CN105176826A - Method for harvesting microalgae through alkalescence flocculation-foam separation and separation device - Google Patents
Method for harvesting microalgae through alkalescence flocculation-foam separation and separation device Download PDFInfo
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- CN105176826A CN105176826A CN201510683998.4A CN201510683998A CN105176826A CN 105176826 A CN105176826 A CN 105176826A CN 201510683998 A CN201510683998 A CN 201510683998A CN 105176826 A CN105176826 A CN 105176826A
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Abstract
The invention discloses a method for harvesting microalgae through alkalescence flocculation-foam separation and a separation device. The method comprises the following steps: 1) adjusting the pH value of an algae liquid; 2) performing flocculating settling on the algae liquid in a settling pond after pH adjustment, thereby obtaining a flocculated algae liquid and supernate; and 3) introducing air into a foam separation tower which is filled with the flocculated algae liquid, a surfactant and a separation additive so as to enrich microalgae to foams, and collecting the foams, thereby obtaining the microalgae. The separation device comprises the settling pond and a circulation foam tower, wherein the flocculated algae liquid outlet in the settling pond is connected with an algae liquid inlet of the circulation foam tower through a middle storage tank. The circulation foam tower consists of a foam section and a rising section, and a circulation section is divided into a rising area and a settling area by using a guide cylinder, so that gas-liquid-solid contact mass transfer can be improved, and the separation efficiency can be improved. The method is high in recycling rate and concentration ratio, can operate continuously, is short in separation time and is applicable to large-scale industrial production, high in production capacity and relatively low in cost, and meanwhile circulation of water can be achieved.
Description
Technical field
The invention belongs to the separation harvesting technique field of micro-algae, be specifically related to a kind of method and tripping device of weakly alkaline flocculation-foam separation microalgae.
Background technology
Microalgae recovery is considered to micro-algae and produces one of factor the most difficult in biofuel process.Usually, in micro algae culturing liquid, algae dry weight only has 0.02-0.5kg/m
3, generally need to be concentrated to 20-70kg/m
3above, next step technique can then just be entered.At present, the separation harvesting technique of micro-algae mainly comprises centrifugation, flocculation separation, air supporting/Paulownia clones and membrane sepn etc.Although centrifugation and membrane sepn can obtain higher cycles of concentration and the rate of recovery, its cost is high, and production capacity is little, is suitable only for and gathers as being separated of the micro-algae of food and medicine material.For oil-producing microalgae, the most extensively to adopt at present and the technology studied mainly is flocculated and air supporting/Paulownia clones.How while acquisition high-recovery and cycles of concentration, realize low cost, the separation of high production capacity gather, be this kind of oil-producing microalgae be separated harvesting technique must in the face of and the problem that solves.
For flocculation process, inorganic flocculating agent is the most frequently used, as Chinese invention patent CN102382769 discloses a kind of technology adopting the recycling of iron trichloride flocculation microalgae and cultivation water body, iron trichloride is concentration 5-150ppm in the solution, settling time 2 ~ 36h is 76% to the rate of recovery of chlorella.Prior art is in order to obtain the high rate of recovery, often need also to add efficient polymer flocculation auxiliary agent, a kind of chitosan-Lewis acid is adopted to be flocculation agent as Chinese invention patent CN102051332 openly knows clearly, the method of the settlement separate micro-algae of flocculating settling after stirring, wherein chitosan concentration 2-30mg/L in algae liquid, Lewis acid concentrations 3-9mg/L, the rate of recovery is up to 99%; This method rate of recovery is high, but the cost of flocculation agent is higher equally, and adding of flocculation agent also brings difficulty to the subsequent disposal of the recycling of clear liquid, concentrated solution after being separated.
Physics flocculation is if electricity flocculation is without flocculation agent consumption.Chinese patent CN102787070 discloses and a kind ofly adopts sun power salt bridge electricity flocculation plant to carry out micro-algae to flocculate the method for gathering, and after electrolysis 6h, the rate of recovery is greater than 95%, and cycles of concentration is greater than 15 times.This method compares traditional electric flocculence, and with the consumption reducing the energy and electrode, but its technology and equipment is complicated, and cost is high, and production capacity is low, and unsuitable industry is amplified.
The method of the raw Chlorococcum in sea regulating the rear filtering separation of pH sedimentation flocculation is all have employed in Chinese invention patent CN102839127, CN103013833, wherein the adjustment pH of CN102839127 report is more than 11, sedimentation more than 3 days, the rate of recovery can reach 99%, but unexposed cycles of concentration; Its sedimentation time is long, and algae micro-in sedimentation liquid is taked to the method for filtering separation, production capacity is low and power cost is high, and is not suitable for the separation of extensive oil-producing microalgae, and adopts NaOH to regulate pH to cause Na in system
+accumulation.
For the method for dissolved air flotation, Chinese invention patent CN1472306 discloses a kind of method adopting the continuous microalgae of dissolved air type air-float, but the unexposed rate of recovery and cycles of concentration.Chinese patent CN101549231 then discloses that a kind of carry the method for micro-algae with sharp separation bubble, rotary filter press needs liquid to enter wet cyclone with high flow velocities by dissolved air floatation and rotary filter press coupling, and the high and unsuitable equally industry of energy consumption is amplified.
Foam separation, or claim pneumatic flotation, by adding specific tensio-active agent in air supporting system, forming stable foam layer, realizing being separated by material to be separated being adsorbed in foam layer, existing successfully application in albumen sepn etc.The core of pneumatic flotation is preferred surfactant system and tripping device, to obtain stable foam layer, and makes separate substance to foam layer fast enriching.Chinese patent CN102127509 discloses a kind of method and apparatus adopting the micro-algae of tensio-active agent pneumatic flotation, and its device essence is a bubble tower.In embodiment, adopt this method to be separated and intend ball algae, tensio-active agent adopts CTAB or TBP, and under best-case, the rate of recovery can more than 98%, and concentration ratio is not reported.This method needs to distribute the bubbles into about 1mm, have employed the tensio-active agent that cost is higher, because adopt periodical operation until redgreen in foam, its high-recovery is to extend disengaging time for cost.Chinese patent CN102127509 also discloses a kind of method adopting Foam concentration microalgae, and the flotation unit adopted also is bubble tower, and inside adds special foam inner member.In an embodiment of this patent, adopt this device to gather micro-algae of certain self-produced foam, concentration ratio reaches 20 times, but the rate of recovery and collecting time etc. are not all reported for work, and owing to lacking necessary technical characteristic, cannot judge efficiency.And aforesaid method, all directly carry out pneumatic flotation from rare algae liquid, required foam additive consumption is large, and equipment volume is large, and disengaging time is long, and its economy is still not good; The operational path adopting interval to be separated is unsuitable for industrialization stably manufactured.
In sum, although prior art provides the technological method that multiple micro-algae is separated, there is high-recovery and cycles of concentration, simultaneously low cost, high production capacity, be suitable for extensive oil-producing microalgae and be separated the industrialization technology of gathering and still need further to be developed.
Summary of the invention
The object of this invention is to provide one and there is high-recovery and cycles of concentration, simultaneously the method for the microalgae recovery of low cost and high production capacity and corresponding tripping device.
The method of microalgae recovery provided by the present invention, comprises the steps:
1) pH regulator is carried out to algae liquid, the algae liquid after adjusted pH;
2) by step 1) in adjustment pH after algae liquid in settling bowl, carry out flocculating settling, obtain flocculation algae liquid and supernatant liquor;
3) to step 2 is housed) in flocculation algae liquid, tensio-active agent and sepa-ration aid foam separating tower in pass into air, make micro-algae be enriched in foam, collect foam, namely gather and obtain micro-algae.
In aforesaid method, step 1) in, described pH regulator carries out by the following method: in described algae liquid, add pH adjusting agent, regulates pH to 10 ~ 10.5 of described algae liquid, and wherein, described pH adjusting agent specifically can be the NaOH aqueous solution, the KOH aqueous solution or NH
3the aqueous solution, is preferably NH
3the aqueous solution.Further, the concentration of pH adjusting agent can be selected according to practical condition.
Micro-algae in described algae liquid specifically can be ball algae or intends ball algae, and described ball algae specifically can be sea growing chlorella (MarineChlorella) or Porphyridium cruentum (Porphyridiumcruentum); Described plan ball algae specifically can be micro-plan ball algae (Nannochloropsissp.).
In aforesaid method, step 2) and step 3) be selected from following a) operate continuously or b) gap operating,
When step 2) and step 3) when being selected from a) operate continuously: (algae liquid flows into subsider with certain flow, bottom subsider, flow out flocculation algae liquid continuously and import Circulation foam tower, in Circulation foam tower, stream adds tensio-active agent and sepa-ration aid, and in foam chute, continuous extraction foam is to collect dense algae liquid)
Step 2) in, the hydraulic detention time of described flocculating settling is 0.5 ~ 2h.
Step 3) in, described tensio-active agent is selected from sodium laurylsulfonate (Sodiumdodecylsulfate, and the mixture of substance A SDS), wherein, the mass ratio of SDS and substance A is 1:0.5 ~ 2, and substance A is selected from Tween20 and/or Tween80, when substance A is Tween20 and Tween80, both can add according to arbitrary proportion, and those skilled in the art carry out preparing according to practical situation.
Described sepa-ration aid specifically can be FeCl
3.
The ratio of described flocculation algae liquid, tensio-active agent and sepa-ration aid is as follows: 1m
3add sepa-ration aid described in tensio-active agent described in 20 ~ 250g and 30 ~ 120g in described flocculation algae liquid, be preferably 1m
330 ~ 120gSDS, 20 ~ 60gTween20 and 40 ~ 80gFeCl is added in described flocculation algae liquid
3, according to aforementioned proportion according to the flow of flocculation algae liquid at the uniform velocity stream add tensio-active agent and sepa-ration aid.
The hydraulic detention time of described flocculation algae liquid in described foam separating tower is 0.3 ~ 2h.
In described foam separating tower, the pH of system is 10 ~ 11, and empty tower gas velocity is 0.06 ~ 0.3cm/s.
When step 2) and step 3) when being selected from b) periodical operation: (a collection of cultivation algae liquid adds subsider, and after sedimentation certain hour, extraction flocculation algae liquid bottom subsider, stored in relay tank.Then a collection of flocculation algae liquid is added Circulation foam tower, disposablely in Circulation foam tower to add or at the uniform velocity stream adds tensio-active agent and sepa-ration aid, in foam chute, continuous extraction foam is to collect dense algae liquid)
Described tensio-active agent and sepa-ration aid is disposable when joining foam separating tower:
Step 2) in, the settling time of described flocculating settling is 0.5 ~ 4h.
Step 3) in, described tensio-active agent is selected from the mixture of SDS and substance A, wherein, the mass ratio of SDS and substance A is 1:0.5 ~ 2, substance A is selected from Tween20 and/or Tween80, when substance A is Tween20 and Tween80, both can add according to arbitrary proportion, and those skilled in the art carry out preparing according to practical situation.
Described sepa-ration aid specifically can be FeCl
3.
The ratio of described flocculation algae liquid, tensio-active agent and sepa-ration aid is as follows: 1m
3add sepa-ration aid described in tensio-active agent described in 60 ~ 240g and 60 ~ 120g in described flocculation algae liquid, be preferably 1m
340 ~ 160gSDS, 30 ~ 90gTween20 and 60 ~ 90gFeCl is added in described flocculation algae liquid
3, according to aforementioned proportion according to the flow of flocculation algae liquid at the uniform velocity stream add tensio-active agent and sepa-ration aid.
The described flocculation algae foam separation time of liquid in described foam separating tower is 0.5 ~ 4h.
Described tensio-active agent and sepa-ration aid are when at the uniform velocity stream is added to foam separating tower:
Step 2) in, the settling time of described flocculating settling is 0.5 ~ 4h.
Step 3) in, described tensio-active agent is selected from the mixture of SDS and substance A, wherein, the mass ratio of SDS and substance A is 1:0.5 ~ 2, substance A is selected from Tween20 and/or Tween80, when substance A is Tween20 and Tween80, both can add according to arbitrary proportion, and those skilled in the art carry out preparing according to practical situation.
Described sepa-ration aid specifically can be FeCl
3.
The ratio of described flocculation algae liquid, tensio-active agent and sepa-ration aid is as follows: 1m
3add sepa-ration aid described in tensio-active agent described in 20 ~ 250g and 30 ~ 120g in described flocculation algae liquid, be preferably 1m
330 ~ 120gSDS, 20 ~ 60gTween20 and 40 ~ 80gFeCl is added in described flocculation algae liquid
3, according to aforementioned proportion according to the flow of flocculation algae liquid at the uniform velocity stream add tensio-active agent and sepa-ration aid.
The described flocculation algae foam separation time of liquid in described foam separating tower is 0.5 ~ 2h.
In aforesaid method, step 3) in, in described foam separating tower, the pH of system is 10 ~ 11, and empty tower gas velocity is 0.06 ~ 0.3cm/s.
In aforesaid method, step 2) in, also comprise passing in described supernatant liquor and be rich in CO
2air, make the pH of described supernatant liquor return to 8.0 ~ 8.5, then returned culture systems and recycle, wherein, described in be rich in CO
2air in CO
2volume fraction be 0.5%-12%.
In aforesaid method, step 3) in, also comprise and import in Debubbling tank by the clear liquid in described foam separating tower, carry out deaeration, obtain deaeration liquid and foam, then deaeration liquid is imported settling bowl, foam imports to the foam enrichment section in described Circulation foam tower.
A kind of concrete tripping device realizing the method for above-mentioned microalgae recovery provided by the present invention, comprise settling bowl and Circulation foam tower, wherein, the flocculation algae liquid outlet in described settling bowl is connected with the algae liquid entrance in described Circulation foam tower by described relay tank.
In said apparatus, described settling bowl is vertical-flow settling bowl, is exported and the export mixes of flocculation algae liquid, wherein by feed liquid port conduit, subsider, overflow, the upper end of described feed liquid port conduit is naked leaks outside the top of described subsider, and remainder is positioned at the inside of described subsider; Described overflow outlet is positioned at middle and upper part or the top of described subsider; The outlet of described flocculation algae liquid is positioned at the bottom of described subsider.
In said apparatus, the aspect ratio of described subsider is 3 ~ 5, and ensures that the apparent settlement speed of algae liquid in settling bath is not higher than 0.05cm/s; Feed liquid port conduit diameter should ensure algae liquid wherein flow velocity be no more than 5cm/s.
In said apparatus, described Circulation foam tower is made up of circulation section (liquid layer) and foam enrichment section (foam layer), and wherein, described circulation section is made up of tower body, guide shell and gas distributor, described foam enrichment section is by foam chute, and foam overflow weir and foam outlet are formed.
Described guide shell is positioned at the inside of described tower body, forms annular space with the inner tower wall of described tower body, and by guide shell, circulation section is divided into rising area and decline district, rising area is positioned at the inside of described guide shell, and decline district is positioned at annular space.
Described gas distributor is positioned at bottom or the bottom of the inner bottom part of described tower body and the inside of described guide shell.
The middle and lower part of described tower body or bottom have algae liquid entrance, and described algae liquid entrance is positioned at the bottom of described guide shell and the top of gas distributor.
The middle and lower part of described tower body or bottom have auxiliary agent entrance, the bottom of the annular space that the inner tower wall that described auxiliary agent entrance is positioned at described guide shell and described tower body is formed.
The middle and upper part of described tower body has purified liquor outlet, the middle and upper part of the annular space that the inner tower wall that described purified liquor outlet is positioned at described guide shell and described tower body is formed.
In said apparatus, the aspect ratio of the circulation section in described Circulation foam tower is (5 ~ 9): 1.
The aspect ratio of the circulation section in described foam chute and described Circulation foam tower is (1 ~ 2): 3, and diameter is than being (1 ~ 2.8): 1.
The ratio of the foam height of weir plate in described Circulation foam tower and described foam chute height is (1 ~ 2): 3.
Quiet liquid level in described foam separating tower is higher than described guide shell upper end 10 ~ 50cm.
Described foam overflow weir specifically can be identical with the diameter of described tower body.The diameter of circulation section draft tube diameter and tower body designs routinely.
In said apparatus, also comprise following auxiliary facility: flocculation pH regulator pond, neutralization tank, relay tank, foam holding tank and Debubbling tank,
Wherein, described flocculation pH regulator pond is connected with the feed liquid port conduit in described settling bowl; Described neutralization tank is connected with the overflow outlet in described settling bowl; Described foam holding tank is connected with the foam outlet in described Circulation foam tower; The entrance of described Debubbling tank is connected with the purified liquor outlet in described Circulation foam tower, and the outlet of described Debubbling tank is connected with the foam enrichment section in described Circulation foam tower with the feed liquid port conduit in described settling bowl respectively.
Present invention employs method concentrated step by step, with the low-down weakly alkaline flocculation of cost for initial concentration, carry out fluid circling bubbling separation waste water treatment on this basis, because the concentrated of the 1st step also can reach about 10 times, therefore the volume of circling and bubbling separation column, energy consumption and auxiliary agent consumption can significantly reduce, and have given full play to the advantage of pneumatic flotation; The present invention adopt with NH
3water regulates the method for pH flocculating settling, without the need to a large amount of inorganic flocculating agent, not only reduces costs, further reduces the accumulation of system mineral ion, really achieve the circulation of clear liquid; The circling and bubbling separation column that the present invention adopts, compare with the foam floating flotating device of tradition based on bubble tower, gas-liquid-solid contact mass transfer obtains strengthening, and the efficiency of separation is improved.Due to the advantage of these techniques and device, make technology of the present invention, and prior art contrast, there is following technical superiority:
1) rate of recovery and concentration ratio high.The total rate of recovery of two steps is greater than 95%, and concentration ratio is more than 150 times.
2) can carry out operate continuously, disengaging time is short, and be applicable to large industrial production, production capacity is high.During operate continuously, the total disengaging time of two steps is less than 4h, is no more than 2h in most cases, can reaches above-mentioned separating effect.
3) achieve the recycle of water, the clear liquid of separation is by passing into CO
2regulate pH can return culture systems to recycle.
4) cost of sepn process is lower.The equipment energy consumption of sepn process is little, and auxiliary agent is cheap, and consumption is little.
Accompanying drawing explanation
Fig. 1 is continuous process and the device of weakly alkaline flocculation-foam separation microalgae recovery in the present invention.
Fig. 2 is operation and the flow schematic diagram of Circulation foam tower in the present invention.
Embodiment
Below by specific embodiment, the present invention will be described, but the present invention is not limited thereto.
Experimental technique described in following embodiment, if no special instructions, is ordinary method; Described reagent and material, if no special instructions, all can obtain from commercial channels.
Following embodiment specifically realizes by the tripping device of following weakly alkaline flocculation-foam separation microalgae.
Can learn from Fig. 1: this tripping device, comprise flocculation pH regulator pond I, settling bowl II, neutralization tank III, relay tank IV, Circulation foam tower V, foam holding tank VI and Debubbling tank VII, wherein, described flocculation pH regulator pond I is connected with the feed liquid port conduit 1 in described settling bowl II; Described neutralization tank III is connected with the overflow outlet 3 in described settling bowl II; Described relay tank IV exports 4 with the flocculation algae liquid in described settling bowl II respectively and is connected with the algae liquid entrance 8 in described Circulation foam tower V; Described foam holding tank VI is connected with the foam outlet 13 in described Circulation foam tower V; Described Debubbling tank VII is connected with the foam enrichment section in described Circulation foam tower V with the purified liquor outlet 10 in described Circulation foam tower V, the feed liquid port conduit 1 in described settling bowl II respectively.
Described settling bowl II is vertical-flow settling bowl, export 4 by feed liquid port conduit 1, subsider 2, overflow outlet 3 and flocculation algae liquid to form, wherein, the upper end of described feed liquid port conduit 1 is naked leaks outside the top of described subsider 2, and remainder is positioned at the inside of described subsider 2; Described overflow outlet 3 is positioned at middle and upper part or the top of described subsider 2; Described flocculation algae liquid outlet 4 is positioned at the bottom of described subsider 2.
Described Circulation foam tower V is made up of circulation section (liquid layer) and foam enrichment section (foam layer), wherein, described circulation section is made up of tower body 5, guide shell 6 and gas distributor 7, and described foam enrichment section is by foam chute 11, and foam overflow weir 12 and foam outlet 13 are formed.
Described guide shell 6 is positioned at the inside of described tower body 5, forms annular space with the inner tower wall of described tower body 5, by guide shell, circulation section is divided into rising area and decline district, and rising area is positioned at the inside of described guide shell 6, and decline district is positioned at annular space.
Described gas distributor 7 is positioned at bottom or the bottom of the inner bottom part of described tower body 5 and the inside of described guide shell 6.
The middle and lower part of described tower body 5 or bottom have algae liquid entrance 8, and described algae liquid entrance 8 is positioned at the bottom of described guide shell 6 and the top of gas distributor 7.
Middle and lower part or the bottom of described tower body 5 have auxiliary agent entrance 9, and described auxiliary agent entrance 9 is positioned at the bottom of the annular space that described guide shell 6 is formed with the inner tower wall of described tower body 5.
The middle and upper part of described tower body 5 has purified liquor outlet 10, and described purified liquor outlet 10 is positioned at the middle and upper part of the annular space that described guide shell 6 is formed with the inner tower wall of described tower body 5.
In order to realize the effect in following embodiment, the aspect ratio of described subsider 2 is 3 ~ 5, and ensures that the apparent settlement speed of algae liquid in settling bath is not higher than 0.05cm/s; Feed liquid port conduit 1 diameter should ensure algae liquid wherein flow velocity be no more than 5cm/s.
The aspect ratio of the circulation section in described Circulation foam tower V is (5 ~ 9): 1.
The aspect ratio of the circulation section in described foam chute and described Circulation foam tower V is (1 ~ 2): 3, and diameter is than being (1 ~ 2.8): 1.
The ratio of the foam height of weir plate in described Circulation foam tower and described foam chute height is (1 ~ 2): 3.
Described foam overflow weir 12 is identical with the diameter of described tower body 5.The diameter of circulation section draft tube diameter and tower body designs routinely.
Embodiment 1, the continuous microalgae of weakly alkaline flocculation-foam separation:
1) sea growing chlorella (MarineChlorella), diameter is 3 ~ 8 μm, (f/2 is adopted to improve sea water medium in sea growing chlorella nutrient solution, the pH value of nutrient solution is 8.4, be called for short algae culturing liquid) in cultivate, at the end of cultivation, in sea growing chlorella nutrient solution, frustule concentration is 4.5 × 10
7individual/mL;
2) adopt the operating method of operate continuously, above-mentioned cultivation had the algae culturing liquid of sea growing chlorella to be injected in the I of pH regulator pond, and add ammoniacal liquor (massfraction 20%) and regulate its pH to 10 ~ 10.5; Flow in subsider 2 (hydraulic detention time is for 1h) by feed liquid port conduit 1 with the flow of 60L/h again, be divided into the dense algae liquid of flocculation and supernatant liquor, the dense algae liquid that flocculates flows out through the pond outlet at bottom 4 of subsider 2, flow in Circulation foam tower V (being entered by algae liquid entrance 8 bottom circulation section) by relay tank IV, and supernatant liquor is derived through the top overflow outlet 3 of subsider 2, enter neutralization tank III, and pass into rich CO wherein
2air (12%, volume ratio), make pH return to 8.0 ~ 8.5, then return culture systems and recycle, continue cultivate micro-algae;
Wherein, the volume of subsider 2 is 68L, and main structure parameters is as follows: high 980mm, and diameter (internal diameter) 300mm (aspect ratio is 3.3), penstock internal diameter is 30mm.
3) by the gas distributor 7 bottom Circulation foam tower V, air is blasted wherein, empty tower gas velocity is 0.06-0.3cm/s, according to the principle of Airlift circulating, make the dense algae liquid formation of the flocculation in inflow Circulation foam tower V around the circulation of guide shell 6, and add tensio-active agent (wherein in auxiliary agent entrance 9 Continuous Flow, tensio-active agent is the mixture of SDS and Tween20, and it is every 1m that stream adds ratio
3the dense algae liquid stream that flocculates adds the SDS of 30 ~ 120g and the Tween20 of 20 ~ 60g) and sepa-ration aid (sepa-ration aid is FeCl
3, stream adds ratio and is: every 1m
3the dense algae liquid stream that flocculates adds the FeCl of 40 ~ 80g
3its effect is that the frustule group diameter of alkalescence flocculation is increased further, reach 10 ~ 40m, to improve the efficiency of foam separation), the stream rate of acceleration (at the uniform velocity stream adds) of tensio-active agent and sepa-ration aid adds ratio-dependent according to feeding rate according to above-mentioned stream; As can be seen from Figure 2: under circulation and ventilation effect, form a large amount of micro-bubble, these bubbles rise to foam section, flowed out by overflow weir 12 and enter foam chute 11, form the foam layer of certain altitude; Frustule is under the mixing effect of circulation, also be enriched in bubble surface in a large number with bubble contact, rise to foam section with bubble, and be enriched in foam layer, collect foam in foam holding tank VI by foam solution outlet 13, and obtain highly enriched algae liquid after leaving standstill froth breaking.After being separated micro-algae, clear liquid flows out from circulation section purified liquor outlet 10 and enters Debubbling tank VII.Air is passed in Debubbling tank, in clear liquid, a small amount of tensio-active agent is taken in foam by the bubble produced further, foam is directly returned the foam chute of Circulation foam tower, and the deaeration liquid after deaeration returns subsider II (mixing with fresh algae liquid after adjustment pH).
In above-mentioned whole operation, the pH keeping system in circulation foam column is 10 ~ 11, and flocculation concentration algae liquid hydraulic detention time is wherein 0.3 ~ 2h, ensures that in Circulation foam tower, quiet liquid level is positioned at 10 ~ 50cm above guide shell 6.
The separating effect of the flocculating settling under this condition is as shown in table 1 below, can learn from following table 1: after adjustment pH is more than 10.5, its backwater rate and concentration ratio are all without significantly improving, therefore pH=10 ~ 10.5 are preferred scope.
The separating effect of table 1, flocculating settling
Embodiment 2, the continuous microalgae of weakly alkaline flocculation-foam separation:
Adopt step in the same manner as in Example 1 completely, only change the flow flowing into sea growing chlorella nutrient solution in subsider 2.When flow difference (thus hydraulic detention time is different) of sea growing chlorella nutrient solution, the separating effect obtained is as shown in table 2, can learn from table 2: along with the prolongation of hydraulic detention time, can obtain the higher rate of recovery and cycles of concentration.
Table 2, flocculation deposition seperation effect
| Algae flow quantity (L/h) | 120 | 60 | 15 |
| Hydraulic detention time (h) | 0.5 | 1 | 4 |
| Supernatant liquor flow (L/h) | 107.4 | 54.2 | 13.8 |
| To flocculate dense algae flow quantity (L/h) | 12.6 | 5.8 | 1.2 |
| Supernatant liquor frustule concentration (individual/mL) | 3.5×10 6 | 7.0×10 5 | 6.0×10 5 |
| The rate of recovery (%) | 92.9 | 98.6 | 98.7 |
| Cycles of concentration | 8.9 | 11.0 | 12.3 |
Embodiment 3, weakly alkaline flocculation-foam separation interval microalgae:
1) the algae kind adopted and nutrient solution are with embodiment 1, and at the end of cultivation, in sea growing chlorella nutrient solution, frustule concentration is 4.5 × 10
7individual/mL;
2) adopt the operating method of periodical operation, above-mentioned cultivation is had the sea growing chlorella nutrient solution of sea growing chlorella, once add 60L in subsider 2, and add ammoniacal liquor (massfraction 20%) and regulate its pH to 10 ~ 10.5; Start sedimentation, make the settling time of algae culturing liquid in subsider 2 be 0.5 ~ 4h, be divided into flocculation dense algae liquid and supernatant liquor, pond outlet at bottom 4 extraction of dense algae liquid through subsider 2 of flocculating, and be stored in relay tank IV and treat that next step is separated; And CO is passed in supernatant liquor
2after regulating pH to cultivation required 8.0 ~ 8.5, then return culture systems and recycle, continue to cultivate micro-algae;
Wherein, the structure of subsider 2 is with embodiment 1.
3) added in foam circulation tower V by dense for a collection of flocculation be stored in relay tank IV algae liquid, tensio-active agent and sepa-ration aid can disposablely add, and pump also can be adopted to add tensio-active agent by Circulation foam tower auxiliary agent entrance 9 Continuous Flow:
When tensio-active agent and auxiliary agent disposable add fashionable, flocculate no longer to produce foam in dense algae liquid time end operation, time needed for whole process adjusts by empty tower gas velocity, and the scope of empty tower gas velocity is 0.06 ~ 0.3cm/s, within the scope of this, usually can complete separation in 0.5 ~ 4h; The tensio-active agent added in foam separating tower is the mixture of SDS and Tween20 or Tween80; Sepa-ration aid is FeCl
3.Disposable when adding the dense algae liquid of flocculation, preferably select for one be: tensio-active agent adopts the combination of SDS and Tween20, every 1m
3the consumption flocculated in dense algae liquid is the FeCl of the SDS of 40 ~ 160g, the Tween20 of 30 ~ 90g and 60 ~ 90g
3,
When tensio-active agent and auxiliary agent stream added-time, continue to pass into air after stream adds end, the scope of empty tower gas velocity is 0.06 ~ 0.3cm/s, until no longer produce foam in algae liquid.The time that tensio-active agent and auxiliary agent stream add is 0.5 ~ 2h, and the tensio-active agent added in foam separating tower is the mixture of SDS and Tween20 or Tween80; Sepa-ration aid is FeCl
3.When adopting fed-batch mode, tensio-active agent adopts the combination of SDS and Tween20, every 1m
3the consumption flocculated in dense algae liquid is the SDS of 30 ~ 120g, the Tween20 of 20 ~ 60g) and the FeCl of 40 ~ 80g
3, stream rate of acceleration (at the uniform velocity) adds the time according to total stream and stream dosage is determined;
By the gas distributor 7 bottom Circulation foam tower V, air is blasted wherein, empty tower gas velocity is 0.06-0.3cm/s, according to the principle of Airlift circulating, make the dense algae liquid formation of the flocculation in Circulation foam tower V around the circulation of guide shell 6, under circulation and ventilation effect, form a large amount of micro-bubble, these bubbles rise to foam section, flowed out by overflow weir 12 and enter foam chute 11, form the foam layer of certain altitude; Frustule is under the mixing effect of circulation, also be enriched in bubble surface in a large number with bubble contact, rise to foam section with bubble, and be enriched in foam layer, collect foam in foam holding tank VI by foam solution outlet 13, and obtain highly enriched algae liquid after leaving standstill froth breaking.After being separated micro-algae, clear liquid flows out from circulation section purified liquor outlet 10 and enters Debubbling tank VII.Air is passed in Debubbling tank, in clear liquid, a small amount of tensio-active agent is taken in foam by the bubble produced further, foam is directly returned the foam chute of Circulation foam tower, and the deaeration liquid after deaeration returns subsider II (mixing with fresh algae liquid after adjustment pH)
In above-mentioned whole operation, the pH keeping system in circulation foam column is 10 ~ 11, ensures that in Circulation foam tower, quiet liquid level is positioned at 10 ~ 50cm above guide shell 6.
The separating effect of different settling time is as shown in table 3.
The separating effect of table 3, weakly alkaline flocculation separation
| Settlement separate time (h) | 0.5 | 1 | 4 |
| Supernatant liquid measure (L) | 49.6 | 53.1 | 54.8 |
| To flocculate dense algae liquid measure (L) | 10.4 | 6.9 | 5.2 |
| Supernatant liquor frustule concentration (individual/mL) | 3.8×10 6 | 7.5×10 5 | 6.0×10 5 |
| The rate of recovery (%) | 92.9 | 98.5 | 98.8 |
| Cycles of concentration | 5.4 | 8.6 | 11.4 |
Embodiment 4, the continuous microalgae of weakly alkaline flocculation-foam separation:
By in embodiment 1 through sedimentation in subsider 2 the dense algae liquid of flocculation that obtains (frustule concentration is 4.5 × 10
8individual/mL) adopt the mode of operate continuously, be injected in Circulation foam tower, carry out foam separation.
Wherein, Circulation foam tower cumulative volume is 20L, and circulation segment body amasss as 7L, and foam enrichment segment body amasss 13L.Main structure parameters is as follows: circulation section height 780mm, diameter (internal diameter) 110mm; Guide shell 6 diameter 70mm, height 620mm; Foam section height 400mm, diameter 200mm.
In foam separation, tensio-active agent, sepa-ration aid and stream dosage have 3 schemes, as shown in table 4.Flocculation concentration algae flow quantity 5.8L/h, the hydraulic detention time 1h in Circulation foam tower, empty tower gas velocity is 0.3cm/min, and pH value of solution is 10.1 ~ 10.6, and the separation of this condition result of gathering is as shown in table 5.
Table 4, three kinds of sepa-ration aid schemes
The separating effect of table 5, foam separation
Note: * is the flow of contained liquid in foam.
Embodiment 5, the continuous microalgae of weakly alkaline flocculation-foam separation:
By dense for the flocculation obtained after hydraulic retention 2h in subsider 2 in embodiment 3 algae liquid, (frustule concentration is 3.9 × 10
8individual/mL) adopt the mode of operate continuously, be injected in Circulation foam tower, carry out foam separation.
In Circulation foam tower, the parameter of each parts as described in example 4 above.
The tensio-active agent adopted, auxiliary agent and stream add ratio to be undertaken by the option A in embodiment 4, and improve in proportion according to the dense algae flow quantity of flocculation, concrete stream rate of acceleration is as shown in table 7.Empty tower gas velocity is 0.3cm/min, and pH value of solution is 10.1 ~ 10.6.In flocculation concentration algae flow quantity difference (therefore hydraulic detention time is different) situation, be separated result of gathering as shown in table 7:
The effect that table 7, state modulator and foam separation are separated
Note: * is the flow of contained liquid in foam.
Embodiment 6, weakly alkaline flocculation-foam separation gap microalgae:
By in embodiment 1 through sedimentation in subsider 2 the dense algae liquid of flocculation that obtains (frustule concentration is 3.8 × 10
8individual/mL) adopt the mode of gap operating, join in Circulation foam tower, carry out foam separation.
In Circulation foam tower, the parameter of each parts as described in example 4 above.
The disposable dense algae liquid that flocculated by 6L joins in Circulation foam tower, simultaneously disposablely adds 400mg surfactant SDS, 120mg tensio-active agent Tween20 and 500mg auxiliary agent FeCl
3.In Circulation foam tower, the pH of system is 10.1 ~ 10.6.Pass into air until no longer produce foam by different empty tower gas velocities, separating resulting is as shown in table 8.
The separating effect of table 8, foam separation
| Empty tower gas velocity (cm/s) | 0.2 | 0.12 | 0.08 |
| Foam separation time (h) | 0.6 | 1.1 | 2 |
| Foam liquid measure * (L) | 0.4 | 0.3 | 0.5 |
| Clear liquid frustule concentration (individual/mL) | 8.4×10 7 | 3.0×10 7 | 8.8×10 6 |
| The rate of recovery (%) | 79.3 | 92.5 | 97.9 |
| Cycles of concentration | 11.9 | 18.5 | 11.7 |
Note: * is the amount (lower same) of contained liquid in foam.
Embodiment 7, weakly alkaline flocculation-foam separation microalgae:
By in embodiment 1 through sedimentation in subsider 2 the dense algae liquid of flocculation that obtains (frustule concentration is 3.8 × 10
8individual/mL) adopt the mode of gap operating, join in Circulation foam tower, carry out foam separation.
In Circulation foam tower, the parameter of each parts as described in example 4 above.
The disposable dense algae liquid that flocculated by 6L adds in Circulation foam tower, and stream adds surfactant SDS, Tween20 and auxiliary agent FeCl
3stream rate of acceleration as shown in table 9.Empty tower gas velocity is 0.08cm/min, and in Circulation foam tower, the pH of system is 10.1 ~ 10.6, adopts different foam disengaging time, the stream rate of acceleration of tensio-active agent and separating resulting as shown in table 9:
The separating effect of table 9, foam separation
Embodiment 8, the continuous microalgae of weakly alkaline flocculation-foam separation:
1) sea growing chlorella (MarineChlorella), diameter is 3 ~ 8 μm, (f/2 is adopted to improve sea water medium in sea growing chlorella nutrient solution, the pH value of nutrient solution is 8.4, be called for short algae culturing liquid) in cultivate, at the end of cultivation, in sea growing chlorella nutrient solution, frustule concentration is 4.5 × 10
7individual/mL;
2) operating method of the continuous operation of weakly alkaline flocculation-fluid circling bubbling separation waste water treatment two-stage is adopted, above-mentioned cultivation there is the sea growing chlorella nutrient solution of sea growing chlorella to be injected in the I of pH regulator pond, and add ammoniacal liquor (massfraction 20%) and regulate its pH to 10 ~ 10.5; Flow in subsider 2 (hydraulic detention time is for 1h) by feed liquid port conduit 1 with the flow of 60L/h again, be divided into the dense algae liquid of flocculation and supernatant liquor, the dense algae liquid that flocculates flows out through the pond outlet at bottom 4 of subsider 2, flow in Circulation foam tower V (being entered by algae liquid entrance 8 bottom circulation section) by relay tank IV, and supernatant liquor is derived through the top overflow outlet 3 of subsider 2, enter neutralization tank III, and pass into rich CO wherein
2air (12%, volume ratio), after making pH return to 8.0 ~ 8.5, then return culture systems and recycle, continue cultivate micro-algae;
Wherein, the volume of subsider 2 is 68L, and main structure parameters is as follows: high 980mm, and diameter (internal diameter) 300mm (aspect ratio is 3.3), penstock internal diameter is 30mm.
3) tensio-active agent adopted, auxiliary agent and stream add ratio to be undertaken by the option A in embodiment 4, and in Circulation foam tower, system pH is 10.1 ~ 10.6, and the hydraulic detention time in Circulation foam tower is 1h.Blast wherein by the gas distributor 7 bottom Circulation foam tower V by air, empty tower gas velocity is 0.3cm/s, according to the principle of the Airlift circulating in embodiment 1, obtains highly enriched algae liquid.After being separated micro-algae, clear liquid flows out from circulation section purified liquor outlet 10 and enters Debubbling tank VII.Air is passed in Debubbling tank, in clear liquid, a small amount of tensio-active agent is taken in foam by the bubble produced further, foam is directly returned the foam chute of Circulation foam tower, and the deaeration liquid after deaeration returns subsider 2 (mixing with fresh algae liquid after adjustment pH).
In above-mentioned whole operation, the pH keeping system in circulation foam column is 10 ~ 11, ensures that in Circulation foam tower, quiet liquid level is positioned at 10 ~ 50cm above guide shell 6.
Collect foam, in foam holding tank, obtain highly enriched algae liquid.The material balance data of continuous operational process is as shown in table 10, and separating effect is as shown in table 11.Finally obtain in dense algae liquid, frustule dry weight content reaches 35g/L.
The material balance data of table 10, weakly alkaline flocculation-fluid circling bubbling separation waste water treatment two-stage continuous operation
Note: * flow is the flow of contained liquid in foam.
The separating effect of table 11, weakly alkaline flocculation-foam separation
| Unit | Subsider | Circulation foam tower | Totally |
| The rate of recovery (%) | 97.8 | 94.4 | 97.6 |
| Concentration ratio | 10.1 | 18.2 | 177 |
Claims (10)
1. a method for microalgae recovery, comprises the steps:
1) pH regulator is carried out to algae liquid, the algae liquid after adjusted pH;
2) by step 1) in adjustment pH after algae liquid in settling bowl, carry out flocculating settling, obtain flocculation algae liquid and supernatant liquor;
3) to step 2 is housed) in flocculation algae liquid, tensio-active agent and sepa-ration aid foam separating tower in pass into air, make micro-algae be enriched in foam, collect foam, namely gather and obtain micro-algae.
2. the method for claim 1, it is characterized in that: described pH regulator carries out by the following method: in described algae liquid, add pH adjusting agent, regulate pH to 10 ~ 10.5 of described algae liquid, wherein, described pH adjusting agent specifically can be the NaOH aqueous solution, the KOH aqueous solution or NH
3the aqueous solution;
And/or the micro-algae in described algae liquid is ball algae or intends ball algae, and described ball algae specifically can be sea growing chlorella or Porphyridium cruentum; Described plan ball algae specifically can be micro-plan ball algae.
3. method as claimed in claim 1 or 2, is characterized in that: step 2) and step 3) be operate continuously or gap operating:
Described step 2) and step 3) for operate continuously time:
Step 2) in, the hydraulic detention time of described flocculating settling is 0.5 ~ 2h;
Step 3) in, described tensio-active agent is selected from the mixture of SDS and substance A, and wherein, the mass ratio of SDS and substance A is 1:0.5 ~ 2, and substance A is selected from Tween20 and/or Tween80;
Described sepa-ration aid is FeCl
3;
The ratio of described flocculation algae liquid, described tensio-active agent and described sepa-ration aid is as follows: 1m
3sepa-ration aid described in tensio-active agent described in 20 ~ 250g and 30 ~ 120g is added in described flocculation algae liquid;
The hydraulic detention time of described flocculation algae liquid in described foam separating tower is 0.3 ~ 2h;
Or, described step 2) and step 3) for periodical operation time:
Described tensio-active agent and sepa-ration aid is disposable when joining foam separating tower:
Step 2) in, the settling time of described flocculating settling is 0.5 ~ 4h.
Step 3) in, described tensio-active agent is selected from the mixture of SDS and substance A, and wherein, the mass ratio of SDS and substance A is 1:0.5 ~ 2, and substance A is selected from Tween20 and/or Tween80;
Described sepa-ration aid is FeCl
3;
The ratio of described flocculation algae liquid, tensio-active agent and sepa-ration aid is as follows: 1m
3sepa-ration aid described in tensio-active agent described in 60 ~ 240g and 60 ~ 120g is added in described flocculation algae liquid;
The described flocculation algae foam separation time of liquid in described foam separating tower is 0.5 ~ 4h;
Described tensio-active agent and sepa-ration aid are when at the uniform velocity stream is added to foam separating tower:
Step 2) in, the settling time of described flocculating settling is 0.5 ~ 4h.
Step 3) in, described tensio-active agent is selected from the mixture of SDS and substance A, and wherein, the mass ratio of SDS and substance A is 1:0.5 ~ 2, and substance A is selected from Tween20 and/or Tween80;
Described sepa-ration aid is FeCl
3;
The ratio of described flocculation algae liquid, tensio-active agent and sepa-ration aid is as follows: 1m
3sepa-ration aid described in tensio-active agent described in 20 ~ 250g and 30 ~ 120g is added in described flocculation algae liquid;
The described flocculation algae foam separation time of liquid in described foam separating tower is 0.5 ~ 2h;
Described foam separating tower is circling and bubbling separation column.
4. method as claimed in claim 3, is characterized in that: step 2) and step 3) be operate continuously or gap operating:
Described step 2) and step 3) for operate continuously time:
The ratio of described flocculation algae liquid, described tensio-active agent and described sepa-ration aid is as follows: 1m
330 ~ 120gSDS, 20 ~ 60gTween20 and 40 ~ 80gFeCl is added in described flocculation algae liquid
3;
Or, described step 2) and step 3) for periodical operation time:
Described tensio-active agent and sepa-ration aid is disposable when joining foam separating tower:
The ratio of described flocculation algae liquid, described tensio-active agent and described sepa-ration aid is as follows: 1m
340 ~ 160gSDS, 30 ~ 90gTween20 and 60 ~ 90gFeCl is added in described flocculation algae liquid
3;
Described tensio-active agent and sepa-ration aid are when at the uniform velocity stream is added to foam separating tower:
The ratio of described flocculation algae liquid, described tensio-active agent and described sepa-ration aid is as follows: 1m
330 ~ 120gSDS, 20 ~ 60gTween20 and 40 ~ 80gFeCl is added in described flocculation algae liquid
3.
5. the method according to any one of claim 1-4, is characterized in that: in described foam separating tower, the pH of system is 10 ~ 11, and empty tower gas velocity is 0.06 ~ 0.3cm/s;
Quiet liquid level in described foam separating tower is higher than described guide shell upper end 10 ~ 50cm.
6. the method according to any one of claim 1-5, is characterized in that: step 2) in, also comprise passing in described supernatant liquor and be rich in CO
2air, make the pH of described supernatant liquor return to 8.0 ~ 8.5, then returned culture systems and recycle, wherein, described in be rich in CO
2air in CO
2volume fraction be 0.5%-12%;
Step 3) in, also comprise and import in Debubbling tank by the clear liquid in described foam separating tower, carry out deaeration, obtain deaeration liquid and foam, then deaeration liquid is imported settling bowl, foam imports to the foam enrichment section in described Circulation foam tower.
7. the method according to any one of claim 1-6 microalgae recovery device, comprise settling bowl (II) and Circulation foam tower (V), wherein, flocculation algae liquid outlet (4) in described settling bowl (II) is connected with the algae liquid entrance (8) in described Circulation foam tower (V) by relay tank (IV).
8. microalgae recovery device as claimed in claim 7, it is characterized in that: described settling bowl (II) is vertical-flow settling bowl, by feed liquid port conduit (1), subsider (2), overflow exports (3) and flocculation algae liquid outlet (4) is formed, wherein, the upper end of described feed liquid port conduit (1) is naked leaks outside the top of described subsider (2), and remainder is positioned at the inside of described subsider (2); Described overflow outlet (3) is positioned at middle and upper part or the top of described subsider (2); Described flocculation algae liquid outlet (4) is positioned at the bottom of described subsider 2;
Described Circulation foam tower (V) is made up of circulation section and foam enrichment section, wherein, described circulation section is made up of tower body (5), guide shell (6) and gas distributor (7), described foam enrichment section is by foam chute (11), and foam overflow weir (12) and foam outlet (13) are formed; Described guide shell (6) is positioned at the inside of described tower body (5), forms annular space with the inner tower wall of described tower body (5); Described gas distributor (7) is positioned at bottom or the bottom of the inner bottom part of described tower body (5) and the inside of described guide shell (6); Middle and lower part or the bottom of described tower body (5) have algae liquid entrance (8), and described algae liquid entrance (8) is positioned at the bottom of described guide shell (6) and the top of gas distributor (7); The middle and lower part of described tower body (5) or bottom have auxiliary agent entrance (9), and described auxiliary agent entrance (9) is positioned at the bottom of the annular space that described guide shell (6) is formed with the inner tower wall of described tower body (5); The middle and upper part of described tower body (5) has purified liquor outlet (10), and described purified liquor outlet (10) is positioned at the middle and upper part of the annular space that described guide shell (6) is formed with the inner tower wall of described tower body (5).
9. microalgae recovery device as claimed in claim 8, is characterized in that: the aspect ratio of described subsider (2) is 3 ~ 5;
The aspect ratio of the circulation section in described Circulation foam tower is (5 ~ 9): 1;
The aspect ratio of the circulation section in described foam chute and described Circulation foam tower is (1 ~ 2): 3, and diameter is than being (1 ~ 2.8): 1;
The ratio of the foam height of weir plate in described Circulation foam tower and described foam chute height is (1 ~ 2): 3;
Quiet liquid level in described foam separating tower is higher than described guide shell upper end 10 ~ 50cm.
10. microalgae recovery device as claimed in any one of claims 7-9, it is characterized in that: described microalgae recovery device comprises following auxiliary facility: flocculation pH regulator pond (I), neutralization tank (III), relay tank (IV), foam holding tank (VI) and Debubbling tank (VII)
Wherein, described flocculation pH regulator pond (I) is connected with the feed liquid port conduit (1) in described settling bowl (II); Described neutralization tank (III) is connected with overflow outlet (3) in described settling bowl (II); Described foam holding tank (VI) is connected with the foam outlet (13) in described Circulation foam tower (V); The entrance of described Debubbling tank is connected with the purified liquor outlet in described Circulation foam tower, and the outlet of described Debubbling tank is connected with the foam enrichment section in described Circulation foam tower with the feed liquid port conduit in described settling bowl respectively.
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106282006A (en) * | 2016-08-31 | 2017-01-04 | 浙江省海洋水产养殖研究所 | A kind of automation equipment preserved for oceanic generator |
| CN108410738A (en) * | 2018-05-28 | 2018-08-17 | 中国科学院南海海洋研究所 | A kind of method that the concentration of purple ball algae harvests and purple ball algae culture harvest the method being coupled with concentration |
| CN114053747A (en) * | 2021-11-27 | 2022-02-18 | 河南恒天久大实业有限公司 | Device system for separating glycerin and methyl ester |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101870883A (en) * | 2009-04-24 | 2010-10-27 | 中国石油天然气股份有限公司 | Method for producing sulfur through separation, vulcanization and hydrogen oxidation of circling foam |
| CN102127509A (en) * | 2010-01-19 | 2011-07-20 | 新奥科技发展有限公司 | Method, device and system for separating microalgae |
| CN102839127A (en) * | 2012-08-28 | 2012-12-26 | 浙江工业大学 | Method for microalgae coupling of culturing and recovery to quickly accumulate algal oil |
| CN103013833A (en) * | 2012-12-28 | 2013-04-03 | 中国科学院南海海洋研究所 | Novel high pH induction and carbon dioxide emission reduction coupling microalgae harvesting method |
| CN104803523A (en) * | 2015-04-13 | 2015-07-29 | 南昌大学 | Electric flocculation and air floatation combined continuous microalgae harvesting device and method |
-
2015
- 2015-10-20 CN CN201510683998.4A patent/CN105176826B/en active Active
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101870883A (en) * | 2009-04-24 | 2010-10-27 | 中国石油天然气股份有限公司 | Method for producing sulfur through separation, vulcanization and hydrogen oxidation of circling foam |
| CN102127509A (en) * | 2010-01-19 | 2011-07-20 | 新奥科技发展有限公司 | Method, device and system for separating microalgae |
| CN102839127A (en) * | 2012-08-28 | 2012-12-26 | 浙江工业大学 | Method for microalgae coupling of culturing and recovery to quickly accumulate algal oil |
| CN103013833A (en) * | 2012-12-28 | 2013-04-03 | 中国科学院南海海洋研究所 | Novel high pH induction and carbon dioxide emission reduction coupling microalgae harvesting method |
| CN104803523A (en) * | 2015-04-13 | 2015-07-29 | 南昌大学 | Electric flocculation and air floatation combined continuous microalgae harvesting device and method |
Non-Patent Citations (2)
| Title |
|---|
| 刘晃等: "饵料微藻采收技术研究进展与展望", 《渔业现代化》 * |
| 胡沅胜等: "微藻处理污水中的絮凝分离/采收研究现状与展望", 《环境科学学报》 * |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106282006A (en) * | 2016-08-31 | 2017-01-04 | 浙江省海洋水产养殖研究所 | A kind of automation equipment preserved for oceanic generator |
| CN106282006B (en) * | 2016-08-31 | 2018-07-27 | 浙江省海洋水产养殖研究所 | A kind of automation equipment preserved for oceanic generator |
| CN108410738A (en) * | 2018-05-28 | 2018-08-17 | 中国科学院南海海洋研究所 | A kind of method that the concentration of purple ball algae harvests and purple ball algae culture harvest the method being coupled with concentration |
| CN114053747A (en) * | 2021-11-27 | 2022-02-18 | 河南恒天久大实业有限公司 | Device system for separating glycerin and methyl ester |
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|---|---|
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