CN202700367U - Wet-process recovery device - Google Patents
Wet-process recovery device Download PDFInfo
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- CN202700367U CN202700367U CN2012203557244U CN201220355724U CN202700367U CN 202700367 U CN202700367 U CN 202700367U CN 2012203557244 U CN2012203557244 U CN 2012203557244U CN 201220355724 U CN201220355724 U CN 201220355724U CN 202700367 U CN202700367 U CN 202700367U
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- reative cell
- absorption tower
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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
- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/584—Recycling of catalysts
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Abstract
The utility model relates to a wet-process recovery device. The wet-process recovery device comprises an absorption tower (1), wherein the inside of the absorption tower (1) is divided into a first reaction chamber and a second reaction chamber, the top and the bottom of the first reaction chamber are respectively communicated with the top and the bottom of the second reaction chamber, a gas distributor (3) is disposed at the bottom of the first reaction chamber, and a gas supply device (4) is disposed at the bottom of the second reaction chamber. In the wet-process recovery device, an absorption process of feed gas and a regeneration process of a catalyst can be continuously implemented.
Description
Technical field
The utility model relates to a kind of hydrometallurgic recovery device.
Background technology
At present, in traditional wet method sulfur recovery technique, relate generally to absorption process and catalyst regeneration process, in absorption and two different devices of regenerating, finish respectively.Finish that the catalyst of inactivation need to be transported to regenerating unit by extra pump behind the absorption reaction, being transmitted back to absorption plant by pump again after processing through regeneration.So move in circles, power consumption is larger, and equipment is complicated.In order to save the energy, reduction equipment is taken up an area the space, and absorption process and catalyst regeneration process are incorporated into the development trend that same device is present wet method sulfur recovery unit.
CN1237474A discloses a kind of liquid phase catalytic oxidation desulfurizer, wherein, can segmentation carry out gas scrubbing desulfurization and desulfurization regeneration on a desulfurizing tower, and regenerator replaces with jet regeneration tank.This appliance arrangement is few, takes up an area littlely, and power consumption reduces, yet Structure of Flue Gas Desulfuration Absorbing is comparatively complicated, implements more loaded down with trivial details.
CN101327396A discloses a kind of spraying oxidizing tower device of wet method sulfur recovery, wherein, absorb and regenerative process can design in single device, but need to control absorption and regenerative process hockets according to color detection equipment, two processes can not be carried out simultaneously.
The utility model content
The purpose of this utility model is to overcome the defects that existing sulfur recovery unit exists, and a kind of new hydrometallurgic recovery device is provided.
The utility model provides a kind of hydrometallurgic recovery device, this device comprises the absorption tower, wherein, be divided into the first reative cell and the second reative cell in the described absorption tower, the top of described the first reative cell and bottom are communicated with top and the bottom of described the second reative cell respectively, the bottom of described the first reative cell is provided with gas distributor, and the bottom of described the second reative cell is provided with feeder.
In one embodiment, described the first reative cell and described the second reative cell are opened by baffle for separating.
In another embodiment, described absorption tower is built-in with cylinder, and the inner chamber of cylinder is described the first reative cell, and the space between the outer wall of cylinder and the inwall on absorption tower is described the second reative cell.Preferably, described cylinder is cylinder or square tube.
In the situation that described absorption tower is built-in with cylinder, described gas distributor is preferably circle distributor.
Preferably, described feeder is aerator.
Preferably, the volume of described the first reative cell is 1-10:1 with the ratio of the volume of described the second reative cell.
Preferably, the bottom on described absorption tower is taper.
Preferably, the bottom on described absorption tower is provided with opening.
Preferably, be provided with liquid-phase catalyst entrance, the outlet of unstripped gas tail gas, unstripped gas entrance and regeneration gas outlet on the top cover on described absorption tower.
Preferably, described device also comprises the anti-corrosion type spinner flowmeter, and described anti-corrosion type spinner flowmeter is communicated with described feeder by described unstripped gas entrance.
Preferably, described device also comprises the duct type flowmeter, and described duct type flowmeter is communicated with described gas distributor.
According to described hydrometallurgic recovery device of the present utility model, in the process of operation, first liquid-phase catalyst is added in the absorption tower, then in the second reative cell, pass into unstripped gas by feeder, described unstripped gas and described liquid-phase catalyst are reacted in described the second reative cell, also are absorption process; Simultaneously, in the first reative cell, pass into regeneration gas by gas distributor, and by regulating the flow of described regeneration gas and described unstripped gas, make the flow of described regeneration gas greater than the flow of described unstripped gas, thereby the interior liquid-phase catalyst of the first reative cell can be under the promotion of regeneration gas, top by the first reative cell enters the second reative cell, and the liquid-phase catalyst to be regenerated in the second reative cell (the also liquid-phase catalyst of i.e. process reaction) can enter through the bottom of the second reative cell the first reative cell under action of gravitation, this liquid-phase catalyst to be regenerated enters after the first reative cell, can react with regeneration gas, so that this liquid-phase catalyst to be regenerated is regenerated, it also is regenerative process; Liquid-phase catalyst after the regeneration can be circulated to the second reative cell again under the promotion of regeneration gas, thereby makes the liquid-phase catalyst in the absorption tower can loop absorption process and regeneration.Therefore, in described hydrometallurgic recovery device of the present utility model, can carry out continuously the absorption process of unstripped gas and the regenerative process of catalyst.
And, in the running of described hydrometallurgic recovery device of the present utility model, only need the circulation that flow can be realized the liquid-phase catalyst in the absorption tower that passes into by control regeneration gas and unstripped gas, thereby the purpose that the regenerative process that realizes making the absorption process of unstripped gas and catalyst is carried out synchronously, as seen, the operation of described hydrometallurgic recovery device of the present utility model is more easy.
Other feature and advantage of the present utility model will partly be described in detail in the specific embodiment subsequently.
Description of drawings
Accompanying drawing is to be used to provide further understanding of the present utility model, and consists of the part of specification, is used from explanation the utility model with the following specific embodiment one, but does not consist of restriction of the present utility model.In the accompanying drawings:
Fig. 1 is the structural representation according to a kind of embodiment of hydrometallurgic recovery device of the present utility model;
Fig. 2 is the structural representation according to the another kind of embodiment of hydrometallurgic recovery device of the present utility model.
Description of reference numerals
1 absorption tower 2a dividing plate
4 feeders, 5 top covers
The outlet of 6 liquid-phase catalyst entrances, 7 unstripped gas tail gas
The outlet of 8 unstripped gas entrances, 9 regeneration gases
10 openings, 11 duct type flowmeters
12 anti-corrosive properties spinner flowmeters, 13 temperature-detecting devices
The specific embodiment
Below in conjunction with accompanying drawing the specific embodiment of the present utility model is elaborated.Should be understood that, the specific embodiment described herein only is used for description and interpretation the utility model, is not limited to the utility model.
In the utility model, in the situation that do opposite explanation, upper and lower shown in " upper and lower " typically refers to reference to the accompanying drawings of the noun of locality of use; " inside and outside " refers to inside and outside with respect to the profile of each parts itself.
As depicted in figs. 1 and 2, described hydrometallurgic recovery device of the present utility model comprises absorption tower 1, wherein, be divided into the first reative cell and the second reative cell in the described absorption tower 1, the top of described the first reative cell and bottom are communicated with top and the bottom of described the second reative cell respectively, the bottom of described the first reative cell is provided with gas distributor 3, and the bottom of described the second reative cell is provided with feeder 4.
In the utility model, for two independently conversion zones are provided with the purpose that is divided into the first reative cell and the second reative cell in the described absorption tower 1, so that the regenerative process of the absorption process of unstripped gas and catalyst can carry out respectively, and do not produce the phase mutual interference.Therefore, the utility model for realize with absorption tower 1 be separated into two independently the specific embodiment of conversion zone do not have that there is no particular limitation.
In one embodiment, as shown in Figure 1, described the first reative cell and described the second reative cell are separated by dividing plate 2a.There is no particular limitation for the concrete shape of described dividing plate 2a, can be the flat board that vertically arranges, also can be for vertically arranging and have the plate of rule or irregular curved shape.In this embodiment, described gas distributor 3 and described feeder 4 preferably all are arranged between the top and bottom of described dividing plate 2a, and more preferably described gas distributor 3 and described feeder 4 are near the bottom of described dividing plate 2a.
In another embodiment, as shown in Figure 2, described absorption tower 1 is built-in with a 2b, and the inner chamber of cylinder 2b is described the first reative cell, and the space between the outer wall of cylinder 2b and the inwall on absorption tower 1 is described the second reative cell.In this embodiment, there is no particular limitation for the shape of described cylinder 2b, for example can for cylinder or square tube, be preferably cylinder.Described gas distributor 3 and described feeder 4 preferably all are arranged between the top and bottom of described cylinder 2b, and more preferably described gas distributor 3 and described feeder 4 are near the bottom of described cylinder 2b.
In described hydrometallurgic recovery device, when being provided with a tin 2b in the described absorption tower 1, the set-up mode of described cylinder 2b is preferably: make the central axis of described cylinder 2b parallel with the central axis on described absorption tower.Most preferably, the central axis of described cylinder 2b is overlapped substantially with the central axis on described absorption tower.In this case, described gas distributor 3 is preferably circle distributor, so that the regeneration gas that injects in the first reative cell by gas distributor 3 can be distributed in whole reative cell more equably.
In the utility model, described feeder 4 is mainly used in injecting unstripped gas to the second reative cell, and therefore, the conventional feeder that uses in this area all can be used as the feeder 4 in the described hydrometallurgic recovery device of the present utility model.Under the preferable case, described feeder 4 is aerator.When selecting aerator as described feeder 4, in the process of the unstripped gas that injects by aerator, can the liquid-phase catalyst in the second reative cell be stirred, thereby can promote the reaction that the second reative cell is interior.
When described the first reative cell and described the second reative cell are separated by dividing plate 2a, and when described feeder 4 was aerator, the top of described aerator was preferably 0.02-0.1 to the ratio of the distance between the bottom of described dividing plate 2a and the total height of described dividing plate 2a; 1; When described the first reative cell and described the second reative cell are separated by cylinder 2b, and described feeder 4 is when being aerator, and the top of described aerator is preferably 0.02-0.1 to the ratio of the distance between the bottom of described cylinder 2b and the total height of described cylinder 2b; 1.
In the utility model, the opening of the opening of described gas distributor 3 and described feeder 4 towards all there is no particular limitation, separately can be up, down or towards the side.Under the preferable case, the opening of the opening of described gas distributor 3 and described feeder 4 all up.
Described gas distributor 3 and described feeder 4 are preferably made by the material of acid and alkali-resistance, for example can be made by polypropylene material.
In the utility model, there is no particular limitation for the volume of described the first reative cell and described the second reative cell size.Under the preferable case, the volume of described the first reative cell is 1-10:1 with the ratio of the volume of described the second reative cell, is preferably 1-5:1, more preferably 1-3:1.
In the utility model, the bottom on described absorption tower 1 can be provided with opening 10, and the bottom on described absorption tower 1 is preferably designed for taper.In this case, be convenient to solid particulate matter sedimentation and discharge with the 1 interior generation of described absorption tower.
In the utility model, preferably be provided with liquid-phase catalyst entrance 6, unstripped gas tail gas outlet 7, unstripped gas entrance 8 and regeneration gas outlet 9 on the top cover 5 on described absorption tower 1.In described liquid-phase catalyst entrance 6, described unstripped gas tail gas outlet 7, described unstripped gas entrance 8 and described regeneration gas outlet 9, be provided with separately valve, so that these openings are conveniently closed when not using.Under the preferable case, described raw material tail gas outlet 7 be arranged on described feeder 4 directly over; Described regeneration gas outlet 9 be arranged on described gas distributor 3 directly over.Can adopt conventional connected mode to be connected between the tower body on described top cover 5 and described absorption tower 1, for example the mode of flange connection.Preferably be provided with the seal gasket of being made by high-elastic rubber between the tower body on described top cover 5 and described absorption tower 1, to guarantee described absorption tower good seal and for convenience detach.
Described hydrometallurgic recovery device can also comprise duct type flowmeter 11 and anti-corrosion type spinner flowmeter 12.Described anti-corrosion type spinner flowmeter 12 is communicated with described feeder 4 by described unstripped gas entrance 8.Described duct type flowmeter 11 is communicated with described gas distributor 3.
Described hydrometallurgic recovery device can also comprise temperature-detecting device 13.Described temperature detection and deriving means 13 are used for detecting in real time the temperature parameter in the absorption tower 1.The set-up mode of described temperature-detecting device 13 is identical with conventional absorption tower.The tower body on described absorption tower 1 is identical with conventional absorption tower, for example can be cylinder.The material on described absorption tower 1 does not have special requirement, yet for the ease of observing the progress of absorption tower 1 internal reaction, described absorption tower 1 is preferably made by transparent lucite.
Should be understood that, described hydrometallurgic recovery device of the present utility model is to carry out improved on the basis on existing absorption tower.Concrete, the main improvements of described hydrometallurgic recovery device of the present utility model are, with two reative cells that are divided into top and bottom in the absorption tower 1 and are interconnected, also be the first reative cell and the second reative cell, and in the bottom of the first reative cell gas distributor is set, in the second reative cell, feeder is set, thereby so that described hydrometallurgic recovery device can be realized the purpose that the regenerative process of the absorption process of unstripped gas and catalyst is carried out synchronously.
The utility model is described in further detail below in conjunction with the operation mechanism of described hydrometallurgic recovery device.
Take described hydrometallurgic recovery device shown in Figure 2 as example, the running of described hydrometallurgic recovery device mainly comprises: liquid-phase catalyst is added in the absorption tower 1, in the second reative cell, pass into unstripped gas by aerator 4, described unstripped gas and described liquid-phase catalyst are reacted in described the second reative cell, also are absorption process; Simultaneously, in the first reative cell, pass into regeneration gas by annular gas distributor 3, and by regulating the flow of described regeneration gas and described unstripped gas, the flow that makes described regeneration gas is greater than the flow of (or much larger than) described unstripped gas, thereby the interior liquid-phase catalyst of the first reative cell can be under the promotion of regeneration gas, top by the first reative cell enters the second reative cell, and the liquid-phase catalyst to be regenerated in the second reative cell (the also liquid-phase catalyst of i.e. process reaction) can enter through the bottom of the second reative cell the first reative cell under action of gravitation, this liquid-phase catalyst to be regenerated enters after the first reative cell, can react with regeneration gas, so that this liquid-phase catalyst to be regenerated is regenerated, it also is regenerative process; Liquid-phase catalyst after the regeneration can be circulated to the second reative cell again under the promotion of regeneration gas, thereby makes the liquid-phase catalyst in the absorption tower 1 can loop absorption process and regenerative process.
Concrete, take liquid-phase catalyst as Complexing Iron solution, unstripped gas as sulfurous gas as example, the running of hydrometallurgic recovery device shown in Figure 2 mainly comprises: Complexing Iron solution is added in the absorption tower 1, in the second reative cell, pass into sulfurous gas by aerator 4, make sulfurous gas and Complexing Iron solution in the second reative cell, redox reaction occur, sulphur component in the sulfurous gas is oxidized to sulphur, and finally can pass through opening 10 sedimentations and discharge, and ferric ion is reduced to ferrous ion; Simultaneously, pass into oxygen or air in the first reative cell as regeneration gas by annular gas distributor 3, and by regulating the flow of regeneration gas and sulfurous gas, the flow that makes regeneration gas is greater than the flow of (or much larger than) sulfurous gas, thereby the interior Complexing Iron solution of the first reative cell can be under the promotion of regeneration gas, top by the first reative cell enters the second reative cell, and the Complexing Iron solution that is reduced in the second reative cell can enter through the bottom of the second reative cell the first reative cell under action of gravitation, the Complexing Iron solution that this is reduced enters after the first reative cell, meeting and regeneration gas generation redox reaction, be ferric ion with oxidation of divalent iron ion, Complexing Iron solution is regenerated; Complexing Iron solution after the regeneration can be circulated to the second reative cell again under the promotion of regeneration gas, thereby makes the Complexing Iron solution in the absorption tower 1 can loop absorption process and regenerative process.
Below describe by reference to the accompanying drawings preferred embodiment of the present utility model in detail; but; the utility model is not limited to the detail in the above-mentioned embodiment; in technical conceive scope of the present utility model; can carry out multiple simple variant to the technical solution of the utility model, these simple variant all belong to protection domain of the present utility model.
Need to prove that in addition each the concrete technical characterictic described in the above-mentioned specific embodiment in reconcilable situation, can make up by any suitable mode.For fear of unnecessary repetition, the utility model is to the no longer separately explanation of various possible combinations.
In addition, also can carry out any combination between the various embodiment of the present utility model, as long as it is without prejudice to thought of the present utility model, it should be considered as content disclosed in the utility model equally.
Claims (12)
1. hydrometallurgic recovery device, this device comprises absorption tower (1), it is characterized in that, be divided into the first reative cell and the second reative cell in the described absorption tower (1), the top of described the first reative cell and bottom are communicated with top and the bottom of described the second reative cell respectively, the bottom of described the first reative cell is provided with gas distributor (3), and the bottom of described the second reative cell is provided with feeder (4).
2. device according to claim 1 is characterized in that, described the first reative cell and described the second reative cell are separated by dividing plate (2a).
3. device according to claim 1 is characterized in that, described absorption tower (1) is built-in with cylinder (2b), and the inner chamber of cylinder (2b) is described the first reative cell, and the space between the outer wall of cylinder (2b) and the inwall of absorption tower (1) is described the second reative cell.
4. device according to claim 3 is characterized in that, described cylinder (2b) is cylinder or square tube.
5. according to claim 3 or 4 described devices, it is characterized in that, described gas distributor (3) is circle distributor.
6. the described device of any one is characterized in that according to claim 1-4, and described feeder (4) is aerator.
7. the described device of any one is characterized in that according to claim 1-4, and the volume of described the first reative cell is 1-10:1 with the ratio of the volume of described the second reative cell.
8. the described device of any one is characterized in that according to claim 1-4, and the bottom of described absorption tower (1) is taper.
9. device according to claim 8 is characterized in that, the bottom of described absorption tower (1) is provided with opening (10).
10. the described device of any one according to claim 1-4, it is characterized in that, be provided with liquid-phase catalyst entrance (6), unstripped gas tail gas outlet (7), unstripped gas entrance (8) and regeneration gas outlet (9) on the top cover (5) of described absorption tower (1).
11. device according to claim 10 is characterized in that, described device also comprises anti-corrosion type spinner flowmeter (12), and described anti-corrosion type spinner flowmeter (12) is communicated with described feeder (4) by described unstripped gas entrance (8).
12. the described device of any one is characterized in that according to claim 1-4, described device also comprises duct type flowmeter (11), and described duct type flowmeter (11) is communicated with described gas distributor (3).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2012203557244U CN202700367U (en) | 2012-07-20 | 2012-07-20 | Wet-process recovery device |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2012203557244U CN202700367U (en) | 2012-07-20 | 2012-07-20 | Wet-process recovery device |
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| Publication Number | Publication Date |
|---|---|
| CN202700367U true CN202700367U (en) | 2013-01-30 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2012203557244U Expired - Lifetime CN202700367U (en) | 2012-07-20 | 2012-07-20 | Wet-process recovery device |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108236840A (en) * | 2017-11-07 | 2018-07-03 | 苏州市凯利勋实验室设备有限公司 | A kind of atomizing harmful gas purification tower |
-
2012
- 2012-07-20 CN CN2012203557244U patent/CN202700367U/en not_active Expired - Lifetime
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108236840A (en) * | 2017-11-07 | 2018-07-03 | 苏州市凯利勋实验室设备有限公司 | A kind of atomizing harmful gas purification tower |
| CN108236840B (en) * | 2017-11-07 | 2020-02-07 | 苏州市凯利勋实验室设备有限公司 | Atomizing harmful gas purifying tower |
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| GR01 | Patent grant | ||
| CX01 | Expiry of patent term |
Granted publication date: 20130130 |
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| CX01 | Expiry of patent term |