CN210796000U - Wastewater treatment system - Google Patents
Wastewater treatment system Download PDFInfo
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- CN210796000U CN210796000U CN201920860292.4U CN201920860292U CN210796000U CN 210796000 U CN210796000 U CN 210796000U CN 201920860292 U CN201920860292 U CN 201920860292U CN 210796000 U CN210796000 U CN 210796000U
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Abstract
The utility model provides a wastewater treatment system. The wastewater treatment system comprises: a primary flocculation reaction tank configured to receive wastewater; ca (OH)2A dosing system configured to add Ca (OH) to the primary flocculation reaction tank2(ii) a The primary clarification tank is communicated with the primary flocculation reaction tank to receive the wastewater in the primary flocculation reaction tank; the secondary flue gas reaction tank is communicated with the primary clarification tank to receive the wastewater in the primary clarification tank; and the smoke adding device is configured to introduce smoke into the secondary smoke reaction tank so as to enable the smoke to react with the wastewater in the secondary smoke reaction tank. Because the secondary flue gas reaction tank is arranged, the waste flue gas of a factory is introduced, and Na is greatly reduced2CO3The dosage of the calcium-adding agent is reduced, the operation cost is reduced, and when Ca is contained in the wastewater2+At a concentration greater than Mg2+In the process, the Na addition is not needed by controlling the aeration rate of the flue gas2CO3。
Description
Technical Field
The utility model relates to a waste water treatment field especially relates to a waste water treatment system.
Background
High SS (solid suspended matter is more than or equal to 1000mg/L) and high hardness (Ca in solution)2+、Mg2+The content of plasma hardness ions is more than or equal to 1000mg/L), if the high-salinity wastewater meets the discharge requirement after treatment, the content of chloride ions in the wastewater must be reduced, the wastewater is concentrated by adopting a reverse osmosis technology, the produced water can be recycled or directly discharged, and the concentrated solution is further concentrated and then is evaporated and crystallized to prepare industrial salt; because the wastewater contains high-concentration suspended substances and Ca2+、Mg2+The direct entry of the plasma hardness ions into the reverse osmosis system causes serious reverse osmosis membrane fouling and scaling phenomena, which results in the failure of the reverse osmosis system to work normally, and therefore all suspended matters and Ca must be removed in the pretreatment step2+、Mg2+Plasma is generated.
The traditional pretreatment system adopts Ca (OH)2—Na2CO3The two-base method, the first reaction being carried out first by adding an excess of Ca (OH)2Removing Mg in wastewater2+Then the mixed solution is coagulated and precipitated by a first-stage clarification tank to produce Mg (OH)2And CaSO4The sediment enters a first sludge concentration system in the form of sludge; the supernatant overflows into a second-stage reaction tank, and then excessive Na is added2CO3Removing Ca in solution2+After the reaction is finished, the reaction product enters a secondary clarification tank for coagulating sedimentation to produce CaCO3The sediment enters a second sludge concentration system in the form of sludge, and the supernatant overflows into a reverse osmosis system for continuous treatment.
However, the inventors have found that the conventional method has at least the following problems:
1. because the wastewater contains Ca with higher concentration2+、Mg2+Ion and medicine addingThe sediment material that later forms is more, and belongs to the colloid form and exists, and density is less, is difficult to deposit, and the clarification tank needs to set up very low rising velocity of flow can satisfy clarification effect requirement, leads to the sectional area of clarification tank very big, and area is huge.
2. The clarification tank is greatly influenced by the environment (mainly the influence of temperature change) and the quality and quantity fluctuation of the incoming water, and although the clarification tank is provided with a large enough sectional area and the wastewater has a low enough ascending flow velocity, the clarification tank still has partial Mg (OH)2、CaSO4、CaCO3Along with waste water inflow reverse osmosis system, the effect of water is unstable, in case a large amount of solid sediment material flows into follow-up reverse osmosis treatment system along with waste water, can cause reverse osmosis system's dirty stifled and scale deposit, and difficult the recovery.
3. Due to the waste water Ca2+、Mg2+High ion concentration, large amount of Ca (OH) needs to be added2And Na2CO3Causing a problem of very high operation cost.
4. Because the waste water is high-concentration waste water, the ion content in the waste water is very high, a large amount of solid sediment substances can be generated after the chemicals are added, so that a large amount of sludge (solid waste) generated by a waste water treatment system every year needs to be treated, and the resource utilization can not be realized.
SUMMERY OF THE UTILITY MODEL
The utility model aims to overcome at least one defect of the high salt waste water treatment of current high SS high rigidity, provide a waste water treatment system.
Specifically, the utility model provides a wastewater treatment system, it includes:
a primary flocculation reaction tank configured to receive wastewater;
Ca(OH)2a dosing system configured to add Ca (OH) to the primary flocculation reaction tank2；
The primary clarification tank is communicated with the primary flocculation reaction tank to receive the wastewater in the primary flocculation reaction tank;
the secondary flue gas reaction tank is communicated with the primary clarification tank to receive the wastewater in the primary clarification tank; and
and the smoke adding device is configured to introduce smoke into the secondary smoke reaction tank so as to enable the smoke to react with the wastewater in the secondary smoke reaction tank.
Optionally, the wastewater treatment system further comprises:
the third-stage flocculation reaction tank is communicated with the second-stage flue gas reaction tank so as to receive the wastewater in the second-stage flue gas reaction tank;
Na2CO3a dosing system configured to add Na to the tertiary flocculation reaction tank2CO3(ii) a And
and the concentration device is communicated with the third-stage flocculation reaction tank to receive the wastewater in the third-stage flocculation reaction tank and concentrate the received wastewater.
Optionally, the wastewater treatment system further comprises a tubular membrane module, which is communicated with the concentration device to receive the wastewater in the concentration device, and discharge the received wastewater after filtering.
Optionally, the flue gas adding device comprises a flue gas feeding pipe, an induced draft fan and a first aeration device;
the first aeration device is arranged in the secondary flue gas reaction tank;
the air outlet of the smoke delivery pipe is communicated with the inlet of the first aeration device;
the draught fan is installed in send the tobacco pipe.
Optionally, the wastewater treatment system further comprises a desulfurization absorption tower, which is communicated with the sludge outlet of the concentration device.
Optionally, the wastewater treatment system further comprises:
the water storage adjusting tank is communicated with the primary flocculation reaction tank;
the second aeration device is arranged in the water storage adjusting tank;
the water producing tank is connected to the water outlet of the tubular membrane module;
the sludge treatment system is connected to a sludge discharge port of the primary clarification tank;
the first stirring device is arranged in the primary flocculation reaction tank;
the second stirring device is arranged in the primary clarification tank; and
and the third stirring device is arranged in the third-stage flocculation reaction tank.
Optionally, the wastewater treatment system further comprises a pH detection device configured to detect a pH value of the wastewater in the secondary flue gas reaction tank.
Alternatively, the Ca (OH)2The molar ratio of the dosage of the dosing system to the magnesium ions in the wastewater in the primary flocculation reaction tank is 5/6-1.
Optionally, in the third flocculation reaction tank, the ratio between the molar concentration of sodium carbonate and the molar concentration of calcium ions is 10/11-1.
Optionally, the wastewater treatment system further comprises: and the circulating pump is arranged between the concentration device and the tubular membrane module and is used for promoting the wastewater to circularly flow between the concentration device and the tubular membrane module.
The utility model discloses an among the effluent disposal system, owing to have second grade flue gas reaction tank, introduce mill's waste flue gas, greatly reduced Na2CO3The dosage of the calcium-adding agent is reduced, the operation cost is reduced, and when Ca is contained in the wastewater2+At a concentration greater than Mg2+In the process, the Na addition is not needed by controlling the aeration rate of the flue gas2CO3。
Furthermore, the waste water treatment system of the utility model occupies less area and does not need to be provided with a secondary clarification tank; tubular microfiltration replaces a traditional clarification tank, ensures the stability of the effluent quality, cannot be influenced by the quality and quantity of the incoming water and environmental factors, and plays a good role in guaranteeing a subsequent reverse osmosis concentration system.
Furthermore, a sludge delivery pump is arranged behind the concentration device, and the sediment generated by the three-stage flocculation reaction tank is mainly CaCO3Mud is directly defeated into the desulfurization system in the garden through the mud delivery pump, uses as desulfurization system absorbent, can realize the utilization of mud as a resources, reduces the production volume of solid useless, has still saved one set of sludge concentration system simultaneously.
The utility model discloses a wastewater treatment system can be the high salt wastewater treatment system of high SS high rigidity of filtration among the zero discharge system, and structural design is reasonable. The utility model belongs to water pollution prevention and control field can be used to the power plant and discharge trades such as manufacturing, food, weaving, power plant, printing and dyeing, municipal administration, car, petrochemical, electron semiconductor waste water zero release, biological fermentation waste water zero release of similar water pollutant. Wherein SS is the content of suspended solid, the wastewater with the SS content of 1000-50000 is generally called high-SS wastewater.
The above and other objects, advantages and features of the present invention will become more apparent to those skilled in the art from the following detailed description of specific embodiments thereof, taken in conjunction with the accompanying drawings.
Drawings
Some specific embodiments of the present invention will be described in detail hereinafter, by way of illustration and not by way of limitation, with reference to the accompanying drawings. The same reference numbers in the drawings identify the same or similar elements or components. Those skilled in the art will appreciate that the drawings are not necessarily drawn to scale. In the drawings:
FIG. 1 is a schematic block diagram of a wastewater treatment system according to one embodiment of the present invention.
Detailed Description
FIG. 1 is a schematic block diagram of a wastewater treatment system according to one embodiment of the present invention. As shown in FIG. 1, the embodiment of the present invention provides a wastewater treatment system. The wastewater treatment system comprises a primary flocculation reaction tank 30, Ca (OH)2A dosing system 31, a primary clarification tank 40, a secondary flue gas reaction tank 50 and a flue gas adding device. The primary flocculation tank 30 is configured to receive wastewater. Ca (OH)2 Dosing system 31 is configured to add Ca (OH) to the primary flocculation reaction tank 302. The primary clarifier 40 is communicated with the primary flocculation reaction tank 30 to receive the wastewater in the primary flocculation reaction tank 30. The secondary flue gas reaction tank 50 is in communication with the primary clarifier 40 to receive the wastewater within the primary clarifier 40. The flue gas adding device is configured to introduce flue gas into the secondary flue gas reaction tank 50 so that the flue gas and the secondary flue gas reaction tank 50, the wastewater in the reactor was reacted. Because the secondary flue gas reaction tank 50 is arranged, the waste flue gas of a factory is introduced, and Na is greatly reduced2CO3The dosage of the calcium-adding agent is reduced, the operation cost is reduced, and when Ca is contained in the wastewater2+At a concentration greater than Mg2+In the process, the Na addition is not needed by controlling the aeration rate of the flue gas2CO3。
In some embodiments of the present invention, the wastewater treatment system further comprises a third-stage flocculation reaction tank 70, Na2CO3A dosing system 71 and a concentration device. The third stage flocculation reaction tank 70 is communicated with the second stage flue gas reaction tank 50 to receive the wastewater in the second stage flue gas reaction tank 50. Na (Na)2CO3The dosing system 71 is configured to add Na to the tertiary flocculation reaction tank 702CO3. The concentration device is communicated with the third-stage flocculation reaction tank 70 to receive the wastewater in the third-stage flocculation reaction tank 70 and concentrate the received wastewater. The concentration device is preferably a concentration tank 80, in particular a tubular membrane concentration tank.
In some embodiments of the present invention, the wastewater treatment system further includes a tubular membrane module 91, which is communicated with the concentration device to receive the wastewater in the concentration device, and filter the received wastewater and discharge the wastewater, so as to filter and separate solid and liquid, such as removing suspended solid, colloid, and partial organic matters in the wastewater. The water outlet of the tubular membrane module 91 can be connected with a water production tank 93. The effluent quality is more stable, the complexity of the system is reduced, the continuous operation can be realized without the help of people, and the occupied area is further reduced. Further, the wastewater treatment system further comprises a circulating pump 92 disposed between the concentration device and the tubular membrane module 91 to promote the wastewater to flow circularly between the concentration device and the tubular membrane module 91. The circulation pump 92 may be used to increase the cross flow ratio of the tubular membrane surface. In some alternative embodiments of the present invention, the water producing tank 93 may also be directly connected to the concentration tank 80.
In some embodiments of the present invention, the flue gas adding device includes a flue gas feeding pipe, an induced draft fan 63 and a first aeration device 62. The first aeration device 62 is arranged in the secondary flue gas reaction tank 50. The air outlet of the smoke delivery pipe is communicated with the inlet of the first aeration device 62. The draught fan 63 is installed on the smoke delivery pipe. The inlet of the smoke delivery pipe may be connected to a smoke exhaust such as a flue 61.
In some embodiments of the present invention, the wastewater treatment system may further include a storage tank 20, a second aeration device 21, a sludge disposal system 42, a first stirring device 32, a second stirring device 41, a third stirring device 72, a pH detection device, and a desulfurization absorption tower 81. The water storage adjusting tank 20 is communicated with the primary flocculation reaction tank 30. The second aeration device 21 is installed in the reservoir tank 20. The sludge disposal system 42 is connected to the sludge discharge port of the primary clarifier 40. The first stirring device 32 is arranged in the primary flocculation reaction tank 30. The second stirring device 41 is disposed in the primary clarifier 40. The third stirring device 72 is arranged in the third-stage flocculation reaction tank 70. The desulfurization absorption tower 81 is communicated with the sludge outlet of the concentration device. The pH detection device is configured to detect the pH value of the wastewater in the secondary flue gas reaction tank 50.
The utility model discloses in the effluent disposal system of embodiment, retaining equalizing basin 20 is received and is stored the waste water that comes from the mill and/or come from the filter press filtrating among other waste water treatment processes. The second aeration device 21 at the bottom of the reservoir tank 20 can play a role of stirring and can remove a part of organic matters at the same time.
Ca (OH) is added into the first-stage flocculation reaction tank 302Removing magnesium ions in the wastewater; preferably, the molar ratio of the calcium hydroxide adding amount to the magnesium ions in the wastewater is 1:1 to 1: 1.2. In the prior art, sodium carbonate is generally used for removing magnesium ions in wastewater, but the price of industrial sodium carbonate is higher than that of calcium hydroxide, so the cost is reduced by using calcium hydroxide in the aspect of removing magnesium ions. Preferably, the first stirring device 32 in the first-stage flocculation reaction tank 30 is used for stirring the wastewater after the calcium hydroxide is added, so that the reaction of magnesium ions and hydroxyl groups in the first-stage flocculation reaction tank 30 to generate magnesium hydroxide precipitate is more complete. The wastewater from the water storage regulating reservoir 20 continuously flows into the first-stage flocculation reaction tank 30, and calcium hydroxide is continuously added in the process, and the first-stage flocculation reaction tank 30 adopts a central cylinder for adding chemicals, so that the reaction residence time of the calcium hydroxide and the wastewater is longer than four hours.
The wastewater in the primary flocculation reaction tank 30 flows into a primary clarification tank 40, and solid sludge such as magnesium hydroxide, calcium sulfate and the like in the wastewater is precipitated in the primary clarification tank 40. The primary clarifier 40 is provided with a sludge discharge port at the connection part with the sludge disposal system 42; the sludge disposal system 42 is used to treat the sludge discharged from the primary clarifier 40. More preferably, a sludge settling device is further arranged in the primary clarifier 40, so that solid sludge such as magnesium hydroxide and the like can be settled and discharged as soon as possible. More preferably, the second stirring device 41 provided in the primary clarifier 40 prevents solid sludge such as magnesium hydroxide from adhering to and coagulating on the wall of the primary clarifier 40, and further blocks the sludge discharge port of the primary clarifier 40, thereby preventing the solid sludge such as magnesium hydroxide from being discharged in time.
The wastewater of the primary clarification tank 40 flows into a secondary flue gas reaction tank 50, the clean flue gas which is generated by factory coal and contains a large amount of carbon dioxide gas and is subjected to desulfurization, denitrification and dedusting treatment is introduced into the secondary reaction tank, a large amount of carbonate ions are generated in the secondary reaction tank, and the carbonate ions are combined with calcium ions in the wastewater to generate solid calcium carbonate precipitate for removing the calcium ions in the wastewater; the pH value of the waste water is gradually reduced along with the continuous introduction of the flue gas, the introduction of the flue gas is stopped when the pH value of the waste water is reduced to 7.5, and the process is continuously changed, so that the pH value of the waste water needs to be monitored in real time. Preferably, the first aeration device 62 is used for stirring the wastewater in the secondary flue gas reaction tank 50 to accelerate the contact of carbonate ions and calcium ions, thereby accelerating the removal of calcium ions in the wastewater.
Sodium carbonate, i.e., a large amount of carbonate ions, is added into the third-stage flocculation reaction tank 70 to further remove calcium ions in the wastewater. In the tertiary flocculation reaction tank 70, the molar concentration of sodium carbonate: the molar concentration of calcium ions is 1:1 to 1:1.1, and the calcium ions in the wastewater need to be monitored in real time. The third stirring device 72 not only accelerates the dissolution of sodium carbonate but also accelerates the combination of carbonate ions with calcium ions in the wastewater to generate solid calcium carbonate.
The concentration tank 80 is connected with the third-stage flocculation reaction tank 70, and the wastewater of the third-stage flocculation reaction tank 70 overflows into the concentration tank 80. The main component of the sludge generated in the concentration tank 80 is calcium carbonate which can be used as a raw material in a desulfurization system, thereby realizing the resource utilization of the sludge.
The water producing tank 93 is connected to the concentration tank 80 for receiving water from the concentration tank 80. More preferably, a tubular membrane system is further disposed between the concentration tank 80 and the water producing pond 93 for removing a large amount of SS (mainly calcium carbonate), organic matters or other suspended matters, colloids and the like in the wastewater, so that the quality of the effluent is controlled below 0.2 NTU. The wastewater from the concentration tank 80 passes through a tubular membrane system and then enters a product water tank 93. The tubular membrane system comprises a circulating pump 92 and a tubular membrane module 91; the circulation pump 92 conveys the wastewater and is used for increasing the flow rate of the wastewater on the surface of the tubular membrane; the tubular membrane module 91 is used for filtering and separating solid and liquid. Further, a tubular membrane feed pump may be provided between the concentration tank 80 and the circulation pump 92 for pumping the wastewater into the tubular membrane system. The tubular membrane microfiltration has a rapid pollution and blockage risk for low SS wastewater, and the flux is rapidly reduced within 120 minutes; however, when the tubular membrane microfiltration is used for treating high SS wastewater, the flux of the tubular membrane microfiltration can not be obviously reduced by means of the scouring and protection of the high SS on the surface of the tubular membrane, so that the tubular membrane system replaces the function of a traditional clarifier and meets the requirement of membrane concentration water inlet of subsequent desulfurization wastewater (the turbidity is less than 0.2 NTU); compared with the traditional clarification tank, the effluent quality of the tubular membrane system is more stable, the automatic continuous operation can be realized, and the solid content (mainly calcium carbonate) of the concentrated solution concentrated by the tubular membrane system can reach 5-10%, so that the tubular membrane system replaces the traditional clarification tank, and a set of sludge concentration system is not required to be arranged independently, thereby greatly simplifying the complexity of the system and improving the stability; and the concentrated solution generated by the tubular membrane concentration tank 80 can be directly injected into a desulfurization system, and calcium carbonate is recycled, so that the economy is improved, and the generation of sludge is reduced. When the water inflow of the impoundment adjusting pool 20 is 2 multiplied by 34m3And h, when SS of inlet water of the water storage regulating pool 20 is 1700ppm and the total filtering area of the tubular membrane system is 255.36 square meters, the SS can be concentrated to be more than or equal to 50000ppm by the tubular membrane system, the quality of produced water is good, and the turbidity is less than 0.2 NTU.
The utility model discloses a waste water treatment system is at the during operation, and the waste water in the retaining equalizing basin 20 flows to one-level flocculation reaction tank 30, through reacting the back, and the entering one-level depositing reservoir 40 that flows automatically, and the upwelling speed of control one-level depositing reservoir 40 is 5m/h, and when mud concentration reached 3-5%, the mud of starting discharging promptly, the mud of arranging is intermittent type operation, and mud gets into mud processing system 42 and deals with this moment. The water produced by the first-level clarification tank 40 flows into the second-level flue gas reaction tank 50 in an overflowing manner, the water enters the third-level flocculation reaction tank 70 after reaction, the wastewater after reaction automatically flows into the concentration tank 80, and after microfiltration and filtration by a tubular membrane system, the produced water (permeate) enters the next wastewater treatment link for continuous treatment, and the concentrate returns to the concentration tank 80, which is a dynamic balance process, along with time accumulation, the concentration of the concentrate in the concentration tank 80 is higher and higher, when the solid content reaches 5%, the bottom of the concentration tank 80 is opened for sludge discharge, after a certain amount of volume is discharged (the SS concentration in the concentration tank 80 is 1-2% after sludge discharge is controlled), sludge discharge is stopped, and the sludge is sent into a desulfurization system through a sewage pump to be used as a desulfurization absorbent. That is, the concentration of the solution in the concentration tank 80 is a dynamically changing process, and the concentration is the lowest after the sludge discharge and the highest before the sludge discharge. Preferably, the thickening tank 80 is conical funnel shaped. In the working process, the control of the flow rate and the control of the sludge discharge can be controlled by a valve.
The utility model discloses a wastewater treatment system has not only improved desulfurization waste water and has gone out water quality stability, has reduced the complexity of system moreover, reduces area, practices thrift the investment. Realizes the recycling of calcium carbonate sludge, saves energy, realizes the cyclic utilization of resources, improves economic benefits and reduces the generation of sludge. The tubular membrane replaces the traditional clarification tank, and then a set of sludge concentration system does not need to be arranged independently, thereby greatly simplifying the complexity of the system and improving the stability.
Thus, it should be appreciated by those skilled in the art that while a number of exemplary embodiments of the invention have been shown and described in detail herein, many other variations and modifications can be made, consistent with the principles of the invention, which are directly determined or derived from the disclosure herein, without departing from the spirit and scope of the invention. Accordingly, the scope of the present invention should be understood and interpreted to cover all such other variations or modifications.
Claims (8)
1. A wastewater treatment system, comprising:
a primary flocculation reaction tank configured to receive wastewater;
Ca(OH)2a dosing system configured to add Ca (OH) to the primary flocculation reaction tank2；
The primary clarification tank is communicated with the primary flocculation reaction tank to receive the wastewater in the primary flocculation reaction tank;
the secondary flue gas reaction tank is communicated with the primary clarification tank to receive the wastewater in the primary clarification tank; and
and the smoke adding device is configured to introduce smoke into the secondary smoke reaction tank so as to enable the smoke to react with the wastewater in the secondary smoke reaction tank.
2. The wastewater treatment system of claim 1, further comprising:
the third-stage flocculation reaction tank is communicated with the second-stage flue gas reaction tank so as to receive the wastewater in the second-stage flue gas reaction tank;
Na2CO3a dosing system configured to add Na to the tertiary flocculation reaction tank2CO3(ii) a And
and the concentration device is communicated with the third-stage flocculation reaction tank to receive the wastewater in the third-stage flocculation reaction tank and concentrate the received wastewater.
3. The wastewater treatment system of claim 2, further comprising:
and the tubular membrane component is communicated with the concentration device to receive the wastewater in the concentration device, filter the received wastewater and discharge the filtered wastewater.
4. The wastewater treatment system of claim 1, wherein the flue gas adding device comprises a flue gas feeding pipe, an induced draft fan and a first aeration device;
the first aeration device is arranged in the secondary flue gas reaction tank;
the air outlet of the smoke delivery pipe is communicated with the inlet of the first aeration device;
the draught fan is installed in send the tobacco pipe.
5. The wastewater treatment system of claim 2, further comprising:
and the desulfurization absorption tower is communicated with the sludge outlet of the concentration device.
6. The wastewater treatment system of claim 3, further comprising:
the water storage adjusting tank is communicated with the primary flocculation reaction tank;
the second aeration device is arranged in the water storage adjusting tank;
the water producing tank is connected to the water outlet of the tubular membrane module;
the sludge treatment system is connected to a sludge discharge port of the primary clarification tank;
the first stirring device is arranged in the primary flocculation reaction tank;
the second stirring device is arranged in the primary clarification tank; and
the third stirring device is arranged in the third-stage flocculation reaction tank;
the concentration device is a concentration tank.
7. The wastewater treatment system of claim 2, further comprising:
and the pH detection device is configured to detect the pH value of the wastewater in the secondary flue gas reaction tank.
8. The wastewater treatment system of claim 3, further comprising:
and the circulating pump is arranged between the concentration device and the tubular membrane module and is used for promoting the wastewater to circularly flow between the concentration device and the tubular membrane module.
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