CN216472713U - Pharmacy waste water salt zero release processing system - Google Patents
Pharmacy waste water salt zero release processing system Download PDFInfo
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- CN216472713U CN216472713U CN202121603794.2U CN202121603794U CN216472713U CN 216472713 U CN216472713 U CN 216472713U CN 202121603794 U CN202121603794 U CN 202121603794U CN 216472713 U CN216472713 U CN 216472713U
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Abstract
The utility model provides a pharmaceutical wastewater salt-free treatment system which comprises a pretreatment system, wherein pharmaceutical wastewater is conveyed to the pretreatment system for treatment, the water outlet end of the pretreatment system is connected with the water inlet end of a nanofiltration system, the concentrated water outlet end of the nanofiltration system is connected with the water inlet end of a first evaporator, the produced water outlet end of the nanofiltration system is connected with the water inlet end of a first reverse osmosis system, the concentrated water outlet end of the first reverse osmosis system is connected with the water inlet end of a second reverse osmosis system, the produced water outlet end of the second reverse osmosis system is connected with the water inlet end of the first reverse osmosis system, and the concentrated water outlet end of the second reverse osmosis system is connected with the produced water outlet end of the second reverse osmosis system. The pharmaceutical wastewater salt-separation zero-discharge treatment system adopts a combined process of pretreatment, nanofiltration, reverse osmosis and evaporator to treat pharmaceutical wastewater, and reduces investment and operation cost while ensuring salt separation effect.
Description
Technical Field
The utility model belongs to the field of industrial wastewater treatment, and particularly relates to a zero-release treatment system for pharmaceutical wastewater containing water and salt.
Background
Under the common conditions, the pharmaceutical wastewater has relatively high treatment difficulty due to high COD, high ammonia nitrogen, high toxicity, complex components and the like. In the pharmaceutical wastewater treatment, due to some complex and difficult-to-degrade organic matter components, the wastewater is difficult to be directly treated by a common biochemical method until the wastewater reaches the standard and is discharged, so that an advanced treatment system is required to be added at the rear end of a biochemical system.
The Fenton method is taken as an example, ferrous sulfate and hydrogen peroxide are added into a water body according to a certain proportion, and hydroxyl radicals with strong oxidizing property are generated by utilizing a chain catalytic reaction between ferrous iron and the hydrogen peroxide to further oxidize refractory organic matters in the wastewater. However, the advanced oxidation technology still has some defects which are difficult to solve, firstly, the advanced oxidation technology cannot resist large water quality fluctuation, and if the dosage is not adjusted in time when water fluctuates, the produced water still cannot reach the standard for recycling; secondly, the process generates a large amount of chemical sludge, most of the chemical sludge is qualified as solid waste and even dangerous waste, the waste needs to be professionally buried in a special landfill site, the processing difficulty is very high, the cost is very high, and the harm to the environment is very obvious.
SUMMERY OF THE UTILITY MODEL
In order to solve the problems in the prior art, the application provides a pharmaceutical wastewater salinity-reduction treatment system which adopts a pretreatment, a nanofiltration, a reverse osmosis and an evaporator, adopts a sectional concentration process in a nanofiltration production section to ensure the salinity-reduction effect, adopts a permeation-assisted reverse osmosis process in a reverse osmosis production section to carry out deep concentration, and can effectively reduce the operation energy consumption and the investment cost through the whole process.
The utility model provides a pharmaceutical wastewater salt-separation zero-emission treatment system which comprises a pretreatment system, wherein pharmaceutical wastewater is conveyed to the pretreatment system for treatment, the water outlet end of the pretreatment system is connected with the water inlet end of a nanofiltration system, the concentrated water outlet end of the nanofiltration system is connected with the water inlet end of a first evaporator, the water outlet end of the produced water of the nanofiltration system is connected with the water inlet end of a first reverse osmosis system, the concentrated water outlet end of the first reverse osmosis system is connected with the water inlet end of a second reverse osmosis system, the water outlet end of the produced water of the second reverse osmosis system is connected with the water inlet end of the first reverse osmosis system, and the concentrated water outlet end of the second reverse osmosis system is connected with the water outlet end of the produced water of the second reverse osmosis system.
In a preferred embodiment, the pretreatment system comprises a biochemical system, a tubular ultrafiltration system and a hardness removal device, wherein the water outlet end of the biochemical system is connected with the water inlet end of the hardness removal device, and the water outlet end of the hardness removal device is connected with the water inlet end of the tubular ultrafiltration system. The pretreatment system mainly removes colloid and suspended matters, and reduces the problems of inorganic scaling and organic pollution of a rear-end membrane.
In a preferred embodiment, the nanofiltration system comprises a first nanofiltration system and a second nanofiltration system, the first nanofiltration system comprises a roll-type nanofiltration membrane module, and the second nanofiltration system comprises a disk-tube nanofiltration membrane module. In the nanofiltration stage, a conventional roll type nanofiltration membrane component is firstly adopted for primary concentration, and roll type nanofiltration concentrated water which is concentrated by five times enters a disc tube type nanofiltration membrane component for further concentration by four times.
In a preferred embodiment, the concentrated water outlet end of the first nanofiltration system is connected with the water inlet end of the second nanofiltration system, the concentrated water outlet end of the second nanofiltration system is connected with the water inlet end of the first evaporator, and the water outlet end of the first nanofiltration system and the water outlet end of the second nanofiltration system are connected with the water inlet end of the first reverse osmosis system. Concentrated water of the second nanofiltration system enters the first evaporator to be evaporated, and most of evaporated salt is divalent salt.
In a preferred embodiment, the water outlet end of the tubular ultrafiltration system is connected to the water inlet end of the first nanofiltration system.
In a preferred embodiment, the first reverse osmosis system comprises a wound reverse osmosis membrane module. The water produced by the first nanofiltration system and the water produced by the second nanofiltration system are mixed firstly and then enter the roll type reverse osmosis membrane component for preliminary primary concentration, and the produced water reaches the standard for recycling.
In a preferred embodiment, the second reverse osmosis system comprises a permeate assisted reverse osmosis membrane module. Concentrated water of the first reverse osmosis system enters the osmosis auxiliary reverse osmosis membrane component, and after further concentration, part of the concentrated water flows back to the water production side of the osmosis auxiliary reverse osmosis membrane component to reduce the osmotic pressure difference at two sides of the membrane.
In a preferred embodiment, the pharmaceutical waste water zero-salt-discharge treatment system further comprises a second evaporator, and the concentrated water outlet end of the second reverse osmosis system is connected with the water inlet end of the second evaporator. And (4) the concentrated water of the deeply concentrated permeation auxiliary reverse osmosis membrane component enters a second evaporator for evaporation and crystallization to generate monovalent salt.
The utility model relates to a pharmaceutical waste water salt-separation zero-discharge treatment system, which mainly adopts a combined process of pretreatment, nanofiltration, reverse osmosis and an evaporator to treat pharmaceutical waste water, wherein a nanofiltration production section adopts a roll-type nanofiltration membrane component and a disc-tube nanofiltration membrane component to carry out segmented salt separation concentration treatment, the nanofiltration production section can intercept most of divalent salt and organic matters with large molecular weight, when the solute concentration of the waste water is lower, the roll-type nanofiltration membrane component with higher economy but common pollution resistance is adopted to carry out primary concentration, the solute concentration of the waste water is improved, and then the disc-tube nanofiltration membrane component with stronger pollution resistance is utilized to further concentrate, so that the economy is improved as much as possible while the operation stability of the membrane is ensured, and the investment and the operation cost are reduced; the reverse osmosis production section adopts a roll type reverse osmosis membrane component and an osmosis auxiliary reverse osmosis membrane component, and the osmosis auxiliary reverse osmosis membrane component is adopted to reduce the osmotic pressure difference of two sides of the membrane through refluxing partial concentrated water, so that a higher concentration multiple is achieved under lower additional driving force, and the operation cost of a rear-end evaporator stage is reduced under the operation cost of a reverse osmosis stage, so that the process is a better pharmaceutical waste water salt concentration process with long-term economical efficiency.
Drawings
The accompanying drawings are included to provide a further understanding of the embodiments and are incorporated in and constitute a part of this specification. The drawings illustrate embodiments and together with the description serve to explain the principles of the utility model. Other embodiments and many of the intended advantages of embodiments will be readily appreciated as they become better understood by reference to the following detailed description. The elements of the drawings are not necessarily to scale relative to each other. Like reference numerals designate corresponding similar parts.
Fig. 1 is a schematic diagram of a pharmaceutical waste water zero-salt-release treatment system according to an embodiment of the utility model.
Detailed Description
In order to make the objects, technical solutions and advantages of the present invention clearer, the present invention will be described in further detail with reference to the accompanying drawings, and it is apparent that the described embodiments are only a part of the embodiments of the present invention, not all of the embodiments. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention.
The utility model will be described in detail with reference to fig. 1, and the pharmaceutical wastewater salt-free zero-discharge treatment system of the utility model comprises a pretreatment system, pharmaceutical wastewater is conveyed to the pretreatment system for treatment, a water outlet end of the pretreatment system is connected with a water inlet end of a nanofiltration system, a concentrated water outlet end of the nanofiltration system is connected with a water inlet end of a first evaporator 6, a water outlet end of the nanofiltration system is connected with a water inlet end of a first reverse osmosis system 7, a concentrated water outlet end of the first reverse osmosis system 7 is connected with a water inlet end of a second reverse osmosis system 8, a water outlet end of the second reverse osmosis system 8 is connected with a water inlet end of the first reverse osmosis system 7, and a concentrated water outlet end of the second reverse osmosis system 8 is connected with a water outlet end of the second reverse osmosis system 8.
In a specific embodiment, the pretreatment system comprises a biochemical system 1, a tubular ultrafiltration system 2 and a hardness removal device 3, wherein the water outlet end of the biochemical system 1 is connected with the water inlet end of the hardness removal device 3, and the water outlet end of the hardness removal device 3 is connected with the water inlet end of the tubular ultrafiltration system 2. The pretreatment system mainly removes colloid and suspended matters, and reduces the problems of inorganic scaling and organic pollution of a rear-end membrane. If the hardness of the produced water of the biochemical system 1 is not high, the hardness removing device 3 can be arranged between the roll-type nanofiltration membrane component and the disc-tube nanofiltration membrane component, and the hardness in the wastewater is concentrated by the roll-type nanofiltration membrane component and then removed, so that the hardness removing efficiency is improved, and the operation dosing cost is reduced.
In a specific embodiment, the nanofiltration system comprises a first nanofiltration system 4 and a second nanofiltration system 5, the first nanofiltration system 4 comprises a roll-type nanofiltration membrane assembly, the second nanofiltration system 5 comprises a disc-tube-type nanofiltration membrane assembly, the water outlet end of the tube-type ultrafiltration system 2 is connected with the water inlet end of the first nanofiltration system 4, the concentrated water outlet end of the first nanofiltration system 4 is connected with the water inlet end of the second nanofiltration system 5, the concentrated water outlet end of the second nanofiltration system 5 is connected with the water inlet end of the first evaporator 6, and the water outlet ends of the first nanofiltration system 4 and the water outlet end of the second nanofiltration system 5 are connected with the water inlet end of the first reverse osmosis system 7.
The water produced by the tubular ultrafiltration system 2 enters the first nanofiltration system 4, namely, the conventional roll-type nanofiltration membrane component is primarily concentrated, and the concentrated water of the first nanofiltration system 4 after being concentrated five times enters the second nanofiltration system 5, namely, the disc-tube nanofiltration membrane component which is more resistant to pollution is further concentrated four times. Concentrated water of the disc-tube nanofiltration membrane component enters the first evaporator 6 to be evaporated, salt produced by evaporation is mostly divalent salt, and the salt produced by evaporation can still be mixed with organic matters due to higher content of organic components in pharmaceutical wastewater, so that the salt purity is limited. And the produced water of the first nanofiltration system 4 and the produced water of the second nanofiltration system 5 are mixed and then enter a reverse osmosis system of the next stage.
In a specific embodiment, the first reverse osmosis system 7 comprises a roll-type reverse osmosis membrane module, the second reverse osmosis system 8 comprises a permeation auxiliary reverse osmosis membrane module, and a concentrated water outlet end of the second reverse osmosis system 8 is connected with the second evaporator 9. The water produced by the first nanofiltration system 4 and the water produced by the second nanofiltration system 5 are mixed and then enter the roll type reverse osmosis membrane component for preliminary concentration, and the produced water is recycled after reaching the standard. The concentrated water of the first reverse osmosis system 7 enters the osmosis auxiliary reverse osmosis membrane component, and after further concentration, part of the concentrated water flows back to the water production side of the osmosis auxiliary reverse osmosis membrane component to reduce the osmotic pressure difference at the two sides of the membrane. The concentrated water of the permeation auxiliary reverse osmosis membrane component after deep concentration enters a second evaporator 6 for evaporation and crystallization. Most organic matters are intercepted in the nanofiltration production section and enter the reverse osmosis production section to be basically a pure salt system, so the salt production purity of the second evaporator 6 can reach a higher level, and the resource recycling of salt is realized. And the produced water of the osmosis auxiliary reverse osmosis membrane component cannot reach the standard for recycling due to mixing with part of concentrated solution of the unit, so that the produced water of the mixed osmosis auxiliary reverse osmosis membrane component returns to the front end of the roll type reverse osmosis membrane component, thereby achieving the closed loop of the process.
The utility model relates to a pharmaceutical waste water salt-separation zero-discharge treatment system, which mainly adopts a combined process of pretreatment, nanofiltration, reverse osmosis and an evaporator to treat pharmaceutical waste water, wherein a nanofiltration production section adopts a roll-type nanofiltration membrane component and a disc-tube nanofiltration membrane component to carry out segmented salt separation concentration treatment, the nanofiltration production section can intercept most of divalent salt and organic matters with large molecular weight, when the solute concentration of the waste water is lower, the roll-type nanofiltration membrane component with higher economy but common pollution resistance is adopted to carry out primary concentration, the solute concentration of the waste water is improved, and then the disc-tube nanofiltration membrane component with stronger pollution resistance is utilized to further concentrate, so that the economy is improved as much as possible while the operation stability of the membrane is ensured, and the investment and the operation cost are reduced; the reverse osmosis production section adopts a roll type reverse osmosis membrane component and an osmosis auxiliary reverse osmosis membrane component, and the osmosis auxiliary reverse osmosis membrane component is adopted to reduce the osmotic pressure difference of two sides of the membrane through refluxing partial concentrated water, so that a higher concentration multiple is achieved under lower additional driving force, and the operation cost of a rear-end evaporator stage is reduced under the operation cost of a reverse osmosis stage, so that the process is a better pharmaceutical waste water salt concentration process with long-term economical efficiency.
While the principles of the utility model have been described in detail in connection with the preferred embodiments thereof, it will be understood by those skilled in the art that the foregoing embodiments are merely illustrative of exemplary implementations of the utility model and are not limiting of the scope of the utility model. The details of the embodiments are not to be interpreted as limiting the scope of the utility model, and any obvious changes, such as equivalent alterations, simple substitutions and the like, based on the technical solution of the utility model, can be interpreted without departing from the spirit and scope of the utility model.
Claims (8)
1. The pharmaceutical wastewater salt zero-emission treatment system is characterized by comprising a pretreatment system, pharmaceutical wastewater is conveyed to the pretreatment system for treatment, the water outlet end of the pretreatment system is connected with the water inlet end of a nanofiltration system, the concentrated water outlet end of the nanofiltration system is connected with the water inlet end of a first evaporator, the produced water outlet end of the nanofiltration system is connected with the water inlet end of a first reverse osmosis system, the concentrated water outlet end of the first reverse osmosis system is connected with the water inlet end of a second reverse osmosis system, the produced water outlet end of the second reverse osmosis system is connected with the water inlet end of the first reverse osmosis system, and the concentrated water outlet end of the second reverse osmosis system is connected with the produced water outlet end of the second reverse osmosis system.
2. The pharmaceutical waste water zero-salt-release treatment system of claim 1, wherein the pretreatment system comprises a biochemical system, a tubular ultrafiltration system and a hardness removal device, wherein a water outlet end of the biochemical system is connected with a water inlet end of the hardness removal device, and a water outlet end of the hardness removal device is connected with a water inlet end of the tubular ultrafiltration system.
3. The pharmaceutical waste water and salt zero emission treatment system according to claim 2, wherein the nanofiltration system comprises a first nanofiltration system and a second nanofiltration system, the first nanofiltration system comprises a roll-type nanofiltration membrane module, and the second nanofiltration system comprises a disc-tube nanofiltration membrane module.
4. The pharmaceutical waste water salt zero-release treatment system according to claim 3, wherein a concentrated water outlet end of the first nanofiltration system is connected with a water inlet end of the second nanofiltration system, a concentrated water outlet end of the second nanofiltration system is connected with a water inlet end of the first evaporator, and a water outlet end of the first nanofiltration system and a water outlet end of the second nanofiltration system are connected with a water inlet end of the first reverse osmosis system.
5. The pharmaceutical waste water zero-salt-release treatment system according to claim 4, wherein the water outlet end of the tubular ultrafiltration system is connected with the water inlet end of the first nanofiltration system.
6. The pharmaceutical waste water salt zero-release treatment system of claim 1, wherein the first reverse osmosis system comprises a roll-to-roll reverse osmosis membrane module.
7. The pharmaceutical waste water zero-salt discharge treatment system of claim 1, wherein the second reverse osmosis system comprises a permeation assisted reverse osmosis membrane module.
8. The pharmaceutical waste water zero-salt-release treatment system of claim 1, further comprising a second evaporator, wherein the concentrated water outlet end of the second reverse osmosis system is connected with the water inlet end of the second evaporator.
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| CN202121603794.2U CN216472713U (en) | 2021-07-14 | 2021-07-14 | Pharmacy waste water salt zero release processing system |
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| CN202121603794.2U CN216472713U (en) | 2021-07-14 | 2021-07-14 | Pharmacy waste water salt zero release processing system |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN115259474A (en) * | 2022-08-23 | 2022-11-01 | 嘉戎技术(北京)有限公司 | Medical wastewater softening and hardness removing unit, treatment system and treatment method |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN115259474A (en) * | 2022-08-23 | 2022-11-01 | 嘉戎技术(北京)有限公司 | Medical wastewater softening and hardness removing unit, treatment system and treatment method |
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