CN112062222A - High enriched brine decompression concentration system - Google Patents
High enriched brine decompression concentration system Download PDFInfo
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- CN112062222A CN112062222A CN202011259856.2A CN202011259856A CN112062222A CN 112062222 A CN112062222 A CN 112062222A CN 202011259856 A CN202011259856 A CN 202011259856A CN 112062222 A CN112062222 A CN 112062222A
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
- B01D61/58—Multistep processes
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A20/00—Water conservation; Efficient water supply; Efficient water use
- Y02A20/124—Water desalination
- Y02A20/131—Reverse-osmosis
Abstract
The invention discloses a high-concentration brine pressure-reducing concentration system, which comprises a desalting concentration system and a pressure-reducing concentration system, wherein the desalting concentration system is used for desalting raw saline water to produce water, the pressure-reducing concentration system is used for reducing pressure difference concentration of the concentrated water produced by the desalting concentration system, part or all of the produced water of the pressure-reducing concentration system flows back to the desalting concentration system for desalting treatment again, the average membrane desalination rate of the pressure-reducing concentration system is less than the average membrane desalination rate of the desalting concentration system, and when the osmotic pressure of the concentrated water produced by the pressure-reducing concentration system is greater than the highest tolerance pressure of a semipermeable membrane in the pressure-reducing concentration system, the average membrane desalination rate of the pressure-reducing concentration system is less than the highest tolerance pressure of the semipermeable membrane in the pressure-reducing concentration system/the osmotic pressure of the concentrated water produced. According to the high-concentration brine pressure-reducing concentration system provided by the invention, the pressure behind each stage of membrane is fully utilized, the energy consumption is reduced, and the concentration effect of salinity is improved.
Description
Technical Field
The invention relates to the technical field of salinity recovery, in particular to a high-concentration brine pressure-reducing concentration system.
Background
In industrial production, industrial wastewater containing inorganic salt is generated, the salt content of the inorganic salt water is high, and part of organic matters are mixed, if the inorganic salt water is directly discharged into the natural environment, the water quality of ground water and underground water can be seriously damaged, simultaneously soil can be damaged, the pH value of the ground is greatly changed, and the growth of ground vegetation in a discharge area is damaged, so that the selection of a proper water treatment method for concentration, reuse and zero discharge treatment of the high-salt wastewater has very important practical significance. Although suspended matters, heavy metals and the like in high-salinity wastewater can be effectively removed through conventional chemical precipitation, coagulation clarification, filtration and the like, the suspended matters, the heavy metals and the like in the high-salinity wastewater are difficult to effectively removeRemove Na+、Cl-、Ca2+And Mg2+When the inorganic ions are dissolved, the salt content of the effluent is still high, the recycling is difficult, and the discharge causes serious pollution to the environment. Common desalination methods for salt-containing wastewater comprise reverse osmosis, electrodialysis, multiple-effect evaporation and the like, and although the common desalination methods have own advantages, the common desalination methods also have corresponding limitations, such as limited salt content of reverse osmosis and electrodialysis treatment, high multiple-effect evaporation investment and operation cost, and the action plan for preventing and treating water pollution (abbreviated as 'ten pieces of water') published by state hospitals in 2015 for 4 months, so that stricter requirements are provided for the treatment of various water body pollution; meanwhile, the national 'thirteen-five' plan further strictly controls the use of water resources and requires industrial production to recover and recycle wastewater generated in the production process as much as possible. In order to comply with relevant laws and regulations and relevant industrial policies, the development of novel treatment methods and systems are urgently needed for treating salt-containing wastewater.
At present, the conventional high-concentration brine reduction technology mainly adopts the processes of a semi-permeable membrane, Electrodialysis (ED), multi-effect evaporation and the like. The membrane process is generally used as primary concentration, brine is concentrated to the salt content of 5-6% of mass concentration, then the brine enters a deep concentration process to be used as primary concentration, the investment cost and the operation cost are low, however, due to the limited maximum withstand pressure of the membrane, the traditional membrane concentration can only concentrate the salt content to less than 10%, and the concentration is difficult to continue. The ED and multi-effect evaporation devices can further concentrate the reverse osmosis concentrated water, but the general investment cost and the operation cost are high. How to overcome the defect to further concentrate the wastewater and reduce the subsequent treatment cost becomes a problem to be solved urgently, so the system structure of the sampling process needs to be improved to solve the problems.
Disclosure of Invention
The invention aims to overcome the defects in the prior art and provide a high-concentration brine pressure-reducing concentration system, so that the pressure behind each stage of membrane is fully utilized, the energy consumption is reduced, and the concentration effect of salt is improved.
In order to achieve the above objects, the present invention provides, in one aspect, a high-concentration brine depressurizing and concentrating system comprising a desalting and concentrating system and a depressurizing and concentrating system, the desalination concentration system is used for desalinating raw saline water to produce water, the depressurization concentration system is used for depressurizing and concentrating concentrated water produced by the desalination concentration system, part or all of the produced water of the depressurization concentration system flows back to the desalination concentration system for desalination treatment again, the average membrane desalination rate of the depressurization concentration system is less than the average membrane desalination rate of the desalination concentration system, when the osmotic pressure of the concentrated water generated by the depressurization concentration system is more than the highest tolerance pressure of the semi-permeable membrane in the depressurization concentration system, the average membrane desalination rate of the depressurization concentration system is less than the highest withstand pressure of a semi-permeable membrane in the depressurization concentration system/osmotic pressure of concentrated water generated by the depressurization concentration system.
Further, the salt content of the concentrated water generated by the depressurization concentration system is more than 10%.
Furthermore, the pressure reduction concentration system comprises a plurality of pressure reduction concentration sections connected in series, the pressure reduction concentration section at the head end is used for carrying out pressure reduction difference concentration on the concentrated water generated by the desalination concentration system, the other pressure reduction concentration sections are sequentially used for carrying out pressure reduction difference concentration on the concentrated water generated by the previous pressure reduction concentration section, and part or all of the produced water generated by all the pressure reduction concentration sections flows back to the desalination concentration system for desalination treatment again.
Further, the average membrane desalination rate of the pressure reduction concentration section at the head end is less than that of the desalination concentration system, and the average membrane desalination rates of all the pressure reduction concentration sections are in a gradient decreasing relation from the head end to the tail end.
Further, when the osmotic pressure of the concentrated water generated by the next step-down concentration section is greater than the highest withstand pressure of the semi-permeable membrane of the next step-down concentration section, the average desalination rate of the membrane of the next step-down concentration section is less than the highest withstand pressure of the membrane of the next step-down concentration section/the osmotic pressure of the concentrated water generated by the next step-down concentration section.
Further, the depressurization concentration system comprises an intermediate section, the average membrane desalination rate of the intermediate section is less than the average membrane desalination rate of the desalination concentration system, the intermediate section is used for carrying out depressurization concentration on the concentrated water generated by the desalination concentration system, and part or all of the produced water of the intermediate section flows back to the desalination concentration system for carrying out desalination treatment again.
Furthermore, the interlude still includes the buffer pool, the product water of interlude flows into in the buffer pool, be provided with a plurality of water pumps that have response percentage flow in the buffer pool.
Furthermore, the depressurization concentration system also comprises a recovery section, wherein the average membrane desalination rate of the recovery section is less than the average membrane desalination rate of the middle section, the recovery section is used for carrying out depressurization and concentration on the concentrated water generated by the middle section, and part or all of the produced water of the recovery section flows back to the desalination concentration system for carrying out desalination treatment again.
Further, when the osmotic pressure of the concentrated water generated by the recovery section is greater than the highest withstand pressure of the semi-permeable membrane of the recovery section, the average membrane desalination rate of the recovery section is less than the highest withstand pressure of the semi-permeable membrane of the recovery section/the osmotic pressure of the concentrated water generated by the recovery section.
On the other hand, the invention also provides a high-concentration brine decompression and concentration system, which comprises a decompression and concentration system and a desalination and concentration system, the pressure-reducing concentration system is used for carrying out pressure-reducing difference concentration on the raw saline water, the desalination concentration system is used for carrying out desalination on the produced water of the pressure-reducing concentration system to produce water, part or all of the concentrated water generated by the desalination concentration system flows back to the pressure reduction concentration system for pressure reduction and concentration, the average membrane desalination rate of the depressurization concentration system is less than the average membrane desalination rate of the desalination concentration system, when the osmotic pressure of the raw water is greater than the highest withstand pressure of the semi-permeable membrane in the reduced-pressure concentration system, the average membrane desalination rate of the depressurization concentration system is less than the highest withstand pressure/osmotic pressure of the collected water of the raw water and the concentrated water returned by the desalination concentration system of the semi-permeable membrane in the depressurization concentration system.
Further, a water pump is arranged between the depressurization concentration system and the desalination concentration system.
Further, concentrated system of step-down includes the concentrated section of a plurality of step-down of establishing ties, is located the concentrated section of step-down is used for carrying out the step-down difference concentration to containing salt raw water, and remaining concentrated section of step-down is used for carrying out the step-down difference concentration to the dense water that the concentrated section of last section step-down produced in proper order, and the product water that all concentrated sections of step-down produced all flows to concentrated system of desalination carries out desalination.
Further, the average membrane desalination rate of the pressure reduction concentration section at the head end is less than that of the desalination concentration system, and the average membrane desalination rates of all the pressure reduction concentration sections are in a gradient decreasing relation from the head end to the tail end.
Further, when the osmotic pressure of the concentrated water generated by the next step-down concentration section is greater than the highest withstand pressure of the semi-permeable membrane of the next step-down concentration section, the average desalination rate of the membrane of the next step-down concentration section is less than the highest withstand pressure of the membrane of the next step-down concentration section/the osmotic pressure of the concentrated water generated by the next step-down concentration section.
Further, the pressure reduction concentration system comprises a middle section and a recovery section, wherein the middle section is used for carrying out pressure reduction concentration on the saline raw water; the recovery section is used for carrying out pressure drop concentration on produced water generated in the middle section, the average membrane desalination rate of the middle section is less than the average membrane desalination rate of the desalination concentration system, and the average membrane desalination rate of the recovery section is less than the average membrane desalination rate of the middle section.
Compared with the prior art, the invention has the beneficial effects that: this high enriched brine decompression concentration system has following benefit:
1. this high enriched brine concentrated system that steps down through providing the system architecture of handling step by step, has realized carrying out the concentrated effect of segmentation to the super high salt system, carries out segmentation processing step by step through adopting the membrane module of making by the semi-permeable membrane of high, medium, low desalination rate respectively for the osmotic pressure is far greater than the super high brine that conventional semi-permeable membrane maximum bearing pressure can realize concentrating under conventional pressure, innovative breakthrough the limitation that traditional membrane system can't concentrate.
2. This concentrated system of high enriched brine step-down can carry out desalination in succession to the number of circulation desalination section can superpose according to the salinity content in the waste water, and multistage concentration system in grades makes the membrane back pressure of each grade obtain abundant utilization, has reduced the energy consumption, has promoted the collection efficiency to the salinity simultaneously.
3. This concentrated system of high enriched salt water step-down controls the salt water osmotic pressure differential of each grade in the bearable within range of membrane module, has reduced the damage of membrane module, and the fault rate in the use is still less relatively, and life can promote, and the economic value of creation is higher, and market prospect is better.
Drawings
Fig. 1 is a process flow diagram of a first embodiment of the invention.
Fig. 2 is a specific process flow diagram of the first embodiment of the present invention.
FIG. 3 is a process flow diagram of a second embodiment of the present invention.
FIG. 4 is a flowchart illustrating a second embodiment of the present invention.
Detailed Description
The technical solutions in the embodiments of the present invention will be clearly and completely described below with reference to the drawings in the embodiments of the present invention, and it is obvious that the described embodiments are only a part of the embodiments of the present invention, and 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.
Referring to fig. 1-2, the present invention provides a technical solution:
the first embodiment is as follows:
a high-concentration brine pressure-reducing concentration system comprises a desalting concentration system and a pressure-reducing concentration system, wherein the desalting concentration system has high desalination rate to the brine raw water to be concentrated, the desalting concentration system comprises a plurality of membrane modules made of semi-permeable membranes with high desalination rate, the high desalination rate is defined as the semi-permeable membranes with desalination rate more than 90%, and the desalting concentration system is mainly used for desalting the brine raw water to produce water;
the pressure-reducing concentration system mainly carries out pressure-reducing differential concentration on raw water with ultrahigh salt content (salt water osmotic pressure > the maximum bearing pressure of a conventional membrane). The average membrane desalination rate of the depressurization concentration system is less than the average membrane desalination rate of the desalination concentration system, the depressurization concentration system is a membrane module made of a semi-permeable membrane with a medium desalination rate and/or a semi-permeable membrane with a low desalination rate, the medium desalination rate is defined as the semi-permeable membrane with the desalination rate of 50% -90%, and the low desalination rate is defined as the semi-permeable membrane with the desalination rate of 0% -50%, and the membrane module is used for carrying out depressurization and differential concentration on concentrated water produced by the desalination concentration system.
Neglecting the influence factors such as membrane concentration polarization, the osmotic pressure P is determined when the ion osmotic pressure exceeds 83barfThe ultra-high salt-containing raw water exists in a semi-permeable membrane or a membrane system with an average salt rejection rate R, so that the ultra-high salt-containing raw water can be separated and concentrated under an operating pressure P which is not higher than the highest withstand pressure (83 bar) of the traditional semi-permeable membrane, and the mathematical relationship between the ultra-high salt-containing raw water and the ultra-high salt-containing raw water can be summarized as follows: r< 83/Pf。
In this embodiment, it can be understood that when the osmotic pressure of the concentrated water generated by the pressure-reducing concentration system is greater than the highest tolerant pressure of the semi-permeable membrane in the pressure-reducing concentration system, and the average desalination rate of the membrane of the pressure-reducing concentration system is less than the highest tolerant pressure of the semi-permeable membrane in the pressure-reducing concentration system/the osmotic pressure of the concentrated water generated by the pressure-reducing concentration system, the saline raw water with the ultrahigh salt content, in which the ion osmotic pressure is far more than 83bar, can be concentrated, so that the back-end treatment cost is further reduced, and the salt content of the concentrated water generated by the pressure-reducing concentration system is greater than 10%.
The pressure reduction concentration system comprises a plurality of pressure reduction concentration sections connected in series, the pressure reduction concentration section at the head end is used for carrying out pressure reduction concentration on concentrated water generated by the desalination concentration system, the rest pressure reduction concentration sections are sequentially used for carrying out pressure reduction concentration on concentrated water generated by the last pressure reduction concentration section, and part or all of produced water generated by all the pressure reduction concentration sections flows back to the desalination concentration system for carrying out desalination treatment again. The average membrane desalination rate of the depressurization concentration section at the head end is less than the average membrane desalination rate of the desalination concentration system, the average membrane desalination rate of all the depressurization concentration sections is in a gradient decreasing relation from the head end to the tail end, the higher the osmotic pressure at the tail end along with the gradual concentration of the solution, the lower the required desalination rate, and the specific relation can be summarized as that when the osmotic pressure of the concentrated water generated by the next depressurization concentration section is greater than the highest withstand pressure of the semi-permeable membrane of the next depressurization concentration section, the average membrane desalination rate of the next depressurization concentration section is less than the highest withstand pressure of the membrane of the next depressurization concentration section/the osmotic pressure of the concentrated water generated by the next depressurization concentration section. In this embodiment, the depressurization concentration system preferably includes an intermediate stage having a membrane average desalination rate < a membrane average desalination rate of the desalination concentration system for conducting depressurization-difference concentration of the concentrate produced by the desalination concentration system, and a recovery stage having a membrane average desalination rate < a membrane average desalination rate of the intermediate stage for conducting depressurization-difference concentration of the concentrate produced by the intermediate stage, and when the osmotic pressure of the concentrate produced by the recovery stage is greater than the highest withstand pressure of the semipermeable membrane of the recovery stage, the membrane average desalination rate of the recovery stage < the highest withstand pressure of the semipermeable membrane of the recovery stage/the osmotic pressure of the concentrate produced by the recovery stage. Wherein the produced water of the middle section and the recovery section can partially or completely flow back to the desalination concentration system for desalination treatment again, and the control of the produced water flow and the salt content of the produced water is realized by adjusting the backflow percentage of the middle section and the recovery section. To achieve partial reflux, the flow rate can be controlled by a simple valve, or a buffer tank (not shown) can be provided at the water producing port of the intermediate and/or recovery sections, and a plurality of water pumps with response percent flow rate can be provided in the buffer tank to achieve a certain percent split.
To further demonstrate the beneficial effects achieved by the above lines, the raw water was concentrated at 8% salt and 14 m/h water yield.
In the experiment, raw water is pretreated and then pressurized to 83bar by a high-pressure plunger pump, and then enters a desalination concentration system for desalination, wherein the average desalination rate is 98.5 percent, the average water flux is 22.08L/H, the recovery rate is 28.27 percent, and the salt content of concentrated water is 9.39 percent; then concentrated water generated by the desalting concentration system enters an intermediate section for decompression concentration, the desalting rate of the intermediate section is 80%, the average water flux is 16.27L/H, the recovery rate is 29.04%, 90% of produced water flows back to the desalting concentration system for desalting treatment again, the rest 10% of produced water is converged with the produced water of the desalting concentration system, and the salt content of the concentrated water is 11.59%; the concentrated water in the middle section enters the final recovery section for further decompression and concentration, the desalination rate of the recovery section is 50%, the average water flux is 16.75L/H, the recovery rate is 14.05%, and the product is produced100% of the water flows back to the first stage for desalting treatment again, the salt content of the concentrated water is 12.14%, and the water content is 9.23m3And/h, the data in the measurement process is stable, and the concentration effect is good.
Example two:
the difference between the second embodiment and the first embodiment is that: in this embodiment, the positions of the desalination concentration system and the depressurization concentration system are interchanged, the raw saline water is firstly subjected to depressurization concentration, and the concentrated produced water is desalted and produced.
Referring to fig. 3 to 4, the high-concentration brine pressure-reducing concentration system in the embodiment includes a pressure-reducing concentration system and a desalination concentration system, the pressure-reducing concentration system is configured to perform pressure-reducing difference concentration on raw salt-containing water, the desalination concentration system is configured to perform desalination and water production on water produced by the pressure-reducing concentration system, all concentrated water produced by the desalination concentration system flows back to the pressure-reducing concentration system to perform pressure-reducing difference concentration, and an average membrane desalination rate of the pressure-reducing concentration system is less than an average membrane desalination rate of the desalination concentration system. Due to the position exchange of the depressurizing concentration system and the desalting concentration system, the mathematical induction formula in the first embodiment can be understood in the present embodiment as that when the osmotic pressure of the raw water is greater than the highest withstand pressure of the semi-permeable membrane in the depressurizing concentration system, the membrane average desalting rate of the depressurizing concentration system is less than the highest withstand pressure of the semi-permeable membrane in the depressurizing concentration system/the osmotic pressure of the collected water of the raw water and the concentrated water returned by the desalting concentration system. The method can realize concentration of the saline raw water with ultrahigh salt content and far exceeding 83bar of ion osmotic pressure, further reduce the cost of rear-stage treatment, and the salt content of the concentrated water generated by the pressure reduction concentration system is more than 10%.
Furthermore, a water pump is arranged between the pressure reduction concentration system and the desalination concentration system, so that produced water of the pressure reduction concentration system can be conveniently sent into the desalination concentration system.
Similarly, concentrated system of step-down also includes the concentrated section of a plurality of step-down of establishing ties in this embodiment, and the concentrated section of step-down that is located the head end is used for carrying out the step-down difference concentration to containing salt raw water, and remaining step-down concentrated section is used for carrying out the step-down difference concentration to the dense water that last step-down concentrated section produced in proper order, and the product water that all step-down concentrated sections produced all flows to concentrated system of desalination and carries out desalination. The average membrane desalination rate of the pressure reduction concentration section at the head end is less than that of the desalination concentration system, and the average membrane desalination rate of all the pressure reduction concentration sections is in a gradient decreasing relation from the head end to the tail end. Specifically, it can be understood that: when the osmotic pressure of the concentrated water generated by the next decompression concentration section is greater than the highest withstand pressure of the semi-permeable membrane of the next decompression concentration section, the average desalination rate of the membrane of the next decompression concentration section is less than the highest withstand pressure of the membrane of the next decompression concentration section/the osmotic pressure of the concentrated water generated by the next decompression concentration section.
Preferably, the depressurization concentration system in the embodiment comprises an intermediate section and a recovery section, wherein the intermediate section is used for carrying out depressurization concentration on the raw water containing salt; the recovery section is used for carrying out pressure drop concentration on the produced water generated in the middle section, the average membrane desalination rate of the middle section is less than that of the desalination concentration system, and the average membrane desalination rate of the recovery section is less than that of the middle section. To further demonstrate the beneficial effects achieved by the above lines, the raw water was concentrated at 8% salt and 14 m/h water yield.
In the experiment, raw water is pretreated and then is pressurized to 50bar by a high-pressure pump, and then enters a pressure reduction concentration system for pressure reduction concentration, wherein the average desalination rate is 34 percent, the average water flux is 25LMH, the recovery rate is 52.3 percent, and the salt content of concentrated water is 11.4 percent;
the salt content of the produced water of the depressurization concentration system is about 5.4 percent, the produced water enters a desalination concentration system for desalination concentration, the desalination rate is 99 percent, the average water flux is 14LMH, the recovery rate is 40.1 percent, and the produced water reaches the standard and is discharged or reused as circulating make-up water or as make-up water of other subsequent advanced treatment units; the salt content of the concentrated water is 9.0 percent, the concentrated water flows back to the front end to be converged with the raw water, and then enters the pressure reduction concentration system again for pressure reduction concentration.
When the depressurization concentration system comprises a plurality of membrane modules with different desalination rates, concentrating the raw water with the salt content of 8% and the water yield of 14m for cultivation/h.
The raw water is pretreated and then is pressurized to 50bar by a high-pressure pump, and then enters a pressure reduction concentration system for pressure reduction concentration, wherein the pressure reduction concentration system comprises three sections of internal membrane modules with sequentially reduced average desalination rate: stages 1, 2 and 3, with specific average salt rejection, average water flux, recovery as shown in the following table:
the salt content of the produced water of the depressurization concentration system is about 5.4 percent, the produced water enters a desalination concentration system for desalination and concentration, the desalination rate of the desalination concentration system is 99 percent, the average water flux is 14LMH, the recovery rate is 40.1 percent, and the produced water reaches the standard and is discharged or reused as circulating make-up water or make-up water of other subsequent advanced treatment units; the salt content of the concentrated water is 9.0 percent, the concentrated water flows back to the front end to be converged with the raw water, and then enters the pressure reduction section again for pressure reduction and concentration.
Example three:
the difference between the third embodiment and the second embodiment is that: in this example, the osmotic pressure of the raw water exceeded the maximum tolerable pressure of the conventional membrane.
To further demonstrate the beneficial effects achieved by the above lines, the raw water was concentrated at a salinity of 12% and a water yield of 14 m/h.
In an experiment, after being pretreated, raw water is pressurized to 70bar by a high-pressure pump and then enters a pressure reduction concentration system for pressure reduction concentration, the average desalination rate is 60%, the average water flux is 10.5LMH, the recovery rate is 55%, the salt content of concentrated water is 16.6%, and the water content is 10.2m for carrying out thin film evaporation;
the produced water of the pressure reduction concentration system has the salt content of about 5.7 percent and enters a desalination concentration system for desalination concentration, the desalination rate is 99 percent, the average water flux is 14.2LMH, the recovery rate is 30 percent, and the produced water reaches the standard and is discharged or reused as circulating make-up water or as make-up water of other subsequent advanced treatment units; the salt content of the concentrated water is 8.2 percent, the concentrated water flows back to the front end to be converged with the raw water, and then the concentrated water enters the pressure reduction concentration system again for pressure reduction concentration.
The high-concentration brine pressure-reducing concentration system is pressurized by the pressure pump, water with certain pressure enters the inlet end of the desalting concentration system, when raw salt water passes through the component of the desalting semipermeable membrane under the pressure, one part of water can directly pass through the semipermeable membrane to form produced water which is collected by a pipeline and then discharged, the other part of concentrated water enters the pressure-reducing concentration system, and under the specific pressure, because the permeable membrane components in the pressure-reducing concentration system are arranged in a gradient manner, the osmotic concentration can be carried out under the condition of the high-concentration water, higher pressure is not needed, the consumption of energy in the desalting process is reduced, a plurality of sections can be arranged according to the needs to carry out continuous operation, the concentration effect is sequentially improved, the concentrated water with higher concentration is obtained, compared with the traditional process of concentration under the same pressure, the stability is better, and the damage of the semipermeable membrane component is not easy to cause, the service life is longer.
Although embodiments of the present invention have been shown and described, it will be appreciated by those skilled in the art that changes, modifications, substitutions and alterations can be made in these embodiments without departing from the principles and spirit of the invention, the scope of which is defined in the appended claims and their equivalents.
Claims (15)
1. The utility model provides a high enriched brine decompression concentration system which characterized in that: contain concentrated system of desalination and the concentrated system of decompression, the concentrated system of desalination is used for carrying out the desalination to the raw water that contains salt and produces water, concentrated system of decompression is used for carrying out the concentrated poor concentration of decompression to the dense water that concentrated system of desalination produced, the product water part or whole backward flow of concentrated system of decompression extremely concentrated system of desalination is once more carried out, the average desalination rate of membrane of concentrated system of decompression < the average desalination rate of membrane of concentrated system of desalination, work as the osmotic pressure of the dense water that concentrated system of decompression produced > when the highest withstand voltage of semi-permeable membrane in the concentrated system of decompression, the average desalination rate of membrane of concentrated system of decompression < the highest withstand voltage of semi-permeable membrane in the concentrated system of decompression/the osmotic pressure of the dense water that concentrated system of decompression produced.
2. The high-brine depressurization concentration system according to claim 1, wherein: the salt content of the concentrated water generated by the pressure reduction concentration system is more than 10 percent.
3. The high-brine depressurization concentration system according to claim 1, wherein: the pressure reduction concentration system comprises a plurality of pressure reduction concentration sections which are connected in series, the pressure reduction concentration section which is positioned at the head end is used for carrying out pressure reduction difference concentration on concentrated water generated by the desalination concentration system, the other pressure reduction concentration sections are sequentially used for carrying out pressure reduction difference concentration on the concentrated water generated by the previous pressure reduction concentration section, and part or all of produced water generated by all the pressure reduction concentration sections flows back to the desalination concentration system for carrying out desalination treatment again.
4. The high-brine depressurization concentration system according to claim 3, wherein: the average membrane desalination rate of the pressure reduction concentration section at the head end is less than that of the desalination concentration system, and the average membrane desalination rate of all the pressure reduction concentration sections is in a gradient decreasing relation from the head end to the tail end.
5. The high-brine depressurization concentration system according to claim 4, wherein: when the osmotic pressure of the concentrated water generated by the next decompression concentration section is greater than the highest withstand pressure of the semi-permeable membrane of the next decompression concentration section, the average desalination rate of the membrane of the next decompression concentration section is less than the highest withstand pressure of the membrane of the next decompression concentration section/the osmotic pressure of the concentrated water generated by the next decompression concentration section.
6. The high-brine depressurization concentration system according to claim 3, wherein: the pressure reduction concentration system comprises an intermediate section, the average membrane desalination rate of the intermediate section is less than the average membrane desalination rate of the desalination concentration system, the intermediate section is used for carrying out pressure reduction concentration on concentrated water generated by the desalination concentration system, and part or all of produced water of the intermediate section flows back to the desalination concentration system for carrying out desalination treatment again.
7. The high-brine depressurization concentration system according to claim 6, wherein: the intermediate section also comprises a buffer pool, the produced water of the intermediate section flows into the buffer pool, and a plurality of water pumps with response percentage flow are arranged in the buffer pool.
8. The high-brine depressurization concentration system according to claim 6, wherein: the pressure reduction concentration system also comprises a recovery section, wherein the average membrane desalination rate of the recovery section is less than the average membrane desalination rate of the middle section, the recovery section is used for carrying out pressure reduction concentration on concentrated water generated by the middle section, and part or all of produced water of the recovery section flows back to the desalination concentration system for carrying out desalination treatment again.
9. The high-brine depressurization concentration system according to claim 8, wherein: when the osmotic pressure of the concentrated water generated by the recovery section is greater than the highest tolerance pressure of the semi-permeable membrane of the recovery section, the average membrane desalination rate of the recovery section is less than the highest tolerance pressure of the semi-permeable membrane of the recovery section/the osmotic pressure of the concentrated water generated by the recovery section.
10. The utility model provides a high enriched brine decompression concentration system which characterized in that: contain concentrated system of step-down and concentrated system of desalination, concentrated system of step-down is used for carrying out the step-down difference concentration to the raw water that contains salt, concentrated system of desalination is used for right the product water of concentrated system of step-down is desalinated and is produced water, the concentrated water part that concentrated system of desalination produced or whole backward flow extremely concentrated system of step-down carries out the step-down difference concentration, the average desalination rate of membrane of concentrated system of step-down < the average desalination rate of membrane of concentrated system of desalination, when the osmotic pressure of raw water is greater than when the highest withstand pressure of the semi-permeable membrane in the concentrated system of step-down, the average desalination rate of membrane of concentrated system of step-down < the highest withstand pressure of the semi-permeable membrane in the concentrated system of step-down/the osmotic pressure of gathering of the concentrated water of raw.
11. The high-strength brine depressurizing and concentrating system according to claim 10, wherein: and a water pump is arranged between the pressure reduction concentration system and the desalination concentration system.
12. The high-strength brine depressurizing and concentrating system according to claim 10, wherein: the concentrated system that steps down includes the concentrated section of a plurality of step-downs of establishing ties, is located the concentrated section of step-down is used for carrying out the pressure reduction difference to containing salt raw water and concentrating, and remaining concentrated section of step-down is used for carrying out the pressure reduction difference concentration to the dense water that last concentrated section of step-down produced in proper order, and the production water that all concentrated sections of step-down produced all flows extremely the concentrated system that desalts carries out desalination.
13. The high-strength brine depressurizing and concentrating system according to claim 12, wherein: the average membrane desalination rate of the pressure reduction concentration section at the head end is less than that of the desalination concentration system, and the average membrane desalination rate of all the pressure reduction concentration sections is in a gradient decreasing relation from the head end to the tail end.
14. The high-strength brine depressurizing concentration system according to claim 13, wherein: when the osmotic pressure of the concentrated water generated by the next decompression concentration section is greater than the highest withstand pressure of the semi-permeable membrane of the next decompression concentration section, the average desalination rate of the membrane of the next decompression concentration section is less than the highest withstand pressure of the membrane of the next decompression concentration section/the osmotic pressure of the concentrated water generated by the next decompression concentration section.
15. The high-strength brine depressurizing and concentrating system according to claim 12, wherein: the pressure reduction concentration system comprises a middle section and a recovery section, wherein the middle section is used for carrying out pressure reduction concentration on the saline raw water; the recovery section is used for carrying out pressure drop concentration on produced water generated in the middle section, the average membrane desalination rate of the middle section is less than the average membrane desalination rate of the desalination concentration system, and the average membrane desalination rate of the recovery section is less than the average membrane desalination rate of the middle section.
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| CN202011259856.2A CN112062222A (en) | 2020-11-12 | 2020-11-12 | High enriched brine decompression concentration system |
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