CN204193648U - The retracting device of solvent in a kind of miscella - Google Patents
The retracting device of solvent in a kind of miscella Download PDFInfo
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- CN204193648U CN204193648U CN201420587525.5U CN201420587525U CN204193648U CN 204193648 U CN204193648 U CN 204193648U CN 201420587525 U CN201420587525 U CN 201420587525U CN 204193648 U CN204193648 U CN 204193648U
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- solvent
- knockout drum
- blending tank
- miscella
- retracting device
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Abstract
The utility model provides the retracting device of solvent in a kind of inoranic membrane and miscella, comprise the fine filter (10) connected by pipeline successively, blending tank (20), solvent pump (30), knockout drum (40) and holding vessel (50), membrane module in knockout drum (40) adopts above-mentioned inoranic membrane, recovery method is included in fine filter (10) and injects miscella and filter, miscella injection blending tank (20) after filtering is kept in, miscella in blending tank (20) is pumped into knockout drum (40) through solvent pump (30) and carries out UF membrane, solvent after UF membrane is injected holding vessel (50) deposit.The utility model can significantly improve solvent recovering rate, and saves energy consumption.
Description
Technical field
The utility model relates to solvent recovery technical field in miscella, especially the retracting device of solvent in a kind of inoranic membrane and miscella.
Background technology
In traditional oil extraction technology, solvent recovery is by twice long tube evaporation, again by steam distillation to carry out recycling design except the method for the middle residual solvent that deoils, because quantity of solvent is very large and have phase transition process, need to consume a large amount of energy, this is one of main power consumption operation of oil extraction and refining.Reclaim solvent in miscella by membrane separation technique and can save mass energy.Membrane separation technique a kind of uses pellicle separation method, be at normal temperatures with film pressure at both sides difference or potential difference for power, solute is separated with solvent, concentrates, purifying.Membrane separation technique mainly adopts natural or Prof. Du Yucang macromolecule membrane, with outside energy or chemical potential difference for motive force, bi-component or multicomponent liquid are separated with solvent, classification, purification and enrichment procedure.The membrane process now applied has counter-infiltration, nanofiltration, hyperfiltration, micro porous filtration, dialysis electrodialysis, gas separaion, pervaporation, Co ntrolled release, liquid film, Membrane Materials membrane reactor etc., and that wherein commonly uses in the food industry has micro-filtration, ultrafiltration and counter-infiltration three kinds.At present, less about adopting the research of membrane separation technique recycling design from miscella report both at home and abroad, from the work carried out, mostly adopt business-like organic film, the kind of film mainly contains ultrafiltration, nanofiltration and counter-infiltration etc.From separating effect, the separating property (flux and rejection) of film is comparatively limited.This is mainly because the n-hexane in miscella has very strong hydrophobicity, and the organic film adopted in above-mentioned research is mostly hydrophilic film, is therefore unsuitable for the separation of miscella system.In addition, research finds, n-hexane equal solvent is very strong to the swelling destructiveness of most of organic film, which has limited the development that embrane method reclaims organic solvent.
Utility model content
The purpose of this utility model is to provide the retracting device of solvent in a kind of miscella, adopts above-mentioned retracting device, can significantly improve solvent recovering rate, and saves energy consumption.
To achieve these goals, the technical solution adopted in the utility model is as follows:
The retracting device of solvent in a kind of miscella, comprise the fine filter, blending tank, solvent pump, knockout drum and the holding vessel that are connected by pipeline successively, the liquid outlet of described fine filter is connected to the inlet at blending tank top, liquid outlet bottom described blending tank is connected to the inlet bottom described knockout drum via solvent pump, the liquid outlet of described knockout drum side is connected to the inlet of described holding vessel side, it is characterized in that, the membrane module of described knockout drum comprises inoranic membrane.
According to above scheme, also comprise vavuum pump, described fine filter, blending tank, knockout drum and holding vessel are connected to the entrance of vavuum pump respectively by pipeline.
According to above scheme, the top of described knockout drum is also provided with loop exit, and the side of described blending tank is provided with loop head, and described loop exit is connected to described loop head by pipeline.
According to above scheme, be provided with valve between described loop head and loop exit to regulate the transmembrane pressure in described knockout drum.
According to above scheme, be connected by pipeline between the liquid outlet of described knockout drum and the liquid outlet of solvent pump, and pass through the connected state of the liquid outlet of Valve controlling knockout drum and the liquid outlet of solvent pump.
According to above scheme, described blending tank is provided with the water-bath chuck of adjustable described blending tank internal temperature.
According to above scheme, described blending tank top is connected with surge tank, compressor and condenser in turn by pipeline, and the outlet of described condenser is connected to described holding vessel.
According to above scheme, described vacuum delivery side of pump is connected to the entrance of described surge tank by pipeline, and whether described vacuum delivery side of pump is provided with valve be connected with surge tank to control vavuum pump.
The beneficial effects of the utility model are: the utility model structure is simple, and arrange rationally, workable, it adopts inorganic ceramic membrane, and make solvent easier in inoranic membrane, membrane flux is highly improved, and can significantly improve solvent recovering rate.
Accompanying drawing explanation
Fig. 1 is structural representation of the present utility model.
In figure: 10, fine filter; 20, blending tank; 30, solvent pump; 40, knockout drum; 50, holding vessel; 60, vavuum pump; 70, surge tank; 80, compressor; 90, condenser; 41, loop exit; 21 loop heads.
Detailed description of the invention
Below in conjunction with accompanying drawing and embodiment, the technical solution of the utility model is described.
The utility model provides a kind of inoranic membrane, is applied to the recovery of solvent in miscella, and the material of described inoranic membrane is for being selected from Al
2o
3, TiO
2, SiO
2or ZrO
2in any one or any two or more compounds, a kind of inorganic ceramic membrane can be formed, when being applied to the organic solvent recovery process of miscella system, can avoid the organic matter that exists in miscella particularly the material such as n-hexane to the conventional destructiveness of film, embrane method can be made to reclaim and to be more widely used in solvent recovery process, embody the superiority of membrane separation technique completely, improve solvent recovery efficiency, save energy consumption.
Preferably, according to above scheme, the surface of described inoranic membrane, through hydrophobic treatment, makes inoranic membrane promote its separating power further.
Further, the molecular cut off of described inoranic membrane is 1kDa ~ 10kDa, goes for the recovery of most of organic solvent, improves of the present utility modelly to be widely used degree.
As shown in Figure 1, the utility model also provides the retracting device of solvent and the recovery method of correspondence in a kind of miscella, is further elaborated the utility model below in conjunction with apparatus and method.
Retracting device of the present utility model comprises the fine filter 10, blending tank 20, solvent pump 30, knockout drum 40 and the holding vessel 50 that are connected by pipeline successively, the liquid outlet of described fine filter 10 is connected to the inlet at blending tank 20 top, liquid outlet bottom described blending tank 20 is connected to the inlet bottom described knockout drum 40 via solvent pump 30, the liquid outlet of described knockout drum 40 side is connected to the inlet of described holding vessel 50 side, the membrane module of described knockout drum 40 comprises inoranic membrane, and the material of this inoranic membrane is above-mentionedly selected from Al
2o
3, TiO
2, SiO
2or ZrO
2in any one or any two or more compounds.Recovery method of the present utility model comprises the following steps: S1, inject miscella and filter in fine filter 10; S2, by filter after miscella inject blending tank 20 keep in; S3, the miscella in blending tank 20 is pumped into knockout drum 40 through solvent pump 30 carry out UF membrane; S4, by after UF membrane solvent inject holding vessel 50 deposit.
When carrying out solvent recovery, through valve V1, miscella is injected fine filter 10 from inlet, after excessively filtering fine particle impurity by fine filter 10, flow in blending tank 20 through pipeline, when stopping after the upper limit that liquid level in blending tank 20 reaches carrying miscella to blending tank 20, open the valve V3 between blending tank 20 and solvent pump 30 and solvent pump 30, miscella in blending tank 20 is conveyed into knockout drum 40 from the inlet of knockout drum 40 and carries out UF membrane, in membrane separating process, solvent in miscella can through film, flow out from the liquid outlet of knockout drum 40, through the valve V8 between knockout drum 40 and holding vessel 50, inject holding vessel 50 from the inlet of holding vessel 50 to preserve.
When carrying out UF membrane solvent recovery by retracting device of the present utility model, owing to adopting inorganic ceramic membrane heat-resisting quantity and good corrosion resistance, mechanical strength is large, clean conditions is good, not easily block, long service life, which reduce maintenance and change, thus saved time and expense, make solvent easier in inoranic membrane simultaneously, membrane flux is highly improved, solvent recovering rate can be significantly improved, in addition the utility model is when reclaiming solvent in miscella, membrane module is adopted to concentrate mixed oil liquid, thus reclaim most of solvent without phase transformation, greatly reduce energy consumption, improve solvent recovery efficiency.
According to above scheme, also comprise vavuum pump 60, described fine filter 10, blending tank 20, knockout drum 40 and holding vessel 50 are connected to the entrance of vavuum pump 60 respectively by pipeline, before carrying out step S1, the absolute pressure in fine filter 10, blending tank 20, knockout drum 40 and holding vessel 50 are down to below 0.01MPa.Particularly before recovery is carried out, first start vavuum pump 60 and the air of pipeline each in retracting device and tank body is extracted out, make pipeline and tank body form negative pressure, the flowing velocity of miscella can be accelerated, effectively improve separative efficiency.
In membrane separating process, solvent in miscella can finally enter holding vessel 50 through film, but also there is part not need to reclaim through still comprising solvent in the miscella of film, therefore according to above scheme, the top of described knockout drum 40 is also provided with loop exit 41, the side of described blending tank 20 is provided with loop head 21, described loop exit 41 is connected to described loop head 21 by pipeline, namely while described step S4 carries out, other product after UF membrane is injected blending tank 20 by the loop exit 41 of knockout drum 40 via the loop head 21 of blending tank 20 and carries out multi-cycle separation.Do not flow out from the loop exit 41 of knockout drum 40 through the miscella of film particularly, through the valve V7 between blending tank 20 and knockout drum 40, be back to blending tank 20 from the loop head 21 of blending tank 20 and carry out multi-cycle separation, to improve the rate of recovery of solvent in miscella.
When carrying out circulation and stress, smooth and easy in order to ensure the flowing of miscella, according to above scheme, valve is provided with to regulate the transmembrane pressure in described knockout drum 40 between described loop head 21 and loop exit 41, the i.e. inlet fluid pressure of knockout drum 40 and the difference of liquid outlet fluid pressure, when carrying out described multi-cycle separation, need to regulate the pressure reduction between the inlet of described knockout drum 40 and liquid outlet to be 0.1 ~ 1.5MPa, this control valve directly can adopt above-mentioned valve V7, the folding degree of control valve V7, transmembrane pressure in knockout drum 40 can be adjusted to suitable scope.
After repeatedly reclaiming, when the flux of the membrane module in knockout drum 40 drops to 35% ~ 50% of original flux, need to rush Xian's operation to membrane module, therefore according to above scheme, the liquid outlet of described knockout drum 40 is connected by pipeline with between the liquid outlet of solvent pump 30, and pass through the connected state of the liquid outlet of Valve controlling knockout drum 40 and the liquid outlet of solvent pump 30, particularly, pure solvent can be loaded in blending tank 20, close the valve V5 between solvent pump 30 and knockout drum 40, and the valve V8 between knockout drum 40 and holding vessel 50, open the valve V6 of the connected state controlling the liquid outlet of knockout drum 40 and the liquid outlet of solvent pump 30 simultaneously, backwash operation can be carried out to the membrane module in knockout drum 40 after opening solvent pump 303, until the flux recovery of film group is original more than 80%.
Certain influence is had to separation process in the temperature of miscella, therefore according to above scheme, described blending tank 20 is provided with the water-bath chuck of adjustable described blending tank 20 internal temperature, after miscella enters blending tank 20, namely while described step S2 carries out, can be heated up to the miscella in blending tank 20 by water-bath chuck, can by temperature increase to 15 ~ 70 DEG C, to promote the separative efficiency of miscella.
Along with constantly carrying out of membrane separating process, miscella concentration in blending tank 20 ratio of solvent volume (oil quality with) can become large gradually, until after miscella concentration reaches 50% ~ 80%, can not effective recycling design by UF membrane, now need stopper film to be separated, adopt the mode of reduction vaporization precipitation to reclaim.Therefore, according to above scheme, described blending tank 20 top is connected with surge tank 70, compressor 80 and condenser 90 in turn by pipeline, the outlet of described condenser 90 is connected to described holding vessel 50, namely, after described step S4 completes, also comprise the steps: S01, heating up to blending tank 20 makes the solvent in miscella evaporate; S02, the solvent flashing to gas is sucked in surge tank 70 temporary; S03, the gas-solvent in surge tank 70 to be cooled by injecting condenser 90 after compressor 80 supercharging; S04, by be cooled to liquid solvent inject holding vessel 50 preserve.Particularly, the process of reduction vaporization precipitation is, by water-bath chuck, the temperature of blending tank 20 is adjusted to 30 ~ 85 DEG C, open compressor 80 simultaneously, solvent in blending tank 20 is reduced pressure and evaporates, solvent in blending tank 20 is evaporated to gas vapor, solvent vapo(u)r is successively through the valve V2 between blending tank 20 top and surge tank 70, interface D and valve V15 enters surge tank 70, and then enter compress in compressor 80 after enter in condenser 90 cool, the solvent being cooled to liquid flows in holding vessel 50 through the valve V17 between the outlet and holding vessel 50 of condenser 90 and stores.
Along with in blending tank 20, the solvent of miscella constantly evaporates, gas pressure in blending tank 20 constantly declines, reduced pressure by compressor 80 and do not have larger effect, therefore according to above scheme, the outlet of described vavuum pump 60 is connected to the entrance of described surge tank 70 by pipeline, and whether the outlet of described vavuum pump 60 is provided with valve is connected with surge tank 70 to control vavuum pump 60, namely also comprise step S05, between blending tank 20 and surge tank 70, access vavuum pump 60, to extract the gas-solvent in blending tank 20.Particularly, when the air pressure of blending tank 20 is until when reducing to 0.08 ~ 0.16MPa, shutoff valve V15 makes blending tank 20 and surge tank 70 isolate, open valve V12, V13 and vavuum pump 606, vavuum pump 606 is made to access between blending tank 20 and surge tank 70, straight empty pump can link with compressor 80, to reduce the gas pressure in blending tank 20 further, until absolute pressure is less than 0.01MPa, after reduction vaporization precipitation terminates, grease in blending tank 20 can be released through interface C and be carried out subsequent treatment by open valve V4, simultaneously purer in holding vessel 50 solvent, by open valve V10, oil extraction is reused for after interface B releases.
Claims (8)
1. the retracting device of solvent in a miscella, it is characterized in that, comprise the fine filter (10) connected by pipeline successively, blending tank (20), solvent pump (30), knockout drum (40) and holding vessel (50), the liquid outlet of described fine filter (10) is connected to the inlet at blending tank (20) top, the liquid outlet of described blending tank (20) bottom is connected to the inlet of described knockout drum (40) bottom via solvent pump (30), the liquid outlet of described knockout drum (40) side is connected to the inlet of described holding vessel (50) side, inoranic membrane is provided with in the membrane module of described knockout drum (40).
2. the retracting device of solvent in miscella according to claim 1, it is characterized in that, also comprise vavuum pump (60), described fine filter (10), blending tank (20), knockout drum (40) and holding vessel (50) are connected to the entrance of vavuum pump (60) respectively by pipeline.
3. the retracting device of solvent in miscella according to claim 2, it is characterized in that, the top of described knockout drum (40) is also provided with loop exit (41), the side of described blending tank (20) is provided with loop head (21), and described loop exit (41) is connected to described loop head (21) by pipeline.
4. the retracting device of solvent in miscella according to claim 3, it is characterized in that, be provided with valve between described loop head (21) and loop exit (41) to regulate the transmembrane pressure in described knockout drum (40).
5. the retracting device of solvent in miscella according to claim 3, it is characterized in that, the liquid outlet of described knockout drum (40) is connected by pipeline with between the liquid outlet of solvent pump (30), and passes through the connected state of the liquid outlet of Valve controlling knockout drum (40) and the liquid outlet of solvent pump (30).
6. the retracting device of solvent in miscella according to claim 3, is characterized in that, described blending tank (20) is provided with the water-bath chuck of adjustable described blending tank (20) internal temperature.
7. the retracting device of solvent in miscella according to claim 2, it is characterized in that, described blending tank (20) top is connected with surge tank (70), compressor (80) and condenser (90) in turn by pipeline, and the outlet of described condenser (90) is connected to described holding vessel (50).
8. the retracting device of solvent in miscella according to claim 7, it is characterized in that, the outlet of described vavuum pump (60) is connected to the entrance of described surge tank (70) by pipeline, and whether the outlet of described vavuum pump (60) is provided with valve be connected with surge tank (70) to control vavuum pump (60).
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201420587525.5U CN204193648U (en) | 2014-10-11 | 2014-10-11 | The retracting device of solvent in a kind of miscella |
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|---|---|---|---|
| CN201420587525.5U CN204193648U (en) | 2014-10-11 | 2014-10-11 | The retracting device of solvent in a kind of miscella |
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| CN204193648U true CN204193648U (en) | 2015-03-11 |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105950279A (en) * | 2016-06-12 | 2016-09-21 | 中国农业科学院油料作物研究所 | Method and system for extracting grease from oil |
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2014
- 2014-10-11 CN CN201420587525.5U patent/CN204193648U/en active Active
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105950279A (en) * | 2016-06-12 | 2016-09-21 | 中国农业科学院油料作物研究所 | Method and system for extracting grease from oil |
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