CN107540148B - Wastewater treatment system and wastewater treatment method for preparing ethanol from cellulose - Google Patents
Wastewater treatment system and wastewater treatment method for preparing ethanol from cellulose Download PDFInfo
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- CN107540148B CN107540148B CN201610464935.4A CN201610464935A CN107540148B CN 107540148 B CN107540148 B CN 107540148B CN 201610464935 A CN201610464935 A CN 201610464935A CN 107540148 B CN107540148 B CN 107540148B
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- 239000001913 cellulose Substances 0.000 title claims abstract description 69
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- 238000007872 degassing Methods 0.000 claims abstract description 157
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- 239000007789 gas Substances 0.000 claims abstract description 146
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- 230000001376 precipitating effect Effects 0.000 claims description 26
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 claims description 24
- MHAJPDPJQMAIIY-UHFFFAOYSA-N Hydrogen peroxide Chemical compound OO MHAJPDPJQMAIIY-UHFFFAOYSA-N 0.000 claims description 22
- 238000004519 manufacturing process Methods 0.000 claims description 22
- 238000005189 flocculation Methods 0.000 claims description 19
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- 229910000359 iron(II) sulfate Inorganic materials 0.000 claims description 11
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- AXZKOIWUVFPNLO-UHFFFAOYSA-N magnesium;oxygen(2-) Chemical compound [O-2].[Mg+2] AXZKOIWUVFPNLO-UHFFFAOYSA-N 0.000 claims description 5
- 239000012716 precipitator Substances 0.000 claims description 3
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- 239000004912 1,5-cyclooctadiene Substances 0.000 abstract 1
- CKMXBZGNNVIXHC-UHFFFAOYSA-L ammonium magnesium phosphate hexahydrate Chemical compound [NH4+].O.O.O.O.O.O.[Mg+2].[O-]P([O-])([O-])=O CKMXBZGNNVIXHC-UHFFFAOYSA-L 0.000 description 28
- 229910052567 struvite Inorganic materials 0.000 description 28
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 12
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- MXZRMHIULZDAKC-UHFFFAOYSA-L ammonium magnesium phosphate Chemical compound [NH4+].[Mg+2].[O-]P([O-])([O-])=O MXZRMHIULZDAKC-UHFFFAOYSA-L 0.000 description 1
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- JTJMJGYZQZDUJJ-UHFFFAOYSA-N phencyclidine Chemical class C1CCCCN1C1(C=2C=CC=CC=2)CCCCC1 JTJMJGYZQZDUJJ-UHFFFAOYSA-N 0.000 description 1
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- AAKBLFQBZDFKMP-UHFFFAOYSA-H trimagnesium azane diphosphate Chemical compound N.[Mg+2].[Mg+2].[Mg+2].[O-]P([O-])([O-])=O.[O-]P([O-])([O-])=O AAKBLFQBZDFKMP-UHFFFAOYSA-H 0.000 description 1
Landscapes
- Physical Water Treatments (AREA)
- Purification Treatments By Anaerobic Or Anaerobic And Aerobic Bacteria Or Animals (AREA)
Abstract
The invention discloses a wastewater treatment system and a wastewater treatment method for preparing ethanol from cellulose, wherein the wastewater treatment system for preparing ethanol from cellulose comprises an anaerobic fermentation reaction device, a wastewater dephosphorization reaction device, a denitrification reactor and a deep treatment system which are sequentially connected in the wastewater treatment process direction, wherein the anaerobic fermentation reaction device comprises an anaerobic fermentation tank body, a gas stripping pipe and a gas feeding pipe, the gas stripping pipe is arranged in the anaerobic reaction chamber, the upper end of the gas stripping pipe is provided with a gas outlet, and the lower end of the gas stripping pipe is provided with a gas inlet; the wastewater dephosphorization reaction device comprises a dephosphorization reaction tank body, an aeration device and a degassing precipitation separator, wherein a dephosphorization reaction chamber is arranged in the dephosphorization reaction tank body, the dephosphorization reaction chamber is provided with a water inlet and a dephosphorization agent adding port, and the aeration device is arranged in the dephosphorization reaction chamber. The wastewater treatment system for preparing ethanol from cellulose has the advantages of simple structure, low cost, good COD and nitrogen and phosphorus treatment effect and the like.
Description
Technical Field
The invention relates to the technical field of environmental protection, in particular to a wastewater treatment system and a wastewater treatment method for preparing ethanol from cellulose.
Background
The traditional ethanol manufacturing process method adopts corn and cassava (namely starch) to prepare ethanol through fermentation and the like, the COD (organic pollutants) of the wastewater is usually between 2 thousands and 3 thousands, and the treatment is easy. However, the production process of the ethanol is forbidden due to the high cost of corn and cassava and limited raw materials.
For this reason, a process for producing ethanol from straw and stalk (cellulose) is proposed in the related art, and for straw and stalk, the cellulose in the interior is coated with external lignin, so that the lignin in the outer layer needs to be blasted by high temperature and high pressure or sulfuric acid, and saccharification is performed to produce ethanol after exposing the cellulose in the interior, the COD of the wastewater is usually between 5 ten thousand and 9 ten thousand, the treatment is relatively difficult, the structure of the wastewater treatment equipment is complex and the cost is high, the COD and nitrogen and phosphorus treatment effects are poor, and there is a need for improvement.
Disclosure of Invention
The present invention aims to solve at least one of the above-mentioned technical problems in the related art to some extent. Therefore, the invention provides a wastewater treatment system for preparing ethanol by cellulose, which has the advantages of simple structure, low cost, good COD and nitrogen and phosphorus treatment effects and the like.
The invention also provides a wastewater treatment method for preparing ethanol by cellulose, which can simplify the system structure, reduce the cost and improve the COD treatment effect.
In order to achieve the above object, according to an embodiment of the first aspect of the present invention, there is provided a wastewater treatment system for producing ethanol from cellulose, the wastewater treatment system for producing ethanol from cellulose including an anaerobic fermentation reaction device, a wastewater dephosphorization reaction device, a denitrification reactor and a further treatment system, which are sequentially connected in a wastewater treatment process direction, wherein the anaerobic fermentation reaction device includes an anaerobic fermentation tank body, a gas stripping tube and a gas supply tube, the anaerobic fermentation tank body is internally provided with an anaerobic reaction chamber, the anaerobic reaction chamber is provided with a wastewater inlet, a water outlet and a gas outlet, the gas stripping tube is arranged in the anaerobic reaction chamber, the upper end of the gas stripping tube is provided with a gas outlet, and the lower end of the gas stripping tube is provided with a gas inlet, and the gas supply tube is connected with the gas inlet of the gas stripping tube for supplying gas for stripping into the gas stripping tube; the wastewater dephosphorization reaction device comprises a dephosphorization reaction tank body, an aeration device and a degassing and precipitation separator, wherein a dephosphorization reaction chamber is arranged in the dephosphorization reaction tank body, the dephosphorization reaction chamber is provided with a water inlet and a dephosphorization agent adding port, the aeration device is arranged in the dephosphorization reaction chamber, and the degassing and precipitation separator is arranged in the dephosphorization reaction chamber and is positioned above the aeration device and is used for separating gas, water and sludge.
The wastewater treatment system for preparing ethanol from cellulose has the advantages of simple structure, low cost, good COD and nitrogen and phosphorus treatment effect and the like.
In addition, the wastewater treatment system for preparing ethanol by cellulose according to the embodiment of the invention can also have the following additional technical characteristics:
according to one embodiment of the invention, the lower end of the gas stripping pipe is adjacent to the bottom of the anaerobic reaction chamber, the upper end of the gas stripping pipe extends to the upper part of the anaerobic reaction chamber, and the water outlet is arranged at the upper part of the anaerobic reaction chamber and higher than the upper end of the gas stripping pipe.
According to one embodiment of the invention, the upper end face of the gas stripping tube is open to form the gas outlet, and the lower end face of the gas stripping tube is open to form the gas inlet.
According to one embodiment of the invention, the gas stripping tube comprises a straight tube section extending along the vertical direction and an arc-shaped section connected with the upper end of the straight tube section, and an included angle between the opening direction of the gas outlet and the vertical downward direction is more than or equal to zero degrees and less than 180 degrees.
According to one embodiment of the invention, the arc-shaped section is in an inverted U shape, and the opening direction of the air outlet is vertically downward.
According to one embodiment of the invention, the stripping pipes are a plurality of and are arranged at intervals in the horizontal plane.
According to one embodiment of the present invention, the anaerobic fermentation reaction apparatus further comprises: the precipitation separator is arranged in the anaerobic reaction chamber and is positioned above the gas stripping pipe, and is provided with a separator water outlet connected with the water outlet and is connected with the water inlet of the wastewater dephosphorization reaction device.
According to one embodiment of the invention, the precipitation separator comprises: the device comprises a box body, wherein a degassing and sedimentation cavity is formed in the box body, a sludge outlet is formed in the bottom of the degassing and sedimentation cavity, and the cross-sectional area of the lower part of the degassing and sedimentation cavity is gradually reduced along the direction from top to bottom; the separator is arranged at the upper part of the degassing and settling cavity, the separator divides the upper part of the degassing and settling cavity into a degassing zone and a settling zone, and the bottom of the degassing zone is communicated with the bottom of the settling zone so that wastewater overflows from the anaerobic reaction chamber into the degassing zone and flows into the settling zone from the bottom of the degassing zone; a sedimentation inclined plate which is arranged in the sedimentation zone; and the overflow weir is arranged in the sedimentation zone and forms an overflow groove with the water outlet of the separator.
According to one embodiment of the invention, the upper edge of the tank portion defining the degassing zone with the partition is lower than the upper edge of the partition and the upper edge of the tank portion defining the sedimentation zone with the partition.
According to one embodiment of the present invention, the case is a rectangular parallelepiped, a lower end of a first longitudinal side wall of a lower portion of the case extends downward beyond a lower end of a second longitudinal side wall of the lower portion of the case, and the lower end of the first longitudinal side wall overlaps with the lower end of the second longitudinal side wall in an up-down direction.
According to one embodiment of the present invention, the anaerobic fermentation reaction apparatus further comprises: the sedimentation separator is arranged outside the anaerobic fermentation tank body, the water outlet is connected with the wastewater dephosphorization reaction device through the sedimentation separator, and the sedimentation separator comprises: the device comprises a box body, wherein a degassing and precipitating cavity is formed in the box body, the degassing and precipitating cavity is provided with an inlet, a separator water outlet and a sludge outlet, the inlet is communicated with the water outlet, the separator water outlet is connected with the wastewater dephosphorization reaction device, the lower part of the degassing and precipitating cavity is formed into at least one conical cavity with the cross-sectional area gradually decreasing along the direction from top to bottom, and the sludge outlet is formed at the bottom of the conical cavity; the sedimentation inclined plate is arranged in the degassing and sedimentation cavity; the overflow weir is arranged in the degassing and settling cavity, and an overflow groove communicated with the water outlet of the separator is formed in the overflow weir.
According to one embodiment of the present invention, the anaerobic fermentation reaction apparatus further comprises: the energy dissipater is connected between the water outlet of the anaerobic reaction chamber and the inlet of the degassing and precipitating cavity.
According to one embodiment of the present invention, the anaerobic fermentation reaction apparatus further comprises: the sludge return pipe is used for returning the sludge discharged from the sludge outlet into the anaerobic reaction chamber, one end of the sludge return pipe is communicated with the anaerobic reaction chamber, the sludge outlet is connected with the sludge return pipe through a sludge discharge pipe, and a sludge return pump is arranged on the sludge return pipe.
According to one embodiment of the present invention, the anaerobic fermentation reaction apparatus further comprises: the anaerobic fermentation tank comprises a water sealed tank body, wherein a safety air port is arranged at the top of the anaerobic fermentation tank body, and the safety air port is connected with the water sealed tank.
According to one embodiment of the invention, the aeration device has a plurality of aeration heads or aeration tubes arranged at intervals.
According to one embodiment of the present invention, the wastewater dephosphorization reaction apparatus further comprises: the upper end and the lower end of each guide cylinder are open, and a plurality of aeration heads or aeration pipes extend into a plurality of guide cylinders from the lower ends of the guide cylinders respectively.
According to one embodiment of the present invention, the wastewater dephosphorization reaction apparatus further comprises: the water distributor is arranged in the dephosphorization reaction chamber and positioned below the aeration device, and the water distributor is connected with the water inlet.
According to one embodiment of the invention, the water distributor is provided with a plurality of water distribution openings which are arranged at intervals and are downward in opening.
According to one embodiment of the invention, the dephosphorization reaction chamber is provided with a discharge hole positioned at the lower part of the dephosphorization reaction tank body.
According to one embodiment of the present invention, the wastewater dephosphorization reaction apparatus further comprises: the cyclone is provided with a cyclone inlet, a mud outlet and a cyclone outlet, wherein the cyclone inlet is communicated with the discharge port, and the cyclone outlet is connected with the dephosphorization reaction chamber through a water return pipe.
According to one embodiment of the present invention, the wastewater dephosphorization reaction apparatus further comprises: the device comprises a pump and a desliming device connected with the pump, wherein clear liquid after sludge is removed by the desliming device is returned to the dephosphorization reaction chamber.
According to one embodiment of the present invention, the wastewater dephosphorization reaction apparatus further comprises: and the clear liquid after being precipitated by the precipitation device is returned to the dephosphorization reaction chamber.
According to one embodiment of the invention, the degassing precipitation separator comprises: the separator body is internally provided with a degassing and precipitating chamber, the bottom of the degassing and precipitating chamber is provided with a sludge discharge port, and the cross-sectional area of the lower part of the degassing and precipitating chamber is gradually reduced along the direction from top to bottom; the baffle plate is arranged at the upper part of the degassing and precipitating chamber, the baffle plate divides the upper part of the degassing and precipitating chamber into a degassing cavity and a precipitating cavity, and the bottom of the degassing cavity is communicated with the bottom of the precipitating cavity so that wastewater overflows from the dephosphorization reaction chamber into the degassing cavity and flows into the precipitating cavity from the bottom of the degassing cavity; the inclined sedimentation plate or the inclined sedimentation pipe is arranged in the sedimentation cavity; the effluent overflow weir is arranged in the sedimentation cavity and forms an effluent overflow groove with a separation outlet communicated with the denitrification reactor.
According to one embodiment of the invention, the upper edge of the separator body portion defining the degassing chamber with the baffle is lower than the upper edge of the baffle and the upper edge of the separator body portion defining the sedimentation chamber with the baffle.
According to one embodiment of the invention, the separator body is rectangular in cross section.
According to one embodiment of the invention, the lower end of the first longitudinal side wall of the lower part of the separator body extends downwards beyond the lower end of the second longitudinal side wall of the lower part of the separator body, and the lower end of the first longitudinal side wall overlaps with the lower end of the second longitudinal side wall in the up-down direction.
According to one embodiment of the present invention, the wastewater dephosphorization reaction apparatus further comprises: an aeration pump or an aeration fan which is arranged outside the dephosphorization reaction tank body and connected with the aeration device, and the water inlet is connected with a wastewater control valve.
According to one embodiment of the invention, a top cover is arranged at the top of the dephosphorization reaction tank body, and the dephosphorization agent adding port is arranged on the top cover.
According to one embodiment of the present invention, the denitrification reactor includes an anaerobic ammonia oxidation reactor and an anoxic-aerobic reaction tank connected to each other.
According to one embodiment of the invention, the wastewater treatment system further comprises a coagulation reaction device, wherein the coagulation reaction device is connected between the denitrification reactor and the advanced treatment system, and the coagulation reaction device is provided with a coagulation tank, a flocculation tank and a sedimentation tank which are sequentially communicated along the wastewater treatment process direction.
According to one embodiment of the invention, the advanced treatment system comprises a plurality of groups of Fenton reaction devices which are sequentially connected along the wastewater treatment process direction, and each group of Fenton reaction devices comprises a Fenton reaction tank and a Fenton sedimentation tank.
According to one embodiment of the invention, a plurality of Fenton reaction chambers and Fenton flocculation chambers which are sequentially communicated along the wastewater treatment process direction are arranged in each Fenton reaction chamber, a Fenton fast stirrer is arranged in each Fenton reaction chamber, a Fenton slow stirrer is arranged in each Fenton flocculation chamber, and a Fenton sloping plate precipitator and a Fenton mud scraper are arranged in each Fenton sedimentation tank.
According to one embodiment of the invention, the depth processing system further comprises: the sand filter is connected with the last Fenton sedimentation tank along the wastewater treatment process direction; and the air storage tank is connected with the sand filter.
According to one embodiment of the invention, the Fenton reaction tanks comprise a first-stage Fenton reaction tank and a second-stage Fenton reaction tank, the Fenton sedimentation tanks comprise a first-stage Fenton sedimentation tank and a second-stage Fenton sedimentation tank, and the first-stage Fenton reaction tank, the first-stage Fenton sedimentation tank, the second-stage Fenton reaction tank and the second-stage Fenton sedimentation tank are sequentially connected along the wastewater treatment process direction.
According to one embodiment of the invention, the depth processing system further comprises: a sulfuric acid storage tank connected to a first one of a plurality of Fenton reaction chambers of each Fenton reaction tank in the wastewater treatment process direction; a ferrous sulfate solution tank connected to a first one of a plurality of Fenton reaction chambers of each Fenton reaction tank in the wastewater treatment process direction; the hydrogen peroxide storage tank is connected with the first one of the Fenton reaction cavities of each Fenton reaction tank along the wastewater treatment process direction; and the Fenton flocculating agent tanks are connected with Fenton flocculating cavities of each Fenton reaction tank.
An embodiment according to a second aspect of the present invention proposes a method for treating wastewater from cellulose-made ethanol, the method comprising the steps of:
a: carrying out biodegradation on the wastewater in an anaerobic environment;
b: aerating and dephosphorizing the waste water after biodegradation;
c: denitrification is carried out on the wastewater after aeration and dephosphorization;
d: and (3) deeply treating the denitrified wastewater to further remove organic pollutants which cannot be biodegraded.
According to the method for treating the wastewater from ethanol preparation by cellulose, disclosed by the embodiment of the invention, the system structure can be simplified, the cost can be reduced, and the COD (chemical oxygen demand) and nitrogen and phosphorus treatment effect can be improved.
According to one embodiment of the invention, in said step a, compressed biogas flowing from bottom to top is fed to bring the wastewater and sludge into full contact.
According to one embodiment of the present invention, in the step a, the wastewater after biodegradation is subjected to degassing, precipitation and separation, and the wastewater after the degassing, precipitation and separation is subjected to the step B.
According to one embodiment of the present invention, in the step B, aeration is performed by introducing air, and magnesium oxide is added as a dephosphorizing agent.
According to an embodiment of the invention, said step C comprises the sub-steps of:
c1: anaerobic ammoxidation reaction is carried out on the wastewater after aeration and dephosphorization;
c2: carrying out denitrification reaction on the wastewater subjected to anaerobic ammoxidation reaction in an anoxic environment;
and C3: and (3) carrying out nitration reaction on the wastewater subjected to denitrification reaction in an aerobic environment.
According to one embodiment of the invention, after the step C, the denitrified wastewater is coagulated, and then the step D is performed.
According to an embodiment of the invention, said step D comprises the sub-steps of:
D1: carrying out a first-stage Fenton reaction on the denitrified wastewater;
d2: carrying out primary degassing, precipitation and separation on the wastewater subjected to the primary Fenton reaction;
d3: carrying out a secondary Fenton reaction on the wastewater after the primary degassing precipitation separation;
d4: carrying out secondary degassing precipitation separation on the wastewater after the secondary Fenton reaction;
d5: and (3) sand filtering the wastewater after the secondary degassing precipitation separation.
According to one embodiment of the present invention, sulfuric acid, ferrous sulfate and hydrogen peroxide are added to stir in the step D1 and the step D4, respectively, and then a flocculant is added to stir.
Drawings
Fig. 1 is a schematic structural view of a wastewater treatment system for producing ethanol from cellulose according to an embodiment of the present invention.
FIG. 2 is a schematic diagram of the anaerobic fermentation reaction apparatus of the wastewater treatment system for producing ethanol from cellulose according to an embodiment of the present invention.
Fig. 3 is a schematic structural view of a wastewater dephosphorization reaction apparatus of a wastewater treatment system for preparing ethanol from cellulose according to an embodiment of the present invention.
Fig. 4 is a schematic diagram of a structure of a degassing and precipitation separator of a wastewater dephosphorization reaction device of a wastewater treatment system for preparing ethanol from cellulose according to an embodiment of the present invention.
Fig. 5 is a schematic structural view of a wastewater treatment system for producing ethanol from cellulose according to a first alternative embodiment of the present invention.
FIG. 6 is a schematic structural view of an anaerobic fermentation reaction apparatus of a wastewater treatment system for producing ethanol from cellulose according to a first alternative embodiment of the present invention.
FIG. 7 is a schematic diagram showing the structure of a precipitation separator of an anaerobic fermentation reaction apparatus of a wastewater treatment system for producing ethanol from cellulose according to a first alternative embodiment of the present invention.
Fig. 8 is a schematic structural view of a wastewater treatment system for producing ethanol from cellulose according to a second alternative embodiment of the present invention.
FIG. 9 is a schematic structural view of an anaerobic fermentation reaction apparatus of a wastewater treatment system for producing ethanol from cellulose according to a second alternative embodiment of the present invention.
Fig. 10 is a schematic structural view of a wastewater treatment system for cellulose-made ethanol according to a third alternative embodiment of the present invention.
FIG. 11 is a schematic structural view of an anaerobic fermentation reaction apparatus of a wastewater treatment system for producing ethanol from cellulose according to a third alternative embodiment of the present invention.
Reference numerals:
a wastewater treatment system 1 for preparing ethanol from cellulose,
Anaerobic fermentation reaction device 10, wastewater dephosphorization reaction device 20, denitrification reactor 40, advanced treatment system 60,
Anaerobic fermentation tank 100, anaerobic reaction chamber 110, wastewater inlet 111, water outlet 112, gas outlet 113, safety gas outlet 114, sludge discharge outlet 115, sludge discharge valve and/or sludge discharge pump 116, feed pump 117, gas control valve 118,
The gas stripping tube 200, a straight tube section 210, a gas inlet 211, an arc section 220, a gas outlet 221,
A gas supply pipe 300,
A precipitation separator 400, a tank 410, a degassing and precipitation chamber 411, a sludge outlet 412, a separator water outlet 413, a first longitudinal side wall 414, a second longitudinal side wall 415, an inlet 416, a partition 420, a degassing zone 421, a precipitation zone 422, a precipitation sloping plate 430, an overflow weir 440, an overflow trough 441, a separation vessel,
500 parts of energy dissipater,
A sludge return pipe 600, a sludge return pump 610,
A sludge discharge pipe 700,
A water sealed tank 800,
A dephosphorization reaction tank 1100, a dephosphorization reaction chamber 1110, a water inlet 1111, a dephosphorization agent adding port 1112, a discharge port 1113, a wastewater control valve 1114, a top cover 1115, a discharge valve 1116,
Aeration device 1200, aeration head or aeration pipe 1210,
The degassing and settling separator 1300, the separator body 1310, the degassing and settling chamber 1311, the degassing chamber 1312, the settling chamber 1313, the sludge discharge port 1314, the first longitudinal side wall 1315, the second longitudinal side wall 1316, the baffle 1320, the inclined settling plate or pipe 1330, the effluent weir 1340, the effluent overflow launder 1341, the separation outlet 1342,
A guide cylinder 1400,
Water distributor 1500, water distribution port 1510,
Cyclone 1600, cyclone inlet 1610, mud outlet 1620, cyclone outlet 1630, return tube 1640,
An aeration pump or fan 1700,
Anaerobic ammoxidation reactor 2100, anoxic and aerobic reaction tank 2200,
Fenton reaction device 4100, primary Fenton reaction tank 4110, secondary Fenton reaction tank 4120, fenton reaction chamber 4111, fenton flocculation chamber 4112, fenton fast mixer 4113, fenton slow mixer 4114, primary Fenton sedimentation tank 4130, secondary Fenton sedimentation tank 4140, fenton sloping plate settler 4131, fenton mud scraper 4132, sand filter 4200, air reservoir 4300, sulfuric acid reservoir 4400, ferrous sulfate solution tank 4500, hydrogen peroxide reservoir 4600, fenton flocculant tank 4700.
Detailed Description
Embodiments of the present invention are described in detail below, examples of which are illustrated in the accompanying drawings, wherein like or similar reference numerals refer to like or similar elements or elements having like or similar functions throughout. The embodiments described below by referring to the drawings are illustrative and intended to explain the present invention and should not be construed as limiting the invention.
Along with the prohibition of the process method for preparing the ethanol by adopting corn and cassava (namely starch), the process method for preparing the ethanol by taking straw and stalk (cellulose) as raw materials is increasingly widely applied, but compared with the traditional process for preparing the ethanol by adopting starch by using cellulose, the COD in the wastewater is increased from 2 thousands to 3 thousands to 5 thousands to 9 thousands, and the difficulty of wastewater treatment is correspondingly increased.
The waste water treatment system for preparing ethanol from cellulose in the related art has the advantages that the COD treatment effect is limited, the COD in the waste water can not be treated to be less than 100mg/L, the procedures are complex, the system structure is complex, and the cost is high.
Specifically, for the wastewater treatment process of cellulose-to-ethanol, anaerobic fermentation purification is an essential process by which organic pollutants in wastewater are degraded by anaerobic organisms.
The existing anaerobic fermentation reaction device is generally provided with an air floatation structure, for example, a pipe body with open upper and lower ends is arranged in an anaerobic reaction chamber, a motor and a stirring element connected with the motor are arranged in the pipe body, the stirring element rotates under the drive of the motor and pushes water flow downwards so as to form downward water flow in the pipe body, and therefore, a mixture of wastewater and sludge in the anaerobic reaction chamber enters from the upper end of the pipe body and flows out from the lower end of an anaerobic fermentation tank body to form circulation.
In addition, the existing anaerobic fermentation reaction device is also generally provided with a flotation cell in the anaerobic reaction chamber, and the upper end and the lower end of the flotation cell are respectively provided with a cleaning element driven by a motor so as to prevent insoluble slurry from being discharged from the anaerobic fermentation reaction device.
The inventors of the present invention found through studies and experiments that the above anaerobic apparatuses each have some problems, limiting their applications.
For example, an anaerobic fermentation reaction device with an air floatation structure is small in stirring range and poor in stirring effect, the COD treatment effect is affected, and an anaerobic fermentation reaction device with a floatation cell is easy to block and affects the stability of COD treatment.
In addition, the present inventors have found that a high-load aeration process and a dephosphorization process are generally provided for a wastewater treatment process for producing ethanol from cellulose, and in a conventional wastewater treatment system for producing ethanol from cellulose, the high-load aeration process and the dephosphorization process are separately performed, and separate facilities are required for the high-load aeration process and the dephosphorization process, respectively, so that the processes are complicated, the system configuration is complicated, and the cost is high.
In addition, with the development of industrial and agricultural production and the improvement of the living standard of people, the discharge amount of nitrogen and phosphorus pollutants is dramatically increased. The eutrophication of water body caused by nitrogen and phosphorus pollution is serious, and the water bloom and the offshore red tide of the lake occur more and more violently. The eutrophication of water body endangers many industries such as agriculture, fishery, travel industry and the like, and also forms a great threat to drinking water sanitation and food safety. The economic and effective control of nitrogen and phosphorus pollution has become a major environmental protection problem to be solved urgently. Struvite has a molecular formula of MgNH4PO4 & 6H2O, is a white crystal which is difficult to dissolve in water, and has a solubility product of 2.5X10-13 in water at normal temperature. By adding chemical reagent, ammonia and phosphate in the wastewater can form struvite, so that nitrogen and phosphorus pollutants can be removed simultaneously. In addition, the struvite contains two nutrient elements of nitrogen and phosphorus, and is a good slow release fertilizer.
The struvite has very low solubility in water and alkali, and the method for forming struvite is used for removing ammonia nitrogen and phosphate in wastewater, so that the method has the characteristics of high efficiency, simplicity and convenience. Such as starch industrial wastewater, livestock and poultry raising wastewater, landfill leachate and the like, contain high-concentration ammonia nitrogen, are difficult to directly carry out biological treatment, and are usually treated by a physical and chemical method (such as a stripping method) in advance. The stripping method requires pH to be more than 10, has low efficiency (not more than 50 percent) and is easy to cause secondary pollution. If the guanite precipitation method is used for treatment, the requirement on the pH condition can be reduced compared with the stripping method, and the efficiency is higher. According to the experiment of Tu nay et al on leather-making waste water, under the condition of pH value of 8-9, adopting struvite dephosphorization method can make the NH4+ removing rate be up to above 75%. Li et al adopts a struvite precipitation method, the concentration of the initial ammonia nitrogen is reduced to 210mg/l within 15 minutes, and the removal rate is over 96 percent. While the pH is controlled to be between 8.5 and 9. In the experiment of Chimenos et al on dye wastewater with initial concentration of NH4 < + > -N of 2320mg/l, the removal rate of NH4 < + > -N is also over 90 percent.
Phosphorus serves on the one hand as a key factor causing eutrophication and on the other hand is a very valuable mineral resource. The world has ascertained that the phosphorus reserves are only enough for human use for 100 years. Since struvite can be directly used as fertilizer, it is considered as one of the most promising phosphorus recovery paths, and the second international academy of phosphorus recovery conference is also an special topic for this purpose, and research on phosphorus recovery from sewage is being conducted. The supernatant of the anaerobic digestion sludge contains high concentration of NH4+ -N and PO 43-P, and is suitable for treatment by a struvite precipitation method. As long as a small amount of Mg2+ is added, the solubility product of various ions in the wastewater can reach a supersaturated state, and struvite precipitation is formed. And because of the lower SS, the produced struvite has higher purity. Mg (OH) 2 and NaOH are added into the sludge digestion liquid in a molar ratio of 1:1 to increase the pH, so that struvite is precipitated in a fluidized bed in the form of small particles. The phosphorus recovery device can realize 90% of soluble phosphate recovery at present, and ensure that biological phosphorus removal runs up to standard. In actual wastewater treatment, struvite precipitation has various limiting factors. First, many wastewater streams have high concentrations of nitrogen and phosphorus, but the ratio of these to each other does not meet the requirements of struvite precipitation. In this case, the addition of certain ions may increase the precipitation efficiency, but may increase the processing cost. And nitrogen and phosphorus are control targets of wastewater treatment, and secondary pollution can be caused by excessive addition. The addition of excess mg2+ is necessary for struvite precipitation, and therefore, inexpensive additives are critical to the practical application of struvite precipitation. Mg (OH) 2 is a relatively desirable Mg2+ additive, which increases both the Mg2+ content and the pH. Mg (OH) 2 slurries have been used in practical production.
In actual wastewater treatment, the wastewater often contains organic pollutants besides nitrogen and phosphorus pollutants, and if the pollutants are not removed, part of the organic pollutants can be entrained in struvite after the struvite process is adopted, so that the purity and the value of the struvite are reduced, and secondary pollution is caused.
In summary, it is important to develop a reaction device capable of simultaneously removing organic pollutants, nitrogen and phosphorus in water for practical wastewater. Under the guidance of the thought, the inventor of the application proposes a dephosphorization reaction device which is used for simultaneously removing ammonia nitrogen (NH 4 < + >), phosphate (PO 43 < + >) and COD from wastewater, and can also recycle struvite as phosphate fertilizer when treating the wastewater.
In consideration of the technical condition of cellulose-made ethanol wastewater treatment in the related art, the invention provides the cellulose-made ethanol wastewater treatment system 1 which has the advantages of simple structure, low cost and good COD (chemical oxygen demand) and nitrogen and phosphorus treatment effects.
A wastewater treatment system 1 for producing ethanol from cellulose according to an embodiment of the present invention will be described below with reference to the accompanying drawings.
As shown in fig. 1 to 11, the wastewater treatment system 1 for preparing ethanol from cellulose according to an embodiment of the present invention includes an anaerobic fermentation reaction device 10, a wastewater dephosphorization reaction device 20, a denitrification reactor 40, and a deep treatment system 60.
The anaerobic fermentation reaction device 10, the wastewater dephosphorization reaction device 20, the denitrification reactor 40 and the advanced treatment system 60 are sequentially connected along the wastewater treatment process direction.
The anaerobic fermentation reaction device 10 comprises an anaerobic fermentation tank body 100, a gas stripping pipe 200 and a gas supply pipe 300. Anaerobic reaction chamber 110 is provided in anaerobic fermentation tank 100, and anaerobic reaction chamber 110 has wastewater inlet 111, water outlet 112 and exhaust port 113. The gas stripping tube 200 is provided in the anaerobic reaction chamber 110, the upper end of the gas stripping tube 200 has a gas outlet 221, and the lower end of the gas stripping tube 200 has a gas inlet 211. The gas supply pipe 300 is connected to the gas inlet 211 of the gas stripping pipe 200 for supplying gas for stripping into the gas stripping pipe 200. The gas used for stripping may be an anoxic gas or an inert gas, preferably biogas.
The wastewater dephosphorization reaction apparatus 20 includes a dephosphorization reaction tank 1100, an aeration apparatus 1200, and a degassing and precipitation separator 1300. The dephosphorization reaction tank 1100 has a dephosphorization reaction chamber 1110, and the dephosphorization reaction chamber 1110 has a water inlet 1111 and a dephosphorization agent adding port 1112. The aeration device 1200 is disposed within the dephosphorization reaction chamber 1110. The degassing and precipitation separator 1300 is provided in the dephosphorization reaction chamber 1110, and the degassing and precipitation separator 1300 is positioned above the aeration device 1200, and the degassing and precipitation separator 1300 is used for separating gas, water and sludge.
As will be understood by those skilled in the art, the wastewater treatment process direction means the flow direction of wastewater from the first process to the last process in the sequence of the respective processes in the whole process of wastewater treatment, that is, the direction of "anaerobic fermentation reaction apparatus 10→wastewater dephosphorization reaction apparatus 20→denitrification reactor 40→advanced treatment system 60".
The wastewater treatment process of the cellulose-to-ethanol wastewater treatment system 1 according to the embodiment of the present invention is described below with reference to the accompanying drawings.
Waste water enters the anaerobic reaction chamber 110 through the waste water inlet 111, the air supply pipe 300 supplies air to the air stripping pipe 200, an anaerobic environment is formed in the anaerobic reaction chamber 110, meanwhile, the air stripping pipe 200 plays a role of stirring the waste water and the anaerobic sludge by outputting lifting air into the anaerobic reaction chamber 110, the waste water in the anaerobic reaction chamber 110 is rapidly mixed with the anaerobic sludge, the waste water is in intense contact with the anaerobic sludge to degrade organic pollutants in the waste water, redundant air in the anaerobic reaction chamber 110 is discharged through the air outlet 113, waste water after anaerobic fermentation purification flows out of the anaerobic reaction chamber 110 through the water outlet 112 and enters the dephosphorization reaction chamber 1110 through the water inlet 1111, a dephosphorization agent (such as magnesium oxide) is added into the dephosphorization reaction chamber 1110 through the dephosphorization agent adding port 1112, the aeration device 1200 supplies oxygen into the dephosphorization reaction chamber 1110, an aerobic environment is formed in the dephosphorization reaction chamber 1110, meanwhile, air supplied from the aeration device 1200 plays a role in stirring wastewater, so that the wastewater in the dephosphorization reaction chamber 1110 is rapidly mixed with aerobic sludge and a dephosphorization agent, biochemical organic matters in a colloid state of solubility in the wastewater are removed, dephosphorization is carried out, the wastewater after reaction overflows into the degassing and precipitation separator 1300, gas, water and aerobic sludge are separated, the separated gas is discharged from the top of the dephosphorization reaction chamber 1110, then water is separated from the aerobic sludge, the separated aerobic sludge is returned from the degassing and precipitation separator 1300 to the dephosphorization reaction chamber 1110 for recycling, the separated water overflows out of the degassing and precipitation separator 1300 with the aerobic sludge, the dephosphorization reaction chamber 1110 is discharged, the denitrification reaction chamber 40 is fed with the denitrified wastewater for denitrification, and the denitrified wastewater enters the advanced treatment system 60 for further removing organic pollutants which cannot be biodegraded in the wastewater.
According to the wastewater treatment system 1 for preparing ethanol from cellulose, disclosed by the embodiment of the invention, COD (chemical oxygen demand) in the wastewater from preparing ethanol from cellulose can be treated to be less than 100mg/L by arranging the anaerobic fermentation reaction device 10, the wastewater dephosphorization reaction device 20, the denitrification reactor 40 and the advanced treatment system 60 which are sequentially connected along the wastewater treatment process direction.
Further, by providing the gas stripping tube 200 and the gas feeding tube 300 in the anaerobic fermentation reaction apparatus 10, the gas can be fed into the gas stripping tube 200 by the gas feeding tube 300, and the gas can be fed into the anaerobic reaction chamber 110 by the gas stripping tube 200 to be stripped, and the gas fed from the gas stripping tube 200 can stir the mixture of the wastewater and the anaerobic sludge in the anaerobic reaction chamber 110, so that the wastewater and the anaerobic sludge can be sufficiently and rapidly contacted, and the stirring range is wide, the stirring effect is good, and the COD treatment effect can be greatly improved. On the other hand, by arranging the air stripping pipe 200, the air flotation structure and a motor and a stirring element which are required to be equipped for the air flotation structure can be eliminated, the structure of the anaerobic fermentation reaction device 10 is simplified, and the cost of the anaerobic fermentation reaction device 10 is reduced. In addition, the anaerobic fermentation reaction device 10 according to the embodiment of the present invention eliminates a flotation cell and a motor and a cleaning element which are required to be equipped for the flotation cell, further simplifies the structure of the anaerobic fermentation reaction device 10, and further reduces the cost of the anaerobic fermentation reaction device 10.
In addition, by providing the dephosphorizing agent adding port 1112 on the dephosphorizing reaction tank 1100 and providing the aeration device 1200 in the dephosphorizing reaction chamber 1110, aeration and dephosphorizing functions are integrated, thereby being capable of replacing the equipment required by each of the high-load aeration process and the dephosphorizing process in the cellulose-made ethanol wastewater treatment system, thereby simplifying the structure of the cellulose-made ethanol wastewater treatment system, reducing the cost of the cellulose-made ethanol wastewater treatment system, and having good COD treatment effect.
The wastewater treatment system 1 for preparing ethanol from cellulose has the advantages of simple structure, low cost, good COD treatment effect and the like.
A wastewater treatment system 1 for producing ethanol from cellulose according to an embodiment of the present invention will be described below with reference to the accompanying drawings.
As shown in fig. 1 to 11, the wastewater treatment system 1 for preparing ethanol from cellulose according to an embodiment of the present invention includes an anaerobic fermentation reaction device 10, a wastewater dephosphorization reaction device 20, a denitrification reactor 40, and a deep treatment system 60, which are sequentially connected in a wastewater treatment direction.
Advantageously, as shown in fig. 2, 6, 9 and 11, the lower end of the gas stripping tube 200 is adjacent to the bottom of the anaerobic reaction chamber 110, and the upper end of the gas stripping tube 200 extends to the upper portion of the anaerobic reaction chamber 110, and the water outlet 112 is provided at the upper portion of the anaerobic reaction chamber 110 and higher than the upper end of the gas stripping tube 200. The gas supplied from the gas supply pipe 300 is transferred from the bottom of the anaerobic reaction chamber 110 to the upper portion of the anaerobic reaction chamber 110 through the gas stripping pipe 200 and is outputted from the gas outlet 221 to agitate the mixture of wastewater and anaerobic sludge in the anaerobic reaction chamber 110, whereby not only can the gas supply pipe 300 be facilitated to supply the gas into the gas stripping pipe 200, but also the agitating range and agitating effect of the gas stripping pipe 200 can be further improved, and the gas outputted from the gas stripping pipe 200 does not interfere with the water outputted from the water outlet 112.
Alternatively, as shown in fig. 2, 6, 9 and 11, the upper end surface of the gas stripping tube 200 is opened to form the gas outlet 221, and the lower end surface of the gas stripping tube 200 is opened to form the gas inlet 211, so that the effective flow area of the gas inlet 211 and the gas outlet 221 can be maximized, thereby improving the output quantity of gas per unit time of the gas stripping tube 200.
In some embodiments according to the present invention, as shown in fig. 2, 6, 9 and 11, the stripping tube 200 includes a straight tube section 210 and an arcuate section 220. The straight pipe section 210 extends in the vertical direction, the arc-shaped section 220 is connected with the upper end of the straight pipe section 210, and an included angle alpha between the opening direction of the air outlet 221 and the vertical downward direction is greater than or equal to zero degrees and less than 180 degrees, namely 0 degrees is less than or equal to alpha less than 180 degrees.
Preferably, as shown in fig. 6 and 11, the arc-shaped section 220 is of an inverted U shape, and the opening direction of the air outlet 221 is vertically downward, in other words, α=0°. The gas outputted from the gas stripping pipe 200 thus agitates the mixture of wastewater and anaerobic sludge downward from the upper portion of the anaerobic reaction chamber 110, further enhancing the agitation range and the agitation effect, and further enhancing the COD treatment effect of the anaerobic fermentation reaction apparatus 10.
In order to further increase the intensity and speed of mixing wastewater with anaerobic sludge, the number of the gas stripping pipes 200 may be plural, one or more gas feeding pipes 300 may be horizontally disposed at the bottom of the anaerobic reaction chamber 110, and the plurality of gas stripping pipes 200 may be spaced apart in a horizontal plane and connected at lower ends thereof to the same gas feeding pipe 300 or respectively connected to the plurality of gas feeding pipes 300.
In some specific examples of the present invention, as shown in fig. 6, the anaerobic fermentation reaction apparatus 10 further includes a precipitation separator 400, the precipitation separator 400 being disposed in the anaerobic reaction chamber 110 and above the gas stripping tube 200, the precipitation separator 400 having a separator water outlet 413 connected to the water outlet 112, the water outlet 112 being connected to the water inlet 1111 of the wastewater dephosphorization reaction apparatus 20. The wastewater after anaerobic fermentation purification overflows into the precipitation separator 400, thereby separating gas from water and anaerobic sludge, the separated gas is discharged from the gas outlet 113, then the water is separated from the anaerobic sludge, the separated anaerobic sludge is returned from the precipitation separator 400 to the anaerobic reaction chamber 110 for recycling, the separated water separator water outlet 413 is conveyed to the water outlet 112, and the wastewater is discharged from the anaerobic reaction chamber 110 and conveyed to the wastewater dephosphorization reaction device 20.
Thus, the gas, water and anaerobic sludge can be separated in the anaerobic reaction chamber 110 by the precipitation separator 400, and then the separated products are respectively conveyed to different areas, so that the purity of the effluent is improved.
Specifically, as shown in fig. 7, the precipitation separator 400 includes a tank 410, a partition 420, a precipitation inclined plate 430, and an overflow weir 440.
A degassing and settling chamber 411 is formed in the case 410, a sludge outlet 412 is formed at the bottom of the degassing and settling chamber 411, and the cross-sectional area of the lower portion of the degassing and settling chamber 411 is gradually reduced in a direction from top to bottom. A partition 420 is provided at an upper portion of the degassing and settling chamber 411, the partition 420 dividing the upper portion of the degassing and settling chamber 411 into a degassing zone 421 and a settling zone 422, the bottom of the degassing zone 421 communicating with the bottom of the settling zone 422 so that wastewater overflows from the anaerobic reaction chamber 110 into the degassing zone 421 and flows from the bottom of the degassing zone 421 into the settling zone 422. A settling swash plate 430 is provided in the settling zone 422. Weir 440 is disposed within settling zone 422 and weir 440 forms isopipe 441 having separator outlet 413.
The separation process of the sedimentation separator 400 for water, gas and anaerobic sludge is described below with reference to fig. 7.
The water degraded by the anaerobic sludge is entrained with gas and anaerobic sludge, the water with the entrained gas and anaerobic sludge overflows to the degassing area 421 of the degassing and settling cavity 411, wherein the gas escapes from the degassing area 421 and is discharged from the exhaust port 113, and gas separation is completed. The water with the anaerobic sludge after being separated from the gas flows from the bottom of the degassing area 421 to the sedimentation area 422, at this time, the anaerobic sludge is settled and is guided by the inclined inner wall at the lower part of the degassing sedimentation cavity 411 to the sludge outlet 412, the sludge outlet 412 discharges the sedimentation separator 400 to enter the anaerobic reaction chamber 110 for continuous wastewater degradation, the water separated from the anaerobic sludge in the degassing sedimentation cavity 411 overflows to the overflow groove 441 of the overflow weir 440, and is discharged from the separator water outlet 413 and the water outlet 112 to the anaerobic reaction chamber 110 for subsequent treatment. In the process of rising the anaerobic sludge and the water, the anaerobic sludge is settled on the settling sloping plate 430 and slides to the bottom of the degassing and settling cavity 411, so that the separation of the anaerobic sludge and the water is facilitated, and the separation of the water, the anaerobic sludge and the gas is completed.
Advantageously, as shown in fig. 7, the upper edge of the tank 410 defining the degassing zone 421 with the partition 420 is lower than the upper edge of the partition 420 and the upper edge of the portion of the tank 410 defining the sedimentation zone 422 with the partition 420. In other words, the upper edge of the portion of the case 410 defining the degassing zone 421 is lower than the upper edge of the portion of the case 410 defining the settling zone 422 and lower than the upper edge of the partition 420. The upper edge of the overflow weir 440 may be flush with or higher than the upper edge of the portion of the tank 410 defining the degassing zone 421, and the upper edge of the overflow weir 440 is lower than the upper edge of the portion of the tank 410 defining the settling zone 422 and the upper edge of the partition 420. Therefore, water in the degassing zone 421 can be prevented from overflowing to the sedimentation zone 422 from the upper part, the water in the degassing zone 421 is ensured to flow from the bottom of the degassing zone 421 to the sedimentation zone 422, and further anaerobic sludge is fully separated, and water in the sedimentation zone 422 overflows into the overflow groove 441, so that anaerobic sludge is prevented from being entrained in water in the overflow groove 441.
Alternatively, as shown in fig. 7, the case 410 is a rectangular parallelepiped, the lower end of the first longitudinal side wall 414 of the lower portion of the case 410 extends downward beyond the lower end of the second longitudinal side wall 415 of the lower portion of the case 410, and the lower end of the first longitudinal side wall 414 overlaps the lower end of the second longitudinal side wall 415 in the up-down direction. Thereby, it is advantageously avoided that anaerobic sludge in the anaerobic reaction chamber 110 enters the degassing and settling chamber 411 of the settling separator 400 through the sludge outlet 412.
For example, among the four longitudinal side walls of the case 410, two longitudinal side walls having a longer length in the horizontal direction are a first longitudinal side wall 414 and a second longitudinal side wall 415, respectively, the lower ends of the first longitudinal side wall 414 and the second longitudinal side wall 415 are adjacent to each other with respect to the upper ends of the first longitudinal side wall 414 and the second longitudinal side wall 415, the lower end of the first longitudinal side wall 414 is located below the lower end of the second longitudinal side wall 415, and projections of the lower ends of the first longitudinal side wall 414 and the lower end of the second longitudinal side wall 415 in the horizontal plane overlap, and a gap between the lower ends of the first longitudinal side wall 414 and the lower end of the second longitudinal side wall 415 constitutes a sludge outlet 412, whereby on one hand, it can be ensured that anaerobic sludge in the degassing and settling chamber 411 can smoothly return to the anaerobic reaction chamber 110 through the sludge outlet 412 after settling, and on the other hand, the structure of the sludge outlet 412 can block anaerobic sludge in the anaerobic reaction chamber 110 from entering the degassing and settling chamber 411 from the sludge outlet 412, ensuring the anaerobic sludge separation effect of the settling separator 400.
In some embodiments of the present invention, as shown in fig. 9 and 11, the anaerobic fermentation reaction apparatus 10 further includes a precipitation separator 400, the precipitation separator 400 is disposed outside the anaerobic fermentation tank body 100, and the water outlet 112 is connected to the water inlet 1111 of the wastewater dephosphorization reaction apparatus 20 through the precipitation separator 400. The precipitation separator 400 includes a tank 410, a precipitation inclined plate 430, and an overflow weir 440.
The degassing and settling chamber 411 is formed in the box 410, the degassing and settling chamber 411 is provided with an inlet 416, a separator water outlet 413 and a sludge outlet 412, the inlet 416 is communicated with the water outlet 112 of the anaerobic reaction chamber 110, the separator water outlet 413 is connected with the water inlet 1111 of the wastewater dephosphorization reaction device 20, at least one conical chamber is formed at the lower part of the degassing and settling chamber 411, the cross-sectional area of each conical chamber is gradually reduced along the direction from top to bottom, and the sludge outlet 412 is formed at the bottom of the conical chamber. A settling inclined plate 430 is provided in the degassing settling chamber 411. Weir 440 is provided in degassing settling chamber 411, and weir 440 is formed in weir 440 to communicate with separator outlet 413.
The separation process of the sedimentation separator 400 for water, gas and anaerobic sludge is described below with reference to fig. 9 and 11.
The water flowing out of the water outlet 112 of the anaerobic reaction chamber 110 carries gas and anaerobic sludge, the water carrying the gas and the anaerobic sludge enters the degassing and settling chamber 411 through the inlet 416, wherein the gas escapes from above the liquid surface and is discharged out of the degassing and settling chamber 411, and gas separation is completed. The water separated from the gas entrains the anaerobic sludge, wherein the anaerobic sludge is settled and is guided by the inner wall of the conical cavity at the lower part of the degassing and settling cavity 411 to the sludge outlet 412, the degassing and settling cavity 411 is discharged from the sludge outlet 412, the water separated from the anaerobic sludge in the degassing and settling cavity 411 overflows into the overflow groove 441 of the overflow weir 440, and the degassing and settling cavity 411 is discharged from the separator water outlet 413 for subsequent treatment. In the process of rising the anaerobic sludge and the water, the anaerobic sludge is settled on the settling sloping plate 430 and slides to the conical cavity at the bottom of the degassing settling cavity 411, so that the separation of the anaerobic sludge and the water is facilitated, and the separation of the water, the anaerobic sludge and the gas is completed.
Thus, the gas, water and anaerobic sludge can be separated out of the anaerobic reaction chamber 110 by the precipitation separator 400, and then the separated products are respectively conveyed to different areas, so that the purity of the effluent is improved.
Further, as shown in fig. 9 and 11, the anaerobic fermentation reaction apparatus 10 further includes an energy dissipater 500, and the energy dissipater 500 is connected between the water outlet 112 of the anaerobic reaction chamber 110 and the inlet 416 of the degassing and settling chamber 411. This can use the energy dissipater 500 to consume and dissipate the energy of the water flowing out of the anaerobic fermentation tank 100, preventing or reducing the scouring damage of the sediment separator 400 by the water flowing out of the anaerobic fermentation tank 100.
Advantageously, as shown in fig. 9 and 11, the anaerobic fermentation reaction apparatus 10 further comprises a sludge return pipe 600, one end of the sludge return pipe 600 is communicated with the anaerobic reaction chamber 110, a sludge outlet 412 of the degassing and settling chamber 411 is connected with the sludge return pipe 600 through a sludge outlet pipe 700, a sludge return pump 610 is arranged on the sludge return pipe 600, and anaerobic sludge discharged from the sludge outlet 412 can be returned to the anaerobic reaction chamber 110 through the sludge outlet pipe 700 and the sludge return pipe 800 in sequence, thereby being reused.
Alternatively, for the external precipitation separator 400, a hydrocyclone or an external flotation device may be used instead.
In some specific examples of the present invention, as shown in fig. 11, the anaerobic reaction chamber 110 has a sludge discharge port 115 at a lower portion thereof, and the sludge discharge port 115 is connected to a sludge discharge valve and/or a sludge discharge pump 116, and the excessive anaerobic sludge in the anaerobic reaction chamber 110 may be discharged out of the anaerobic reaction chamber 110 through the sludge discharge port 115.
Alternatively, as shown in fig. 9 and 11, a supply pump 117 is connected to the wastewater inlet 111 to control whether wastewater is supplied to the anaerobic reaction chamber 110 and the amount of wastewater supplied to the anaerobic reaction chamber 110. As shown in fig. 1 and 2, the gas supply pipe 300 is provided with a gas control valve 118 located outside the anaerobic reaction chamber 110 to control whether gas is supplied to the gas stripping pipe 200 and the amount of gas supplied to the gas stripping pipe 200.
Further, the water inlet pipe at the wastewater inlet 111 may be connected with a water distributor, or a water distribution hole is formed on the water inlet pipe.
Advantageously, as shown in fig. 2, 6, 9 and 11, the anaerobic fermentation reaction apparatus 10 further comprises a water sealed tank 800, and a safety gas port 114 is provided at the top of the anaerobic fermentation tank 100, and the safety gas port 114 is connected to the water sealed tank 800. Therefore, the water sealed tank 800 can be utilized to isolate air, maintain the pressure of the anaerobic reaction chamber 110, play a role in fire retarding, and play a certain role in purifying biogas.
Alternatively, a relief valve may be employed instead of the water sealed tank 800.
In some embodiments of the present invention, as shown in fig. 3, the wastewater dephosphorization reaction apparatus 20 further includes an aeration pump or fan 1700, the aeration pump or fan 1700 being disposed outside the dephosphorization reaction tank 1100 and being connected to the aeration apparatus 1200 to pump air to the aeration apparatus 1200. In some embodiments, aeration device 1200 is blast aeration and includes an aeration air pipe and an aeration pan or aeration tube mounted at the end of the aeration air pipe, the aeration pump or aeration blower 1700 delivering air through the aeration air pipe to the aeration pan or aeration tube, the aeration pan or aeration tube aerating the air into the dephosphorization reaction chamber 1110.
Alternatively, the aeration device 1200 may be a jet aeration device, in which case an aeration pump or an aeration fan 1700 provided outside the dephosphorization reaction tank 1100 is not required, and the jet aeration device sucks air into the dephosphorization reaction chamber 1110 using a jet hydraulic impact type air diffusion device, for example, a jet ejector provided in the dephosphorization reaction chamber 1110 is combined with a jet pump provided outside the dephosphorization reaction tank 1100.
Advantageously, as shown in fig. 3, a wastewater control valve 1114, which is located outside the dephosphorization reaction tank 1100, is connected to the water inlet 1111 to control whether wastewater is supplied to the dephosphorization reaction chamber 1110 and the amount of wastewater supplied to the dephosphorization reaction chamber 1110.
As shown in fig. 3, in order to facilitate the smooth feeding of the dephosphorizing agent into the dephosphorizing reaction chamber 1110 and to prevent other impurities from entering the dephosphorizing reaction chamber 1110, and to achieve the effect of reducing the heating energy consumption, a top cover 1115 is provided on the top of the dephosphorizing reaction tank 1100, and a dephosphorizing agent feeding port 1112 is provided on the top cover 1115.
In some embodiments of the present invention, as shown in fig. 3, the aeration device 1200 has a plurality of aeration heads or aeration pipes 1210, the plurality of aeration heads or aeration pipes 1210 are disposed at intervals in the dephosphorization reaction chamber 1110, and the aeration device 1200 uniformly aerates the dephosphorization reaction chamber 1110 through the plurality of aeration heads or aeration pipes 1210, thereby improving the uniform effect of oxygen supply and the uniform stirring effect of wastewater and aerobic sludge.
Further, as shown in fig. 3, the wastewater dephosphorization reaction apparatus 20 further comprises a plurality of guide cylinders 1400, the number of the guide cylinders 1400 corresponds to the number of aeration heads or aeration tubes 1210, the upper end and the lower end of each guide cylinder 1400 are open, and the plurality of aeration heads or aeration tubes 1210 extend into the plurality of guide cylinders 1400 from the lower ends of the plurality of guide cylinders 1400, respectively. Therefore, the plurality of guide cylinders 1400 can be utilized to play a role in guiding, so that the wastewater in the dephosphorization reaction chamber 1110 can be fully contacted with aerobic sludge, the aerobic sludge is in a suspension state, the contact degree of the wastewater and the aerobic sludge is improved, and the wastewater treatment efficiency is improved.
By combining with the design of a guide cylinder, mg (OH) 2 emulsion is added under the optimal reaction condition to generate magnesium ammonia phosphate (MgNH 4PO4.6H2O, commonly known as struvite) crystal. Under such circumstances, a portion of the COD may also be removed by dissolved oxygen in the wastewater, forming new biomass and carbon dioxide.
Optionally, as shown in fig. 3, the wastewater dephosphorization reaction device 20 further includes a water distributor 1500, the water distributor 1500 is disposed in the dephosphorization reaction chamber 1110 and is located below the aeration device 1200, the water distributor 1500 is connected to the water inlet 1111, and the water distributor 1500 has a plurality of water distribution ports 1510 that are spaced apart and open downward. Wastewater enters the water distributor 1500 from the water inlet 1111 and is uniformly dispersed into the dephosphorization reaction chamber 1110 from the plurality of water distribution ports 1510 of the water distributor 1500.
In some specific examples of the present invention, as shown in fig. 3, the wastewater dephosphorization reaction apparatus 20 further comprises a cyclone 1600, the dephosphorization reaction chamber 1110 has a discharge outlet 1113 located at the lower part of the dephosphorization reaction tank 1100, the cyclone 1600 has a cyclone inlet 1610, a sludge outlet 1620 and a cyclone outlet 1630, the cyclone inlet 1610 is communicated with the discharge outlet 1113, a discharge valve 1116 is connected between the cyclone inlet 1610 and the discharge outlet 1113, and the cyclone outlet 1630 is connected with the dephosphorization reaction chamber 1110 through a water return pipe 1640.
The liquid-solid mixture deposited at the bottom of the dephosphorization reaction chamber 1110 can enter the cyclone 1600 through the discharge hole 1113, the discharge valve 1116 and the cyclone inlet 1610 in sequence and be separated in the cyclone 1600, the separated water returns to the dephosphorization reaction chamber 1110 through the cyclone outlet 1630 and the water return pipe 1640 in sequence, and the separated solid (such as magnesium ammonium phosphate) is conveyed to the struvite pool through the mud outlet 1620 and can be used as fertilizer.
The cyclone is combined with the design of the cyclone to separate struvite crystals from activated sludge and water so as to improve the purity of struvite and apply the struvite as fertilizer.
Compared with the traditional dephosphorization device, the dephosphorization reaction device provided by the embodiment of the invention has lower cost compared with a ferric salt adding device, one set of dephosphorization reaction device has multiple purposes (ammonia nitrogen and COD removal), and the produced struvite does not cause secondary pollution, and also slowly releases high-quality fertilizers of N, P and Mg. Struvite particles are separated from the apparatus by means of cyclones, the quality of which meets for example the fertilizer related standards of the european union.
In some embodiments of the present invention, the wastewater dephosphorization reaction apparatus 20 further comprises a pump and a desliming apparatus connected to the pump, wherein the clear liquid after sludge removal of the desliming apparatus is returned to the dephosphorization reaction chamber 1110, thereby improving the utilization rate of the wastewater.
Alternatively, the desliming device may be replaced by a precipitation device, i.e., the wastewater dephosphorization reaction device 20 further comprises a pump and a precipitation device connected to the pump, wherein the supernatant after precipitation by the precipitation device is returned to the dephosphorization reaction chamber 1110.
In some specific examples of the invention, as shown in fig. 3 and 4. The degassing and settling separator 1300 includes a separator body 1310, a baffle 1320, an inclined settling plate or pipe 1330, and an effluent weir 1340.
A degassing settling chamber 1311 is formed in the separator body 1310, and a sludge discharge port 1314 is formed at the bottom of the degassing settling chamber 1311, and the cross-sectional area of the lower portion of the degassing settling chamber 1311 is gradually reduced in a direction from top to bottom. A baffle 1320 is provided at an upper portion of the degassing settling chamber 1311, the baffle 1320 dividing the upper portion of the degassing settling chamber 1311 into a degassing chamber 1312 and a settling chamber 1313, a bottom of the degassing chamber 1312 communicating with a bottom of the settling chamber 1313 so that wastewater overflows from the dephosphorization reaction chamber 1110 into the degassing chamber 1312 and flows from the bottom of the degassing chamber 1312 into the settling chamber 1313. An inclined settling plate or tube 1330 is provided within the settling chamber 1313. A effluent weir 1340 is provided within the settling chamber 1313 and the effluent weir 1340 forms an effluent overflow launder 1341 having a separation outlet 1342 in communication with the denitrification reactor 40.
The separation process of the deaeration and precipitation separator 1300 for water, gas and aerobic sludge is described below with reference to fig. 3 and 4.
The water degraded by the aerobic sludge is entrained with gas and aerobic sludge, the water with the entrained gas and the aerobic sludge overflows to a degassing cavity 1312 of a degassing and precipitating chamber 1311, wherein the gas escapes from the degassing cavity 1312 and is discharged from the top of a dephosphorization reaction chamber 1110, and gas separation is completed. The water with the aerobic sludge after being separated from the gas flows to a sedimentation chamber 1313 from the bottom of the degassing chamber 1312, at this time, the aerobic sludge is sedimented and is guided by the inclined inner wall at the lower part of the degassing sedimentation chamber 1311 to a sludge discharge port 1314, the sludge is discharged from the sludge discharge port 1314 to the degassing sedimentation separator 1300 to enter the dephosphorization reaction chamber 1110 for further wastewater degradation, and the water separated from the aerobic sludge in the degassing sedimentation chamber 1311 overflows into a water outlet overflow groove 1341 of a water outlet overflow weir 1340 and is discharged to the outside of the dephosphorization reaction chamber 1110 from a separation outlet 1342 for subsequent treatment. In the process of rising the aerobic sludge and water, the aerobic sludge is settled on an inclined sedimentation plate or an inclined sedimentation pipe 1330 and falls to the bottom of a degassing sedimentation chamber 1311, which is helpful for separating the aerobic sludge from the water, and thus, the separation of the water, the aerobic sludge and the gas is completed.
Advantageously, as shown in fig. 4, the upper edge of the separator body 1310 that defines the degassing cavity 1312 with the baffle 1320 is lower than the upper edge of the baffle 1320 and the upper edge of the portion of the separator body 1310 that defines the sedimentation cavity 1313 with the baffle 1320. In other words, the upper edge of the portion of the separator body 1310 that defines the degassing chamber 1312 is lower than the upper edge of the portion of the separator body 1310 that defines the settling chamber 1313 and lower than the upper edge of the baffle 1320. The upper edge of the effluent weir 1340 may be flush with or higher than the upper edge of the portion of the separator body 1310 defining the degassing cavity 1312 and the upper edge of the effluent weir 1340 is lower than the upper edge of the portion of the separator body 1310 defining the sedimentation cavity 1313 and the upper edge of the baffle 1320. Therefore, water in the degassing cavity 1312 can be prevented from overflowing to the sedimentation cavity 1313 from the upper side, the water in the degassing cavity 1312 is guaranteed to flow to the sedimentation cavity 1313 from the bottom of the degassing cavity 1312, aerobic sludge is further fully separated, and water in the sedimentation cavity 1313 overflows into the effluent overflow groove 1341, so that the entrainment of the aerobic sludge in the water in the effluent overflow groove 1341 is avoided.
Alternatively, as shown in fig. 4, the separator body 1310 has a rectangular cross section, for example, a rectangular parallelepiped shape, a lower end of the first longitudinal side wall 1315 of the lower portion of the separator body 1310 extends downward beyond a lower end of the second longitudinal side wall 1316 of the lower portion of the separator body 1310, and the lower end of the first longitudinal side wall 1315 overlaps with the lower end of the second longitudinal side wall 1316 in the up-down direction. Whereby the aerobic sludge in the dephosphorization reaction chamber 1110 is advantageously prevented from entering the degassing and settling chamber 1311 of the degassing and settling separator 1300 through the sludge discharge port 1314.
For example, among the four longitudinal side walls of the separator body 1310, two longitudinal side walls having a longer length in the horizontal direction are the first longitudinal side wall 1315 and the second longitudinal side wall 1316, respectively, the lower end of the first longitudinal side wall 1315 and the lower end of the second longitudinal side wall 1316 are adjacent to each other with respect to the upper end of the first longitudinal side wall 1315 and the upper end of the second longitudinal side wall 1316, the lower end of the first longitudinal side wall 1315 is located below the lower end of the second longitudinal side wall 1316, and projections of the lower end of the first longitudinal side wall 1315 and the lower end of the second longitudinal side wall 1316 in the horizontal plane overlap, and a gap between the lower end of the first longitudinal side wall 1315 and the lower end of the second longitudinal side wall 1316 constitutes a sewage sludge discharge port 1314, whereby on the one hand, it can be ensured that the aerobic sludge in the degassing and precipitating chamber 1311 can smoothly return to the dephosphorization reaction chamber 1110 through the sludge discharge port 1314, and on the other hand the structure of the sludge discharge port 1314 can block the aerobic sludge in the dephosphorization reaction chamber 1110 from entering the sludge discharge port 1314 into the aerobic precipitation chamber 1311, ensuring the aerobic sludge separation effect of the degassing separator 1300.
In some embodiments of the present invention, as shown in fig. 1, 5, 8 and 10, the denitrification reactor 40 includes an anaerobic ammonia oxidation reactor 2100 and an anoxic aerobic reaction tank 2200 connected in sequence in the wastewater treatment process direction. Wherein the anaerobic ammonia oxidation reactor 2100 is connected with the wastewater dephosphorization reaction device 20, the anoxic-aerobic reaction tank 2200 is connected with the advanced treatment system 60, and wastewater flowing out of the wastewater dephosphorization reaction device 20 sequentially flows through the anaerobic ammonia oxidation reactor 2100 and the anoxic-aerobic reaction tank 2200 for denitrification treatment.
In some specific examples of the present invention, the wastewater treatment system 1 for preparing ethanol from cellulose further comprises a coagulation reaction device, wherein the coagulation reaction device is connected between the denitrification reactor 40 and the advanced treatment system 60, the coagulation reaction device is provided with a coagulation tank, a flocculation tank and a sedimentation tank which are sequentially communicated along the wastewater treatment process direction, a coagulant is added into the coagulation tank, a flocculant is added into the flocculation tank, and the sedimentation tank is used for degassing, sedimentation and separation.
In some embodiments of the present invention, as shown in fig. 1, 5, 8 and 10, the advanced treatment system 60 includes a plurality of sets of Fenton reaction devices 4100 sequentially connected in the wastewater treatment process direction, each set of Fenton reaction devices 4100 including a Fenton reaction tank and a Fenton sedimentation tank. The wastewater exiting the denitrification reactor 40 passes through the Fenton reaction tank and the Fenton sedimentation tank of each Fenton reaction device 4100 to be subjected to Fenton oxidation so as to further remove the organic pollutants which cannot be biodegraded in the wastewater.
Specifically, as shown in fig. 1, 5, 8 and 10, each Fenton reaction tank is provided with a plurality of Fenton reaction chambers 4111 and Fenton flocculation chambers 4112 which are sequentially communicated along the wastewater treatment process direction, a Fenton fast stirrer 4113 is arranged in each Fenton reaction chamber 4111, and a Fenton slow stirrer 4114 is arranged in each Fenton flocculation chamber 4112. It should be appreciated here that the speed of Fenton fast mixer 4113 and Fenton slow mixer 4114 are relative, i.e., the speed of Fenton fast mixer 4113 and the speed of Fenton slow mixer 4114 are Gao Yufen. A Fenton sloping plate settler 4131 and a Fenton mud scraper 4132 are arranged in each Fenton sedimentation tank.
For example, the Fenton reaction tanks include a first Fenton reaction tank 4110 and a second Fenton reaction tank 4120, the Fenton sedimentation tanks include a first Fenton sedimentation tank 4130 and a second Fenton sedimentation tank 4140, and the first Fenton reaction tank 4110, the first Fenton sedimentation tank 4130, the second Fenton reaction tank 4120 and the second Fenton sedimentation tank 4140 are sequentially connected along the wastewater treatment process direction. Wherein, each of the first-stage Fenton reaction tank 4110 and the second-stage Fenton reaction tank 4120 is internally provided with three Fenton reaction chambers 4111 and one Fenton flocculation chamber 4112 which are sequentially communicated along the wastewater treatment process direction, the Fenton reaction chambers 4111 are respectively internally provided with a Fenton fast stirrer 4113, and the Fenton flocculation chamber 4112 is internally provided with a Fenton slow stirrer 4114. Fenton sloping plate precipitators 4131 and Fenton mud scrapers 4132 are respectively arranged in the first-stage Fenton sedimentation tank 4130 and the second-stage Fenton sedimentation tank 4140.
Further, as shown in fig. 1, 5, 8 and 10, the depth treatment system 60 further includes a sand filter 4200 and an air reservoir 4300. Sand filter 4200 is connected to the last of the Fenton settling tanks (e.g., secondary Fenton settling tank 4140) along the wastewater treatment process direction. The air reservoir 4300 is connected to a sand filter 4200. Water from the last Fenton sedimentation basin (e.g., second Fenton sedimentation basin 4140) in the wastewater treatment process direction enters the sand filter 4200, and the air reservoir 4300 supplies air to the sand filter 4200 to filter the water within the sand filter 4200, thereby improving the purity of the water from the deep treatment system 60.
Optionally, as shown in fig. 1, 5, 8 and 10, the advanced treatment system 60 further includes a sulfuric acid tank 4400, a ferrous sulfate solution tank 4500, a hydrogen peroxide tank 4600 and a Fenton flocculant tank 4700.
The sulfuric acid storage tank 4400 is connected to a first Fenton reaction chamber 4111 along the wastewater treatment process direction among the Fenton reaction chambers 4111 of each of the Fenton reaction tanks, namely, the sulfuric acid storage tank 4400 is connected to the first Fenton reaction chamber 4111 of the primary Fenton reaction tank 4110 and the first Fenton reaction chamber 4111 of the secondary Fenton reaction tank 4120 for providing sulfuric acid. The ferrous sulfate solution tank 4500 is connected to a first Fenton reaction chamber 4111 of the Fenton reaction chambers in the wastewater treatment process direction, that is, the ferrous sulfate solution tank 4500 is connected to the first Fenton reaction chamber 4111 of the first-stage Fenton reaction chamber 4110 and the first Fenton reaction chamber 4111 of the second-stage Fenton reaction chamber 4120, for providing ferrous sulfate. The hydrogen peroxide tank 4600 is connected to a first Fenton reaction chamber 4111 along the wastewater treatment process direction in each Fenton reaction chamber, that is, the hydrogen peroxide tank 4600 is connected to the first Fenton reaction chamber 4111 of the first-stage Fenton reaction chamber 4110 and the first Fenton reaction chamber 4111 of the second-stage Fenton reaction chamber 4120, and is used for providing hydrogen peroxide. A Fenton flocculant tank 4700 is connected to the Fenton flocculation chamber 4112 of each of the Fenton reaction tanks, i.e., the Fenton flocculant tank 4700 is connected to the Fenton flocculation chamber 4112 of the primary Fenton reaction tank 4110 and the Fenton flocculation chamber 4112 of the secondary Fenton reaction tank 4120 for providing flocculant.
The method for treating cellulosic ethanol wastewater according to an embodiment of the present invention will be described below with reference to the accompanying drawings in combination with the above-described cellulosic ethanol wastewater treatment system 1, and comprises the steps of:
a: the wastewater is fed to the anaerobic fermentation reaction apparatus 10, and the wastewater is biodegraded in an anaerobic environment.
B: the wastewater flowing out of the anaerobic fermentation reaction device 10 is conveyed to a wastewater dephosphorization reaction device 20, oxygen is supplied and aerated in the wastewater dephosphorization reaction device 20, and the wastewater after biodegradation is subjected to aerobic biodegradation and dephosphorization.
C: the wastewater discharged from the wastewater dephosphorization reaction apparatus 20 is fed to a denitrification reactor 40, and denitrification is performed on the wastewater in the denitrification reactor 40.
D: the wastewater discharged from the denitrification reactor 40 is fed to a deep treatment system 60, and the wastewater after dephosphorization is deeply treated to further remove organic pollutants which cannot be biodegraded.
According to the method for treating the wastewater from ethanol preparation by cellulose, disclosed by the embodiment of the invention, the system structure can be simplified, the cost can be reduced, and the COD (chemical oxygen demand) treatment effect can be improved.
According to the wastewater treatment method for preparing ethanol by cellulose, disclosed by the embodiment of the invention, anaerobic fermentation purification, aeration dephosphorization, denitrification and advanced treatment are sequentially carried out on wastewater, so that COD (chemical oxygen demand) in the wastewater can be treated to be below 100mg/L, the COD treatment effect is excellent, the structure of a wastewater treatment system for preparing ethanol by cellulose can be simplified, and the cost of the wastewater treatment system for preparing ethanol by cellulose is reduced.
In some embodiments of the present invention, in the step a, compressed biogas flowing from bottom to top is introduced into the anaerobic fermentation reaction apparatus 10 so that wastewater and sludge are sufficiently contacted.
Further, in the step a, the wastewater after biodegradation is subjected to degassing, precipitation and separation by using the precipitation separator 400 of the anaerobic fermentation reaction device 10, and the wastewater after the degassing, precipitation and separation is subjected to the step B to remove gas and solids in the wastewater before entering the step B.
Optionally, in the step B, air is introduced into the wastewater dephosphorization reaction apparatus 20 to perform aeration, and magnesium oxide is added as a dephosphorization oxidizer, such as magnesium oxide, into the wastewater dephosphorization reaction apparatus 20.
In some specific examples of the present invention, the step C includes the sub-steps of:
c1: the wastewater discharged from the wastewater dephosphorization reaction apparatus 20 is transferred to the anaerobic ammoxidation reactor 2100 of the denitrification reactor 40 to perform an anaerobic ammoxidation reaction on the aerated wastewater.
C2: the wastewater discharged from the anaerobic ammoxidation reactor 2100 of the denitrification reactor 40 is transferred into the anoxic reaction chamber of the anoxic-aerobic reaction tank 2200 of the denitrification reactor 40 to perform denitrification reaction on the wastewater subjected to the anaerobic ammoxidation reaction in an anoxic environment.
And C3: the wastewater in the anoxic reaction chamber of the anoxic-oxic reaction tank 2200 of the denitrification reactor 40 is transferred to the aerobic reaction chamber of the anoxic-oxic reaction tank 2200 of the denitrification reactor 40, and the denitrification-reacted wastewater is nitrified in an aerobic environment.
In some specific examples of the present invention, after the step C, the denitrified wastewater is coagulated first, and then the step D is performed.
In some embodiments of the invention, the step D comprises the sub-steps of:
d1: delivering the wastewater flowing out of the denitrification reactor 40 to a first-stage Fenton reaction tank 4110 to perform a first-stage Fenton oxidation reaction on the denitrified wastewater;
d2: the wastewater flowing out of the first Fenton reaction tank 4110 is conveyed to a first Fenton sedimentation tank 4130, and the wastewater subjected to the first Fenton oxidation reaction is subjected to first-stage degassing, sedimentation and separation in the first Fenton sedimentation tank 4130;
d3: the wastewater flowing out of the first-stage Fenton sedimentation tank 4130 is conveyed to a second-stage Fenton reaction tank 4120, and the wastewater subjected to degassing sedimentation separation is subjected to a second-stage Fenton oxidation reaction in the second-stage Fenton reaction tank 4120;
d4: the wastewater flowing out of the secondary Fenton reaction tank 4120 is conveyed to a secondary Fenton sedimentation tank 4140, and the wastewater after the secondary Fenton oxidation reaction is subjected to secondary degassing, sedimentation and separation in the secondary Fenton sedimentation tank 4140;
D5: the wastewater discharged from the secondary Fenton sedimentation tank 4140 is sent to a sand filter 4200, and the wastewater separated by the secondary deaeration sedimentation is sand-filtered by the sand filter 4200.
Optionally, in the step D1, sulfuric acid, ferrous sulfate and hydrogen peroxide are added into the Fenton reaction chamber 4111 of the first-stage Fenton reaction tank 4110 to stir, and then a flocculant is added into the Fenton flocculation chamber 4112 of the first-stage Fenton reaction tank 4110 to stir. In the step D4, sulfuric acid, ferrous sulfate and hydrogen peroxide are added into the Fenton reaction chamber 4111 of the secondary Fenton reaction tank 4120 to stir, and then a flocculant is added into the Fenton flocculation chamber 4112 of the secondary Fenton reaction tank 4120 to stir.
According to the wastewater treatment system 1 and the wastewater treatment method for preparing ethanol from cellulose, disclosed by the embodiment of the invention, anaerobic biodegradation, aeration dephosphorization, denitrification and advanced treatment are sequentially carried out on the wastewater generated by preparing ethanol from cellulose, so that COD (chemical oxygen demand) in the wastewater can be treated to be below 100mg/L, and the wastewater treatment system is simple in structure, low in cost and small in occupied area. In addition, according to the wastewater treatment system 1 and the process for preparing ethanol from cellulose, not only the COD treatment effect is good, but also the removal effect of nitrogen and phosphorus is good, for example, nitrogen can reach below 15mg/L, and phosphorus can reach below 0.5 mg/L.
In the description of the present invention, it should be understood that the terms "center", "longitudinal", "lateral", "length", "width", "thickness", "upper", "lower", "front", "rear", "left", "right", "vertical", "horizontal", "top", "bottom", "inner", "outer", "clockwise", "counterclockwise", etc. indicate orientations or positional relationships based on the orientations or positional relationships shown in the drawings are merely for convenience in describing the present invention and simplifying the description, and do not indicate or imply that the devices or elements referred to must have a specific orientation, be configured and operated in a specific orientation, and thus should not be construed as limiting the present invention.
Furthermore, the terms "first," "second," and the like, are used for descriptive purposes only and are not to be construed as indicating or implying a relative importance or implicitly indicating the number of technical features indicated. Thus, a feature defining "a first" or "a second" may explicitly or implicitly include one or more such feature. In the description of the present invention, the meaning of "plurality" means at least two, for example, two, three, etc., unless specifically defined otherwise.
In the present invention, unless explicitly specified and limited otherwise, the terms "mounted," "connected," "secured," and the like are to be construed broadly, and may be, for example, fixedly connected, detachably connected, or integrally formed; can be mechanically or electrically connected; can be directly connected or indirectly connected through an intermediate medium, and can be communicated with the inside of two elements or the interaction relationship of the two elements. The specific meaning of the above terms in the present invention can be understood by those of ordinary skill in the art according to the specific circumstances.
In the present invention, unless expressly stated or limited otherwise, a first feature "above" or "below" a second feature may include both the first and second features being in direct contact, as well as the first and second features not being in direct contact but being in contact with each other through additional features therebetween. Moreover, a first feature being "above," "over" and "on" a second feature includes the first feature being directly above and obliquely above the second feature, or simply indicating that the first feature is higher in level than the second feature. The first feature being "under", "below" and "beneath" the second feature includes the first feature being directly under and obliquely below the second feature, or simply means that the first feature is less level than the second feature.
In the description of the present specification, a description referring to terms "one embodiment," "some embodiments," "examples," "specific examples," or "some examples," etc., means that a particular feature, structure, material, or characteristic described in connection with the embodiment or example is included in at least one embodiment or example of the present invention. In this specification, schematic representations of the above terms are not necessarily directed to the same embodiment or example. Furthermore, the particular features, structures, materials, or characteristics described may be combined in any suitable manner in any one or more embodiments or examples. Further, one skilled in the art can engage and combine the different embodiments or examples described in this specification.
While embodiments of the present invention have been shown and described above, it will be understood that the above embodiments are illustrative and not to be construed as limiting the invention, and that variations, modifications, alternatives and variations may be made to the above embodiments by one of ordinary skill in the art within the scope of the invention.
Claims (35)
1. A wastewater treatment system for preparing ethanol from cellulose is characterized by comprising an anaerobic fermentation reaction device, a wastewater dephosphorization reaction device, a denitrification reactor and a deep treatment system which are sequentially connected in the wastewater treatment process direction,
The anaerobic fermentation reaction device comprises an anaerobic fermentation tank body, a gas stripping pipe and a gas supply pipe, wherein an anaerobic reaction chamber is arranged in the anaerobic fermentation tank body, the anaerobic reaction chamber is provided with a wastewater inlet, a water outlet and an exhaust port, the gas stripping pipe is arranged in the anaerobic reaction chamber, the upper end of the gas stripping pipe is provided with a gas outlet, the lower end of the gas stripping pipe is provided with a gas inlet, and the gas supply pipe is connected with the gas inlet of the gas stripping pipe and is used for supplying gas for stripping into the gas stripping pipe;
the wastewater dephosphorization reaction device comprises a dephosphorization reaction tank body, an aeration device and a degassing and precipitation separator, wherein a dephosphorization reaction chamber is arranged in the dephosphorization reaction tank body, the dephosphorization reaction chamber is provided with a water inlet and a dephosphorization agent adding port, the aeration device is arranged in the dephosphorization reaction chamber, and the degassing and precipitation separator is arranged in the dephosphorization reaction chamber and is positioned above the aeration device and is used for separating gas, water and sludge;
the lower end of the air stripping pipe is adjacent to the bottom of the anaerobic reaction chamber, the upper end of the air stripping pipe extends to the upper part of the anaerobic reaction chamber, and the water outlet is arranged at the upper part of the anaerobic reaction chamber and is higher than the upper end of the air stripping pipe;
The upper end face of the gas stripping pipe is opened to form the gas outlet, and the lower end face of the gas stripping pipe is opened to form the gas inlet;
the air stripping pipe comprises a straight pipe section extending along the vertical direction and an arc-shaped section connected with the upper end of the straight pipe section, and an included angle between the opening direction of the air outlet and the vertical downward direction is greater than or equal to zero degrees and less than 180 degrees;
the anaerobic fermentation reaction device further comprises: the precipitation separator is arranged in the anaerobic reaction chamber and is positioned above the gas stripping pipe, and is provided with a separator water outlet connected with the water outlet and connected with the water inlet of the wastewater dephosphorization reaction device;
the precipitation separator includes:
the device comprises a box body, wherein a degassing and sedimentation cavity is formed in the box body, a sludge outlet is formed in the bottom of the degassing and sedimentation cavity, and the cross-sectional area of the lower part of the degassing and sedimentation cavity is gradually reduced along the direction from top to bottom;
the separator is arranged at the upper part of the degassing and settling cavity, the separator divides the upper part of the degassing and settling cavity into a degassing zone and a settling zone, and the bottom of the degassing zone is communicated with the bottom of the settling zone so that wastewater overflows from the anaerobic reaction chamber into the degassing zone and flows into the settling zone from the bottom of the degassing zone;
A sedimentation inclined plate which is arranged in the sedimentation zone;
the overflow weir is arranged in the sedimentation zone and forms an overflow groove with the water outlet of the separator;
the aeration device is provided with a plurality of aeration heads or aeration pipes which are arranged at intervals;
the wastewater dephosphorization reaction device further comprises:
the upper end and the lower end of each guide cylinder are open, and a plurality of aeration heads or aeration pipes extend into the guide cylinders from the lower ends of the guide cylinders respectively;
the advanced treatment system comprises a plurality of groups of Fenton reaction devices which are sequentially connected along the wastewater treatment process direction, and each group of Fenton reaction devices comprises a Fenton reaction tank and a Fenton sedimentation tank.
2. The system for treating wastewater from ethanol production from cellulose as recited in claim 1, wherein the arc-shaped section is in an inverted U shape, and the opening direction of the air outlet is vertically downward.
3. The cellulosic ethanol wastewater treatment system of any one of claims 1-2, wherein the plurality of stripping tubes are spaced apart in a horizontal plane.
4. The cellulosic ethanol wastewater treatment system of claim 1, wherein an upper edge of a tank portion defining the degassing zone with the partition is lower than an upper edge of the partition and an upper edge of a tank portion defining the settling zone with the partition.
5. The system for treating wastewater from ethanol production from cellulose as recited in claim 4, wherein the tank is rectangular, wherein a lower end of a first longitudinal side wall of a lower portion of the tank extends downward beyond a lower end of a second longitudinal side wall of the lower portion of the tank, and wherein the lower end of the first longitudinal side wall overlaps the lower end of the second longitudinal side wall in an up-down direction.
6. The wastewater treatment system for producing ethanol from cellulose according to claim 1, wherein the anaerobic fermentation reaction apparatus further comprises: the sedimentation separator is arranged outside the anaerobic fermentation tank body, the water outlet is connected with the wastewater dephosphorization reaction device through the sedimentation separator, and the sedimentation separator comprises:
the device comprises a box body, wherein a degassing and precipitating cavity is formed in the box body, the degassing and precipitating cavity is provided with an inlet, a separator water outlet and a sludge outlet, the inlet is communicated with the water outlet, the separator water outlet is connected with the wastewater dephosphorization reaction device, the lower part of the degassing and precipitating cavity is formed into at least one conical cavity with the cross-sectional area gradually decreasing along the direction from top to bottom, and the sludge outlet is formed at the bottom of the conical cavity;
The sedimentation inclined plate is arranged in the degassing and sedimentation cavity;
the overflow weir is arranged in the degassing and settling cavity, and an overflow groove communicated with the water outlet of the separator is formed in the overflow weir.
7. The system for treating wastewater from ethanol production from cellulose as recited in claim 6, wherein the anaerobic fermentation reaction apparatus further comprises: the energy dissipater is connected between the water outlet of the anaerobic reaction chamber and the inlet of the degassing and precipitating cavity.
8. The system for treating wastewater from ethanol production from cellulose as recited in claim 6, wherein the anaerobic fermentation reaction apparatus further comprises:
the sludge return pipe is used for returning the sludge discharged from the sludge outlet into the anaerobic reaction chamber, one end of the sludge return pipe is communicated with the anaerobic reaction chamber, the sludge outlet is connected with the sludge return pipe through a sludge discharge pipe, and a sludge return pump is arranged on the sludge return pipe.
9. The wastewater treatment system for producing ethanol from cellulose according to claim 1, wherein the anaerobic fermentation reaction apparatus further comprises: the anaerobic fermentation tank comprises a water sealed tank body, wherein a safety air port is arranged at the top of the anaerobic fermentation tank body, and the safety air port is connected with the water sealed tank.
10. The system for treating wastewater from ethanol production from cellulose as recited in claim 1, wherein the wastewater dephosphorization reaction apparatus further comprises:
the water distributor is arranged in the dephosphorization reaction chamber and positioned below the aeration device, and the water distributor is connected with the water inlet.
11. The system for treating wastewater from ethanol production from cellulose as recited in claim 10, wherein the water distributor has a plurality of water distribution openings which are spaced apart and open downward.
12. The system for treating wastewater from ethanol production from cellulose as recited in claim 1, wherein the dephosphorization reaction chamber has a discharge port at a lower portion of the dephosphorization reaction tank.
13. The system for treating wastewater from the production of ethanol from cellulose as recited in claim 12, wherein the wastewater dephosphorization reaction apparatus further comprises:
the cyclone is provided with a cyclone inlet, a mud outlet and a cyclone outlet, wherein the cyclone inlet is communicated with the discharge port, and the cyclone outlet is connected with the dephosphorization reaction chamber through a water return pipe.
14. The system for treating wastewater from the production of ethanol from cellulose as recited in claim 12, wherein the wastewater dephosphorization reaction apparatus further comprises: the device comprises a pump and a desliming device connected with the pump, wherein clear liquid after sludge is removed by the desliming device is returned to the dephosphorization reaction chamber.
15. The system for treating wastewater from the production of ethanol from cellulose as recited in claim 12, wherein the wastewater dephosphorization reaction apparatus further comprises: and the clear liquid after being precipitated by the precipitation device is returned to the dephosphorization reaction chamber.
16. The cellulosic ethanol wastewater treatment system of claim 1, wherein the degasification precipitation separator comprises:
the separator body is internally provided with a degassing and precipitating chamber, the bottom of the degassing and precipitating chamber is provided with a sludge discharge port, and the cross-sectional area of the lower part of the degassing and precipitating chamber is gradually reduced along the direction from top to bottom;
the baffle plate is arranged at the upper part of the degassing and precipitating chamber, the baffle plate divides the upper part of the degassing and precipitating chamber into a degassing cavity and a precipitating cavity, and the bottom of the degassing cavity is communicated with the bottom of the precipitating cavity so that wastewater overflows from the dephosphorization reaction chamber into the degassing cavity and flows into the precipitating cavity from the bottom of the degassing cavity;
the inclined sedimentation plate or the inclined sedimentation pipe is arranged in the sedimentation cavity;
the effluent overflow weir is arranged in the sedimentation cavity and forms an effluent overflow groove with a separation outlet communicated with the denitrification reactor.
17. The cellulosic ethanol wastewater treatment system of claim 16, wherein an upper edge of the separator body portion defining the degassing chamber with the baffle is lower than an upper edge of the baffle and an upper edge of the separator body portion defining the settling chamber with the baffle.
18. The cellulosic ethanol wastewater treatment system of claim 16, wherein the separator body is rectangular in cross-section.
19. The cellulosic ethanol wastewater treatment system of claim 16, wherein the lower end of the first longitudinal sidewall of the lower portion of the separator body extends downward beyond the lower end of the second longitudinal sidewall of the lower portion of the separator body, and wherein the lower end of the first longitudinal sidewall overlaps the lower end of the second longitudinal sidewall in the up-down direction.
20. The system for treating wastewater from the production of ethanol from cellulose as recited in claim 1, wherein the wastewater dephosphorization reaction apparatus further comprises: an aeration pump or an aeration fan which is arranged outside the dephosphorization reaction tank body and connected with the aeration device, and the water inlet is connected with a wastewater control valve.
21. The wastewater treatment system for preparing ethanol from cellulose according to claim 1, wherein a top cover is arranged at the top of the dephosphorization reaction tank body, and the dephosphorization agent adding port is arranged on the top cover.
22. The wastewater treatment system for producing ethanol from cellulose according to claim 1, wherein the denitrification reactor comprises an anaerobic ammoxidation reactor and an anoxic aerobic reaction tank connected to each other.
23. The system for treating wastewater from ethanol production from cellulose as recited in claim 1, further comprising a coagulation reactor connected between the denitrification reactor and the advanced treatment system, wherein the coagulation reactor has a coagulation tank, a flocculation tank and a sedimentation tank which are sequentially communicated in the wastewater treatment process direction.
24. The system of claim 1, wherein each Fenton reaction tank is provided with a plurality of Fenton reaction chambers and Fenton flocculation chambers which are sequentially communicated along the wastewater treatment process direction, a Fenton fast stirrer is arranged in each Fenton reaction chamber, a Fenton slow stirrer is arranged in each Fenton flocculation chamber, and a Fenton sloping plate precipitator and a Fenton mud scraper are arranged in each Fenton sedimentation tank.
25. The cellulosic ethanol wastewater treatment system of claim 1, wherein the further treatment system further comprises:
The sand filter is connected with the last Fenton sedimentation tank along the wastewater treatment process direction;
and the air storage tank is connected with the sand filter.
26. The system of any one of claims 24-25, wherein the plurality of Fenton reaction tanks comprises a primary Fenton reaction tank and a secondary Fenton reaction tank, and the plurality of Fenton sedimentation tanks comprises a primary Fenton sedimentation tank and a secondary Fenton sedimentation tank, and wherein the primary Fenton reaction tank, the primary Fenton sedimentation tank, the secondary Fenton reaction tank and the secondary Fenton sedimentation tank are sequentially connected along the wastewater treatment process direction.
27. The cellulosic ethanol wastewater treatment system of any one of claims 24-25, wherein the further treatment system further comprises:
a sulfuric acid storage tank connected to a first one of a plurality of Fenton reaction chambers of each Fenton reaction tank in the wastewater treatment process direction;
a ferrous sulfate solution tank connected to a first one of a plurality of Fenton reaction chambers of each Fenton reaction tank in the wastewater treatment process direction;
The hydrogen peroxide storage tank is connected with the first one of the Fenton reaction cavities of each Fenton reaction tank along the wastewater treatment process direction;
and the Fenton flocculant tanks are connected with Fenton flocculation cavities of each Fenton reaction tank.
28. A method for treating cellulosic ethanol wastewater using the cellulosic ethanol wastewater treatment system of any one of claims 1-27, comprising the steps of:
a: carrying out biodegradation on the wastewater in an anaerobic environment;
b: aerating and dephosphorizing the waste water after biodegradation;
c: denitrification is carried out on the wastewater after aeration and dephosphorization;
d: and (3) deeply treating the denitrified wastewater to further remove organic pollutants which cannot be biodegraded.
29. The method for treating wastewater from ethanol production from cellulose as recited in claim 28, wherein in the step a, compressed biogas flowing from bottom to top is introduced so that the wastewater and the sludge are sufficiently contacted.
30. The method according to claim 28, wherein in the step a, the waste water after biodegradation is subjected to degassing, precipitation and separation, and the waste water after the degassing, precipitation and separation is subjected to the step B.
31. The method for treating wastewater from ethanol production from cellulose as recited in claim 28, wherein in the step B, aeration is performed by introducing air, and magnesium oxide is added as a dephosphorizing agent.
32. The method for treating wastewater from ethanol production from cellulose as recited in claim 28, wherein the step C comprises the substeps of:
c1: anaerobic ammoxidation reaction is carried out on the wastewater after aeration and dephosphorization;
c2: carrying out denitrification reaction on the wastewater subjected to anaerobic ammoxidation reaction in an anoxic environment;
and C3: and (3) carrying out nitration reaction on the wastewater subjected to denitrification reaction in an aerobic environment.
33. The method according to claim 28, wherein after the step C, the denitrified wastewater is coagulated before the step D.
34. The method for treating wastewater from ethanol production from cellulose as recited in claim 28, wherein the step D comprises the sub-steps of:
d1: carrying out a first-stage Fenton reaction on the denitrified wastewater;
d2: carrying out primary degassing, precipitation and separation on the wastewater subjected to the primary Fenton reaction;
d3: carrying out a secondary Fenton reaction on the wastewater after the primary degassing precipitation separation;
D4: carrying out secondary degassing precipitation separation on the wastewater after the secondary Fenton reaction;
d5: and (3) sand filtering the wastewater after the secondary degassing precipitation separation.
35. The method for treating wastewater from ethanol production from cellulose as recited in claim 34, wherein sulfuric acid, ferrous sulfate and hydrogen peroxide are added to the step D1 and the step D4, respectively, and stirring is performed by adding a flocculant thereto.
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