower body, the open-top of barrel with flange joint is passed through to the bottom of tower body, heating element set up in the inside bottom of barrel, the bottom of barrel is equipped with the liquid outlet.
7. The dilute sulfuric acid concentration device according to claim 6, wherein: the heating assembly comprises a heating tube bundle, and the heating tube bundle is arranged in the cylinder in the extending direction of the circulation channel.
8. The dilute sulfuric acid concentration device according to claim 7, wherein: the arrangement density of the heating tube bundles is gradually increased along the flow direction of the dilute sulfuric acid in the cylinder body.
9. The dilute sulfuric acid concentration device according to claim 1, wherein: and the concentration kettle is provided with a temperature detector for detecting the temperature of different positions in the circulation channel.
10. The dilute sulfuric acid concentration device according to any one of claims 1 to 9, wherein: still include the evacuation subassembly, the evacuation subassembly with concentrated cauldron is connected.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201920757156.2U CN210078872U (en) | 2019-05-23 | 2019-05-23 | Dilute sulfuric acid concentration device |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201920757156.2U CN210078872U (en) | 2019-05-23 | 2019-05-23 | Dilute sulfuric acid concentration device |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN210078872U true CN210078872U (en) | 2020-02-18 |
Family
ID=69479892
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201920757156.2U Active CN210078872U (en) | 2019-05-23 | 2019-05-23 | Dilute sulfuric acid concentration device |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN210078872U (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112494969A (en) * | 2020-11-10 | 2021-03-16 | 衡阳丰联精细化工有限公司 | Dilute sulfuric acid concentration device and system thereof |
| CN113321191A (en) * | 2020-02-28 | 2021-08-31 | 博特化工装置股份公司 | Sulfuric acid concentration equipment |
| CN114588646A (en) * | 2021-03-26 | 2022-06-07 | 江苏御镐智能制造有限公司 | Waste acid concentration treatment tower |
-
2019
- 2019-05-23 CN CN201920757156.2U patent/CN210078872U/en active Active
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113321191A (en) * | 2020-02-28 | 2021-08-31 | 博特化工装置股份公司 | Sulfuric acid concentration equipment |
| CN113321191B (en) * | 2020-02-28 | 2024-04-16 | 博特化工装置股份公司 | Sulfuric acid concentration equipment |
| CN112494969A (en) * | 2020-11-10 | 2021-03-16 | 衡阳丰联精细化工有限公司 | Dilute sulfuric acid concentration device and system thereof |
| CN114588646A (en) * | 2021-03-26 | 2022-06-07 | 江苏御镐智能制造有限公司 | Waste acid concentration treatment tower |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN210078872U (en) | Dilute sulfuric acid concentration device | |
| CN110054164B (en) | Concentrated recovery system of dilute sulfuric acid | |
| CN113215592B (en) | Comprehensive heat management system of large alkaline electrolyzed water hydrogen production device | |
| CN102267868B (en) | Industrial production apparatus for trichloroethylene | |
| CN210065174U (en) | Concentrated recovery system of dilute sulfuric acid | |
| CN205948388U (en) | Flash distillation of tower tray formula heat transfer integration equipment | |
| CN105923610B (en) | Acetylene cleaning acid regeneration technique | |
| CN210786298U (en) | Pyrolysis gas grading treatment device | |
| CN201762266U (en) | Trichloroethylene industrialized production device | |
| CN102350068B (en) | Falling film evaporation reboiler | |
| CN112661110A (en) | Hydrogen production system | |
| WO2014006742A1 (en) | Device for treating saline wastewater and method for treating same | |
| CN217612931U (en) | Byproduct recovery unit of eight bromo ether production usefulness of methyl | |
| KR101178486B1 (en) | Condenser for gas from thermal decomposition of polymer-compound-wastes | |
| CN208394816U (en) | A kind of flash evaporation plate-type falling film evaporator | |
| CN113560319B (en) | Solvent gasification pyrolysis device and method for waste circuit board | |
| CN217708963U (en) | Furfuryl alcohol coproduction 2-methyl furan technology waste water treatment recycling system | |
| CN216549990U (en) | Waste liquid recycling system | |
| CN108726475A (en) | A kind of hydrogen producer and its hydrogen production process | |
| CN212687558U (en) | Hydrogen bromide's purification device | |
| CN208406934U (en) | Unsym-trimethyl benzene oxidation separation device | |
| CN210159229U (en) | Novel chemical industry rectification device | |
| CN208694286U (en) | It is a kind of for synthesizing the reaction unit of pseudocumene | |
| CN111228941A (en) | Tail gas separation device and method in process for electrochemically synthesizing adiponitrile from acrylonitrile | |
| CN212102070U (en) | Distillation device |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant |