CN1178513A - Process for high concentrated waste water treatment using membrane separation - Google Patents
Process for high concentrated waste water treatment using membrane separation Download PDFInfo
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- CN1178513A CN1178513A CN96192563A CN96192563A CN1178513A CN 1178513 A CN1178513 A CN 1178513A CN 96192563 A CN96192563 A CN 96192563A CN 96192563 A CN96192563 A CN 96192563A CN 1178513 A CN1178513 A CN 1178513A
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Abstract
The present invention relates to a process for treatment of high concentrated waste water from animal husbandry, human excretion and other high organic waste. This process includes warming, anaerobic digestion, separation with ultra filtration (UF)/reversed osmosis (RO) membranes. The residual solution after RO separation is the raw material of liquid fertilizer for water culture and foliar spray.
Description
The present invention relates generally to the method that the utilization membrane sepn is handled high concentrated waste water.It is applicable to cattle breeding, the processing of human feces, and in the processing of other high organic sewage.
This method is by heating, anaerobic digestion (fermentation), and ultrafiltration and last reverse osmosis isolation stage finish, and separate the concentrated solution that leaches by RO (reverse osmosis) and can be used as liquid fertilizer.
Usually, from economy and technological standpoint, there are some problems in the many existing method that is used for sewage disposal, so they seldom are used in industrial circle.Although the well-known self-cleaning limit is the BOD (biochemical oxygen demand (BOD)) of 10mg/L, from the scope of the sewage of the sanitary wastewater BOD from tens to several thousand 10mg/L, and the scope of animal sewage is from the BOD of tens to several ten thousand 10mg/L.
Fig. 1 is the sectional view of heating installation.
Fig. 2 is a sectional view of adjusting jar.
Fig. 3 is the sectional view of anaerobic digestor.
Fig. 4 is mounted in the profile of odor removal in the heating installation.
The present invention is different from common existing Sewage treatment systems.It can decompose highly enriched organic sewage by anaerobically fermenting in several days, anaerobically fermenting sewage is to handle with the BOD of UF/RO film with 0.1mg/L.
In the heating phase, the ammonia that suppresses anaerobically fermenting is discharged from, and lipid acid is decomposed.And sewage temperature remains between 33 ℃ to 35 ℃ the anaerobically fermenting stage below this is fit to.
Sewage from anaerobic jar is converted into the comparison clean water by the UF/RO membrane sepn.And can be used as the energy by the methane gas that anaerobically fermenting produces as byproduct.And the surplus solution after RO separates is aseptic and is rich in organic and inorganic composition, therefore by adding the raw material that some additives can become it liquid fertilizer.
In the present invention, some steps such as the sewage collecting of pretreatment stage, simple precipitation is identical with general traditional method with solid-liquid separation, but core procedure of the present invention is as heating, and the predecomposition adjusting stage, anaerobically fermenting separates with UF/RO and need purify waste water.
These step diagrams are as follows:
The present invention is to the detailed description of high concentrated waste water treatment process, can be in the time of needs with reference to accompanying drawing, as follows:
(1) heating phase
The branch of getting rid of through solid-liquid separator in the sewage of solid matter is dried up, enters heating installation 1 by water inlet pipe 2, is heated when it flows through on the hot-plate 5 that stainless material makes, and disposes copper pipe 10 below this hot-plate to be used for flowing through about 90 ℃ hot water.Separated flow has a down dip and is attached at the coarse plate 6 that the stupalith on hot-plate 5 one sides is made then, flows into waste pipe 3 gradually, and this hot-plate has 8 to 13 rank in order.
Discharge by the venting hole 4 of gas collector and deodorizing (utilize the odor removal of Fig. 4, it is designed and applied for registration of by the present inventor and is Korean Utility Model, notification number 94-1158) at this stage ammonia, some lipid acid decompose simultaneously.Adjust jar 11 (the fibre-reinforced plastics (FRP) or stainless) in the thermal insulation of Fig. 2 from the waste pipe 3 effusive hot-water storages of described heating installation 1, thereby temperature is remained between 33 ℃ to 35 ℃, and be transported in the anaerobic digestor 22 by constant flow power pump 19,20 each constant flows.
In the heating phase, at first by adopting multistep nature dropping process might get rid of a large amount of ammonia that suppresses anaerobic digestion at short notice effectively; The secondth, remain on the method for 33 ℃ to 35 ℃ adjustment jar inflow anaerobic digestor through temperature by making hot water, make described hot water after the process waste pipe 3 of described heating installation 1, temperature when it flows into anaerobic digestor 22 remains on 33 ℃ to 35 ℃, thereby helps the breeding (optimum temps: 30 ℃ to 35 ℃) of mesophilic bacteria.The 3rd, partial fatty acid just was decomposed at initial stage heating phase, the part remaining fatty acid is attracted on coarse plate 5 and the coarse plate 6 and discharges, Sheng Xia lipid acid can more easily fully be decomposed rapidly in anaerobic digestor 22 like this, at initial stage heating phase, by discharging abundant fatty acid, the life-span of film has been extended, because this ester fat acid is the material that reduces the UF/RO membrane permeability, this effect has proved the deciding factor that adopts the UF/RO membrane separating method in sewage disposal.
Each hot-plate 5 that is used for the heating installation 1 of heating phase separates each other, and so just removes the solid matter that is held by them and coarse plate 6 in the heating operation stage easily.
(2) the anaerobic digestion stage.
Flow into from the effusive hot water of the waste pipe 3 of heating installation 1 and describedly adiabaticly to adjust jars 11, through the adjusting stage, and be sent to anaerobic digestor 22 by described power pump 19,20 at there.Then, the hot water that flows into anaerobic digestors 22 through the water inlet pipe 23 of anaerobic digestor 22 has passed through the first contact medium layer 29 and the second contact medium layer 30, they are all in the centre chamber of described anaerobic digestor 22, upwards flow from following, and after this arrive waste pipe 24 by the 3rd contact medium layer 31, at last, by the UF/RO phase separating membrane.
More detailed adjustment and anaerobic digestion phase process are as follows:
If ideal anaerobic digestor 22 can be set up in a large number, such as, two to four, help the organic acid production phase, the quiet run in medium stage and each stage in methane gas production stage.
If in adjusting jar 11, ammonia, hydrogen sulfide etc. vapor away in the heating phase, and they volatilize by venting hole 21 one more chances.By the granular microbial that is deposited in the described anaerobic digestor 22 is returned to the described release that might prevent this quasi-microorganism in the jar 11 of adjusting, also help anaerobic digestion stable at short notice.
By a subsidiary agitator that reducing motor 17 is arranged being installed described the adjustment on jars 11, make waste water be stirred (quality according to the sewage of high BOD decides) with the slow speed in six weeks per hour thus microorganism can not stopped very actively by impact.
Remain on 33 ℃ to 35 ℃ from adjusting jar 11 hot water temperatures that flow into described anaerobic digestor 22, the power pump 19,20 by constant flow little by little flows into anaerobic digestor 22 with certain flow at every turn.The quick mobile of water impacts in order to prevent being subjected to into by methanogen, and ideal designs is such: the diameter of each water inlet pipe 23 is 40mm, and they laterally are arranged side by side, and the horal water inlet in each hole of water inlet pipe 23 preferably is maintained at about about 10 liters.
In order to prevent granular settling plugging hole sedimentary the time, water inlet pipe 23 is designed to both sides all perforate.By a series of constant flow power pumps 19,20 are installed, rather than only one, might alleviate the once long-time excessively work of a pump, prevention simultaneously has a pump danger of fault to occur.
Described anaerobic digestor 22 usefulness FRP or stainless steel are made circle; guarantee that it has the high strength of pressing in the opposing; three layers of diathermic wall are used for keeping inner 33 ± 1 ℃ steady temperature, even also be like this when the outside is-43 ℃ to 47 ℃, the protection methanogen avoids external impact.
It is about 30% of described anaerobic digestor 22 total heights that the height of each contact medium layer (polypropylene material) is made, the first contact medium layer 29 is positioned at 5/10 to 8/10 zone of this tank body height, the second contact medium layer 30, in 2/10 to 5/10 zone of this tank body height, the 3rd contact medium layer 31, in 4/10 to 7/10 zone of this tank body height, all be in order to increase of the absorption of this place to methanogen.
By such layout, effluent stream in the described anaerobic digestor 22 is being directed upwards through the first contact medium layer 29, absorption to the microorganism that may lose is more prone to, the current following current is fallen through the second contact medium layer 30 then, last adverse current is through the 3rd contact medium layer 31, stoped as much as possible and methanogen keeps enlivening to greatest extent in this place microorganism forfeiture.
In case a series of four anaerobic digestors with same design are set up, working efficiency has just improved, and the time of anaerobic digestion has just shortened greatly.
The methane that produces as the byproduct of anaerobic digestion can be collected in the holding tank (not shown) by a venting hole 28, is used for being converted into energy.
As mentioned above, the present invention carries out the process of anaerobic digestion at anaerobic digestor, meet nature whereabouts method, therefore, also can obtain to be used for enough pH (7.2 to 7.5) of anaerobic digestion even without artificial adjustment, make begin to run well after, when the steady flow of COD value is lasting, even in two days processing, also may finish anaerobic digestion.Although exist changes of seasons and sewage to flow into, COD value still keeps stablizing, and whatsoever under the situation, has just finished anaerobic digestion within five days, considers that common anaerobic digestion will use up 30 to 35 days, and this can't but be a surprising progress.
The size of anaerobic digestor is determined by the quality of the sewage that will handle.
(3) phase separating membrane
In order separating in the sewage that still is dispersed in by the anaerobic digestion stage,, to have used UF (ultrafiltration, 0.01 to 0.05mm), and be accompanied by RO (reverse osmosis with the solid matter that the fine particle form exists; 0.002 to 0.005mm) handle.In the present invention, by ultrafiltration, colloidal particle and soluble high-molecular material are separated, and are used for making liquid fertilizer.Among the present invention, the employed ultra-filtration membrane of phase separating membrane is by Mierocrystalline cellulose, polyacrylonitrile, and polyolefine, perhaps polysulfones is made.
At the RO phase separating membrane, be eliminated less than 350 material such as inorganic salt and carbohydrate equimolecular quantity.Rhodia, fat gather the film that acid amides and their mixture make and all can be used for this purpose.
Filter method at separation phase adopts cross-flow filtration, and in this process, does not accumulate on the film because the solute particulate can not surpass a certain thickness, thereby might carry out a large amount of operation continuously; The filtration unit that the back washing device is installed is applied, thereby film can be cleaned automatically.
(4) production of liquid fertilizer
In the present invention, high concentrated waste water passes through solids-liquid separation step, heating phase, adjust and anaerobic digestion stage and being cleaned, like this, when it is quite pure during at last by aforesaid UF/RO film, and can obtain aseptic, be rich in the surplus solution of the organic and inorganic substance of molecular weight from 130 to 5000, this organic and inorganics can be by the UF film but can not be passed through the RO film.
When surplus solution separates when concentrated through continuously many-RO (multi-RO), can obtain the concentrated liquid fertilizer of nitrogenous substances up to about 2%.And, through the UF membrane channel,, providing almost aseptic liquid fertilizer by removing most bacterium and yeast, this fertilizer also is highly suitable for applying fertilizer on the blade face.For preventing in the use of liquid fertilizer because the possible pollution of microorganism growth, add weight ratio and be 0.05% the concentrated mugwort extraction liquid (it contain chloro acid (chlosgenic acid) can suppress microbial growth effectively) of liquid fertilizer, or weight ratio is 0.1% a chitosan granule of liquid fertilizer and mixed.Mugwort also helps to remove the slight ight soil smell that still exists especially.
In the present invention, can utilize with methyl alcohol as solvent extraction and spissated concentrated mugwort extraction liquid.
Liquid fertilizer of the present invention can be used as that water planting is supported and the nutritive medium of foliage-spray.
Below the present invention is set forth, can be in the time of needs with reference to the example among the embodiment.
(1) heating phase
From stock-farms accumulative high concentrated waste water and mixed with 5 to 5 ratio from the human feces of human feces processing plant, and mixed sewage, wherein 10 tonnes are passed through solids-liquid separation step.In the heating installation that is equipped with 13 hot-plates (as shown in Figure 1), isolated sewage was handled according to the method described above in the heating phase of the present invention.The part hot water in the waste pipe of heating installation is flow through in extraction, and the effect analysis of the matter that clears the pollution off by heat treated is obtained the result, as following table 1:
Table 1. heating phase is removed the effect of all contaminations matter
| Distinguish | Project (ppm) | |||||
| BOD | ?COD | The N-hexane extract | ?NH 4-N | ?PO 4-P | ??SS | |
| Be untreated | 8600 | ?1500 | ?140 | 500 | ?120 | 2800 |
| After the heating | 6880(20) | ?1425(5) | ?110(21) | 350(30) | ?117(3) | 860(69) |
() clearance rate %
(2) the anaerobic digestion stage
Be inhaled into through heat treated and from the effusive hot water of the waste pipe of heating installation, and be stored in adjustment jar (as shown in Figure 2); It flows into anaerobic digestor (as shown in Figure 3) with 0.5 ton flow per hour under the effect of the constant flow power pump of adjusting jar, and carries out five days anaerobic treatment according to the above-mentioned steps of anaerobic digestion.Can use the umbrella extensive region to draw uncommon lattice ring (Sam Hwan Rash Ring, name of product) for the contact medium layer in the anaerobic digestor.After carrying out Anaerobic Digestion, extract the part of contaminated water and the analysis of flowing out anaerobic digestor through Send out pump, with the decontamination effect improving after definite heating and the combination of anaerobic digestion stage, following table 2 has provided the result who obtains.
In order to determine the effect in anaerobic digestion stage self, extract some and do not pass through the sewage in heat treated stage and carry out anaerobic treatment.The analytical results of this part is also contained in the table 2.
The decontamination effect improving of table 2. anaerobic digestion
| Distinguish | Project (ppm) | |||||
| BOD | COD | The N-hexane extract | NH 4-N | ?PO 4-P | ?SS | |
| ??Orig. | ??8600 | ??1500 | ??140 | ??500 | ??120 | ??2800 |
| ??UAD | ??1608(81.3) | ??250(83.3) | ??21(85) | ??100(80) | ??48(60) | ??65(98) |
| ??W+UAD | ??1286(85) ??17(99.4) | ??238(84.2) | ??17(87.9) | ??70(86) | ??46.8(61.0) | |
() clearance rate %
Orig.: untreated sewage UAD: W+UAD after the anaerobic digestion: after heating and the anaerobic digestion
(3) phase separating membrane
By the environmental operations that table 3 provides, can analyze the decontamination effect improving and the life-span of different types of membranes, the result is provided by following table 4 and 5.
Table 3. film type and operating environment
| ??UF | ??RO | |
| Temperature | ??19.9～21.1 | ????21.5 |
| Flow (m 3/hr) | ??1.0～1.2 | ????0.95～1.1 |
| Pressure (kg/cm 2) | ??6.0～8.8 | ????25～26 |
| Enrichment factor | ??4.7 | ????7.2 |
| Average flux (L/m 2.hr：25℃) | ??31.9 | ????21.9 |
Table 4.
| ????UF | ????RO | |||||
| ??Orig. | ??A | ????B | ??????C | ??????D | ????E | |
| BOD | ??8600 | ??1500(93.5) | ??230(97.3) | ???1930(77.6) | Less than 0.1 | ???70 |
| COD | ??1500 | ??1200(20.2) | ??350(96.7) | ???1430(4.7) | ????2.7 | ???140 |
| SS | ??2800 | ??950(66.1) | ??0(100.0) | ???2300(17.8) | ?????-- | ???-- |
| NH 4-N | ??500 | ??500(0.0) | ??460(8.0) | ???500(0.0) | ????20 | ???35 |
| PO 4-P | ??120 | ??68(43.3) | ??55(54.2) | ???84(30.0) | ????0.16 | ???5.4 |
| The N-hexane extract | ??140 | ??--(100.0) | ??--(100.0) | ???23(83.6) | ????-- | ???-- |
| Colourity | ??++ | ??++ | ???++ | Pink colour | ???+ | |
| Smell | Dog excrement flavor | ??++ | ???++ | The ammonia flavor | Dog excrement flavor | |
Sewage when the #RO film is handled is effusive from UF film B.
A: polysulfones B: polyacrylonitrile C: Mierocrystalline cellulose D: polymeric amide
E: rhodia+: pure--: do not detect
The mean lifetime of table 5. differing materials film
| ????UF | ????RO | ||
| Material | Life-span (moon) | Material | Life-span (moon) |
| Polysulfones | ????8 | Polymeric amide | A little more than 16 |
| Polyacrylonitrile | ????10 | Rhodia | ????10 |
| Mierocrystalline cellulose | ????7 | ||
On the basis of this test-results, to carry out a UF (UF (B) film of utilization table 4) and RO (RO (D) film of utilization table 4) processing again through the sewage of Anaerobic Digestion, determine decontamination effect improving, following table 6 is total has provided result progressively.
Table 6. is decontamination effect improving progressively
| Handle | Project (ppm) | |||||
| BOD | COD | SS | ?NH 4-H | PO 4-H | The N-hexane extract | |
| Be untreated: | 8600 | 1500 | 2800 | 500 | 120 | 140 |
| Post-heating W+UAD | 6880(20.0) 1286(85.0) | 1425(5.0) 238(84.2) | 860(69.0) 17(99.4) | 350(30.0) 70(86.0) | 117(3.0) 46.8(61.0) | 110(21.0) 17(87.9) |
| Behind UF (B) | 34.7(99.6) | 55.5(96.3) | --(100.0) | 64.4(87.2) | 21.4(82.1) | --(100.0) |
| (W+UAD+ UF)+RO (D) passage | Less than 0.1 (greater than 99.9) | Less than 1.2 (greater than 99.02) | --(100.0) | 2.8(99.5) | Less than 0.1 (greater than 99.9) | --(100.0) |
--: do not detect
(): purify %
(4) the liquid fertilizer production phase
In the stage of membrane sepn, still also concentrated with many continuously-RO separated and collected by the surplus solution of RO film by the UF film, portion water is discharged from and has obtained 1.8 tons of concentrated liquid fertilizer; Add weight percent and be 0.05% concentrated mugwort extraction liquid, obtain enough liquid fertilizers thereby dilute this mixed solution with 300 to 800 times water then.
This liquid fertilizer of test in Horticulture carries out on the blade of vegetables and flower finding that it can promote growth effectively usually, improves their output when spray on the blade face that especially chromatic colour is as shown in table 7.
The effect of liquid fertilizer when table 7. carries out the blade face injection
| Plant | Not fertilising | Apply liquid fertilizer | Remarks |
| Watermelon (sugariness) | ????10°-11?° | ??14?°-15° | |
| Radish (weight) | 42 grams | 51 grams | In 20 days |
| Red pepper (fruit amount weekly) | ????42-42 | ????48-52 | |
| Carnation (color) | ??????++ | ?????+++ | Color is clear |
| Lily (freshness) | ??????++ | ?????+++ | An about week |
Claims (6)
1. a method of handling high concentrated waste water comprises solids-liquid separation step, heating phase, anaerobic digestion stage, and ultrafiltration/reverse osmosis membrane separation stage.
2. in accordance with the method for claim 1, it is characterized in that: the heating phase comprises the inflow that enters the sewage of heating installation (1) through solid-liquid separator, sewage is heated on a series of hot-plates (5) in this heating installation, the side that is installed in them that each hot-plate (5) all has a coarse plate (6) to tilt, and heat sewage at last and flow out naturally by waste pipe 3.
3. in accordance with the method for claim 1, it is characterized in that: the anaerobic digestion stage comprises that heating sewage flows into an anaerobic digestor (22), wherein heat sewage and upwards flow through one first contact medium layer (29) successively, and be downward through one second contact medium layer (30), flow through one the 3rd contact medium layer (31) again.
4. in accordance with the method for claim 1, also comprise the adjusting stage, it is characterized in that: the sewage by the heat treated heating is stored in before the anaerobic digestion stage in the insulation adjustment jar (11), and temperature remains between 33 ℃ to 35 ℃.
5. in accordance with the method for claim 1, further comprise the liquid fertilizer production phase, it is characterized in that: the surplus solution after the reverse osmosis isolation is aseptic and is rich in organic and inoganic solids material, through reverse osmosis isolation repeatedly it concentrated the concentrated solution that obtains to be used for liquid fertilizer.
6. according to the method for claim 5, also comprise in concentrated solution adding mugwort extraction liquid or chitosan.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN96192563A CN1178513A (en) | 1995-02-17 | 1996-02-17 | Process for high concentrated waste water treatment using membrane separation |
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| KR3034/95 | 1995-02-17 | ||
| CN96192563A CN1178513A (en) | 1995-02-17 | 1996-02-17 | Process for high concentrated waste water treatment using membrane separation |
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| Publication Number | Publication Date |
|---|---|
| CN1178513A true CN1178513A (en) | 1998-04-08 |
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| Application Number | Title | Priority Date | Filing Date |
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| CN96192563A Pending CN1178513A (en) | 1995-02-17 | 1996-02-17 | Process for high concentrated waste water treatment using membrane separation |
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Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102276120A (en) * | 2011-07-27 | 2011-12-14 | 胡孟春 | Sewage treatment zero emission technical device utilizing solar septic tank |
| CN101863688B (en) * | 2009-04-16 | 2013-11-27 | 上海综宝环境工程有限公司 | Method for preparing water soluble quick-acting organic fertilizer from activated sludge |
| CN103663856A (en) * | 2013-04-26 | 2014-03-26 | 郭强 | High mixed-flow anaerobic combined type membrane biological reaction treatment process |
| CN106396281A (en) * | 2016-11-19 | 2017-02-15 | 郑州天舜电子技术有限公司 | Domestic small sewage treatment device |
| CN111712470A (en) * | 2017-12-15 | 2020-09-25 | 西博动力有限公司 | Salt management system for portable renewable energy micro power generation system |
-
1996
- 1996-02-17 CN CN96192563A patent/CN1178513A/en active Pending
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101863688B (en) * | 2009-04-16 | 2013-11-27 | 上海综宝环境工程有限公司 | Method for preparing water soluble quick-acting organic fertilizer from activated sludge |
| CN102276120A (en) * | 2011-07-27 | 2011-12-14 | 胡孟春 | Sewage treatment zero emission technical device utilizing solar septic tank |
| CN103663856A (en) * | 2013-04-26 | 2014-03-26 | 郭强 | High mixed-flow anaerobic combined type membrane biological reaction treatment process |
| CN106396281A (en) * | 2016-11-19 | 2017-02-15 | 郑州天舜电子技术有限公司 | Domestic small sewage treatment device |
| CN111712470A (en) * | 2017-12-15 | 2020-09-25 | 西博动力有限公司 | Salt management system for portable renewable energy micro power generation system |
| CN111712470B (en) * | 2017-12-15 | 2023-09-08 | 西博动力有限公司 | Salt management system for portable renewable energy micro power generation system |
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