CN112919670A - Condensed water recovery processing system and processing method thereof - Google Patents
Condensed water recovery processing system and processing method thereof Download PDFInfo
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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
- C02F9/00—Multistage treatment of water, waste water or sewage
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- 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
- C02F1/28—Treatment of water, waste water, or sewage by sorption
- C02F1/283—Treatment of water, waste water, or sewage by sorption using coal, charred products, or inorganic mixtures containing them
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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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- 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
- C02F1/66—Treatment of water, waste water, or sewage by neutralisation; pH adjustment
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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
- C02F2101/00—Nature of the contaminant
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- C02F2101/20—Heavy metals or heavy metal compounds
- C02F2101/203—Iron or iron compound
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- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
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- C02F2301/00—General aspects of water treatment
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Abstract
The invention relates to a condensed water recovery processing system, at least comprising: a condensed water delivery conduit; the pollutant removing subsystem is used for introducing the condensed water to be recovered and treated through the condensed water conveying pipeline under the condition that the condensed water is not reduced to the normal temperature and treating and removing pollutants at least comprising oil and/or iron in the condensed water; and the mixed ion exchange treatment subsystem is used for desalting the condensed water which is obtained after the treatment of the pollutant removal subsystem and is in a non-high-temperature state so as to enable the obtained effluent to reach the indexes of primary desalted water or secondary desalted water.
Description
Technical Field
The invention relates to the technical field of steam condensate recovery, in particular to a condensate recovery processing system and a condensate recovery processing method.
Background
At present, nearly 50% of condensed water in a steam heating system of large industrial mechanical equipment in most domestic enterprises is not completely recycled and utilized, and the loss of hundreds of millions of tons of water resources and the waste of heat are caused every year. Domestic water for thermal power generation and coal chemical industry is large in water consumption, a large amount of condensed water generated in the industrial production process can be sent back to a boiler or enters a water treatment device after exchanging heat with make-up water, so that the cost of fuel and water treatment is saved, and the consumption of the make-up water is reduced. However, the industrial steam condensation process cannot avoid the pollution of the process medium, and meanwhile, certain gas impurities are dissolved in the condensed water conveying process, so that the turbine condensed water and the carrier of the process condensed water, namely heat exchange equipment and a conveying pipeline, are corroded in the recycling process, and a large amount of condensed water cannot be recycled due to serious corrosion. Therefore, in order to save energy, reduce consumption and eliminate the pollution to the plant environment caused by the emission of secondary flash steam, an effective recovery system needs to be designed urgently, and the heat energy and the condensed water of the system are recovered to the greatest extent. In the condensed water formed after each production device uses steam in the industrial production process, when the content of impurities exceeds the standard, the condensed water cannot be directly reused in the desalted water. In order to stably reuse the condensed water for a long period, the condensed water is subjected to oil removal and iron removal treatment, and the treated condensed water can be used as demineralized water.
The conventional condensed water treatment process at present comprises the following steps: the process condensate water returned by chemical devices and other steam users is gathered to a water treatment station through a pneumatic pump and then enters a desalting and iron-removing system for treatment, and the process of the condensate water treatment process is as follows: condensed water coming → condensed water tank → condensed water pump → heat exchanger → high efficiency filter → composite membrane condensed water deironing and deoiling device → mixed bed ion exchanger → first/second stage demineralized water tank → demineralized water system pipe network, condensed water can be used as first or second stage demineralized water after the process flow (application of condensed water treatment and recycling technology of Zhang dragon. petrochemical plant [ J ]. industry, 2016, 000(007): P.31-31.). In the prior art, as proposed in patent document with publication number CN110642308A, a condensate integrated oil and iron removing process is provided, which comprises the steps of detecting condensate generated by a process device through an oil on-line analyzer, discharging the condensate with excessive oil content to an oil-containing sewage treatment system through a discharge system, and conveying the qualified condensate to a condensate raw water tank; the condensed water enters an integrated oil and iron removing device after being pressurized by a raw water pump, oil stains and iron in the condensed water are removed, and the produced water is detected by an oil on-line analyzer and then is conveyed to a product water tank; finally, the mixture is pumped by an external water pump to be conveyed out of the battery limits.
In the prior art, the condensate recovery processing system adopted by the patent documents adopts a conventional composite membrane condensate oil and iron removing process, and the recovered steam condensate is cooled and then subjected to oil and iron removal, so that the oil content in the low-temperature condensate can be reduced to a certain extent. However, in the conventional process for removing oil and iron from the condensed water of the composite membrane, the adopted common salt-removing anion resin resists temperature of 40 ℃, the heat-resistant anion resin generally does not exceed 70 ℃ at present, namely, the incoming water can enter the composite membrane after heat exchange and temperature reduction, so that not only is a heat source wasted, but also other energy-using equipment is required to be provided for heat exchange and temperature reduction, and the recovery and treatment cost of the condensed water is increased.
Furthermore, on the one hand, due to the differences in understanding to the person skilled in the art; on the other hand, since the inventor has studied a lot of documents and patents when making the present invention, but the space is not limited to the details and contents listed in the above, however, the present invention is by no means free of the features of the prior art, but the present invention has been provided with all the features of the prior art, and the applicant reserves the right to increase the related prior art in the background.
Disclosure of Invention
In the prior art, a condensate recovery processing system adopted by a condensate integrated oil and iron removing process, such as that proposed in patent document with publication number CN110642308A, adopts a conventional composite membrane condensate oil and iron removing process, and performs cooling processing on recovered steam condensate and then removes oil and iron, so that the oil content in low-temperature condensate can be reduced to a certain extent. However, in the conventional process for removing oil and iron from the condensed water of the composite membrane, the adopted common salt-removing anion resin resists temperature of 40 ℃, the operating temperature of the heat-resistant anion resin is generally not more than 70 ℃ at present, namely, the incoming water can enter the composite membrane after heat exchange and temperature reduction, so that not only is a heat source wasted, but also other energy-using equipment is required to be provided for heat exchange and temperature reduction, and the recovery and treatment cost of the condensed water is increased.
In view of the above-mentioned deficiencies of the prior art, the present invention provides a condensed water recycling system, which is characterized in that the system at least comprises: a condensed water delivery conduit; the pollutant removing subsystem is used for introducing the condensed water to be recovered and treated through the condensed water conveying pipeline under the condition that the condensed water is not reduced to the normal temperature and treating and removing pollutants at least comprising oil and/or iron in the condensed water; and the mixed ion exchange treatment subsystem is used for desalting the condensed water which is obtained after the treatment of the pollutant removal subsystem and is in a non-high temperature state so as to enable the obtained effluent to reach the indexes of primary desalted water or secondary desalted water. The application provides a can make full use of condensate water heat energy in order to reach the condensate water recovery processing system who reduces condensate water recovery processing cost by a wide margin, and this system allows high temperature condensate water not through heat transfer cooling with regard to direct entering to remove the pollutant subsystem, and this in-process condensate water warp closed transport can make the heat source loss minimize. Meanwhile, the system can fully utilize the high heat energy of the condensed water to promote the process benefits of oil removal, iron removal and the like of the pollutant removal subsystem, thereby realizing energy conservation and consumption reduction while ensuring the high-benefit operation of the pollutant removal subsystem, and greatly reducing the existing condensed water recovery and treatment cost. In addition, in the steam thermodynamic system of domestic large-scale petroleum and chemical industry, the amount of condensed water per hour of a medium-high pressure boiler mainly used at present can be from dozens of tons to hundreds of tons, and the medium-high pressure boiler is basically recovered in an open mode with low cost consumption and high pollution, so that the exhaust steam in a plant area often flows away. The condensed water recycling and treating system provided by the application adopts closed conveying to treat condensed water, avoids the problem of environmental pollution caused by the existing steam thermodynamic system, simultaneously keeps lower operation cost, has large energy-saving potential and strong popularization and application performance. The application provides a condensate recovery processing system, has not only strengthened the recycle ratio of the industrial steam condensate to reach the purpose that reduces water waste and calorific loss, can also furthest prolong industrial mechanical equipment's life.
According to a preferred embodiment, the pollutant removing subsystem can introduce the turbine condensate to be recycled and treated through the turbine condensate conveying pipeline under the condition that the turbine condensate is not reduced to the normal temperature and can treat and remove pollutants at least comprising oils and/or iron in the turbine condensate, and the mixed ion exchange treatment subsystem can carry out desalination treatment on the process condensate and the turbine condensate which are obtained after the treatment of the pollutant removing subsystem and are in a non-high temperature state. Utilize the condensate recovery processing system that this application provided, can realize the different initial treatment technology to condensate and turbine condensate, this system can distinguish promptly that the processing oil/iron class pollutant proportion is different and the coming water self temperature is different treats the recovery processing and comes the water, is favorable to realizing the high benefit of condensate recovery processing technology, can guarantee the water quality requirement of process water simultaneously.
The pollutant removing subsystem at least comprises a deironing filter, an oil removing filter and an active carbon filter device, and is used for removing pollutants such as iron and oil in condensed water respectively.
According to a preferred embodiment, the pollutant removing subsystem at least comprises a first pollutant removing device and a second pollutant removing device, and the first pollutant removing device intercepts pollutants in the incoming water in a mode different from that of the second pollutant removing device. The entrapment means referred to in this application may include one or more of adsorption, coalescence, mechanical retention, overlap, bridging.
According to a preferred embodiment, the first pollutant removing device can achieve the purpose of removing oil and iron from the incoming water in a manner that a main composite membrane in the device can self-regulate the membrane treatment capacity depending on the change of the temperature of the incoming water.
According to a preferred embodiment, the first pollutant removal device can achieve the purpose of removing oil and iron from the incoming water by means of a main composite membrane and a mechanical actuating mechanism thereof which cooperate to adjust the membrane treatment capacity of the first pollutant removal device depending on the temperature change of the incoming water.
According to a preferred embodiment, said first pollution-removal device is capable of obtaining at least two oil pollutants having different size distributions from each other, in such a way that its main composite membrane and its mechanical actuation mechanism cooperate in regulating its membrane treatment capacity depending on the variation of the temperature of the incoming water itself.
According to a preferred embodiment, the first pollutant removing device is provided with a temperature sensor for detecting the temperature of the internal environment thereof, and the mechanical actuating mechanism can adjust the operating parameters based on the internal environment temperature monitored by the temperature sensor so as to enable the mechanical acting force provided by the mechanical actuating mechanism to the incoming water to change correspondingly.
According to a preferred embodiment, the first pollutant removing device can utilize the main composite membrane to respectively obtain oil pollutants and iron pollutants through back washing after synchronously removing oil and iron. Most of composite membrane oil and iron removing devices proposed in the prior art cover wood fiber powder and activated carbon powder on a special porous key (filter element) by utilizing the bridging effect of filter materials, form a compact composite filter membrane on the surface of the filter element, enter low-temperature hot water to be treated into a pipe from the outside of the pipe through gaps of the filter membrane and the filter element, remove oil impurities and iron impurities at one time by means of comprehensive effects of a series of means such as mechanical retention, adsorption, overlapping, bridging and the like, however, the discharged waste liquid is mixed with the oil impurities and the iron impurities at the same time and is difficult to further recycle. Therefore, the treatment system provided by the application not only can meet the synchronous removal effect of the oil and iron pollutants, but also can realize the separate recovery of the oil and iron pollutants.
Preferably, the first pollutant removing device further comprises an oil pollutant collecting gap arranged outside the main composite membrane, and oil pollutants in the incoming water introduced into the main composite membrane can be intercepted by the main composite membrane and collected to the oil pollutant collecting gap.
The application also provides a condensate recovery processing system, includes at least: a condensed water delivery conduit; the pollutant removing subsystem is used for introducing the condensed water to be recovered and treated through the condensed water conveying pipeline under the condition that the condensed water is not reduced to the normal temperature and treating and removing pollutants at least comprising oil and/or iron in the condensed water; and the mixed ion exchange treatment subsystem is used for desalting the condensed water which is obtained after the treatment of the pollutant removing subsystem and is in a non-high temperature state so as to enable the obtained outlet water to reach the index of primary desalted water or secondary desalted water, wherein the pollutant removing subsystem at least comprises a first pollutant removing device and a second pollutant removing device which are used for removing iron pollutants or oil pollutants in the condensed water.
The application has still provided a condensate recovery processing system, includes first and second pollutant removal device at least, the first pollutant removal device accessible main complex film in its device relies on the change of coming water self temperature and the mode of self-regulation membrane throughput realizes the deoiling deironing purpose to coming water.
The application also proposes a condensate treatment method comprising at least one or several of the following steps: introducing the condensed water to be recycled through a condensed water conveying pipeline under the condition that the condensed water is not reduced to normal temperature; treating and removing pollutants at least comprising oil and/or iron in the condensate by using a pollutant removing subsystem; and a mixed ion exchange treatment subsystem is utilized to carry out desalination treatment on the condensate water which is obtained after the treatment of the pollutant removal subsystem and is in a non-high temperature state so as to enable the obtained effluent water to reach the index of primary desalted water or secondary desalted water. The application also provides a condensed water treatment method, which at least comprises the following steps: the purpose of removing oil and iron from the incoming water is achieved by a mode that the main composite membrane can self-regulate the membrane treatment capacity depending on the temperature change of the incoming water.
Drawings
FIG. 1 is a simplified process flow diagram of a condensate recovery processing system provided by the present invention;
FIG. 2 is a simplified process flow diagram of the contaminant removal subsystem provided by the present invention;
fig. 3 is a simplified structural schematic diagram of the composite membrane oil and iron removal device provided by the invention.
Detailed Description
The following discussion is a brief description of the concepts and terms involved in the present application for the understanding of those skilled in the art.
A turbine, also known as a turbine or a turbomachine, refers to a vane-type engine that converts energy contained in a fluid medium (such as gas, steam or water) into mechanical energy via a rotating vane. The most important part of the turbine is the rotating element (rotor or impeller) which is mounted on the turbine shaft and has blades arranged uniformly along its circumference. When the fluid with energy passes through the jet pipe, the energy is converted into kinetic energy, and when the fluid flows through the impeller, the fluid impacts the blades to push the impeller to rotate, so that the turbine shaft is driven to rotate, and mechanical work is output. Turbine can be divided into a water turbine (used as a power source of a hydropower station), a steam turbine (used for a thermal power plant, ship propulsion, and the like), a gas turbine (used as propulsion power of a jet plane, ship power, a power plant, a small power station for peak load, and the like), an air turbine (compressed air is used as a working medium to drive the turbine to rotate, and only can be used as micro power), and the like according to different fluid media.
EDI technology, Electrodeionization, is a continuous Electrodeionization technology, which is a novel water treatment method that fills mixed-bed resin between ion exchange membranes and realizes continuous desalination under the action of a direct current electric field. The most critical parts of the EDI technology are: h produced by water ionization+Ions and OH-The ion exchange resin is continuously regenerated by the ions, and a layer of fresh resin which is continuously regenerated is reserved at the outlet of the E DI equipment for a long time by utilizing the key process of water ionization and resin regeneration, so that the quality of the effluent water is kept good for a long time. The EDI system mainly comprises an anion/cation exchange membrane, a concentrated water chamber, a positive electrode, a negative electrode and anion/cation exchange resin, and the main working principle is as follows: by means of the ion exchange effect of the ion exchange resin and the selective permeation effect of the anion exchange membrane and the cation exchange membrane to anions and cations, the ion directional migration is realized under the action of a direct current electric field, and thus the deep desalination of water is completed. The membrane and resin are associated with water due to ion exchange, ion transfer and electrical regeneration of the ion exchange resinThe ionization of the water is continuously carried out on the interface of the water generating device, and H generated by the ionization+And OH-The ions continuously regenerate the ineffective ion exchange resin, so that a protective layer consisting of fresh resin is formed at the bottom of the resin layer, and the effluent quality of the EDI equipment is good. Like a mixed ion exchanger working while regenerating, can continuously produce high quality pure water, and thus EDI is also called a continuous electrically regenerating mixed bed.
Example 1
The embodiment proposes a condensed water recycling system as shown in fig. 1, which is specifically as follows:
1. and the condensate water pretreatment unit is used for collecting process condensate water recovered by a chemical device and returned by other steam users, and cooling the process condensate water through a condensate water heat exchange station arranged in the condensate water pretreatment unit. And conveying the process condensate to a process condensate water tank connected with the condensate water heat exchange station under the condition that the temperature of the process condensate water is not higher than 50 ℃. The process condensate water in the process condensate water tank can be pressurized and conveyed to the next processing unit by the process condensate water pump.
2. And the iron removal filtering treatment unit is used for removing iron from the process condensate water obtained after the heat exchange and temperature reduction treatment, so that iron pollutants and suspended impurities in the process condensate water can be removed. The iron impurities in the process condensate water are mainly from steel pipes for conveying the condensate water, corrosion products of the iron impurities bring iron pollutants, the iron pollutants entering the process condensate water mainly exist in the form of particles and colloidal state and are few in dissolved state, the particle size of the iron pollutants is usually more than several microns, and the iron impurities can be removed by adopting an iron removal filtering unit. The deironing filtration processing unit can adopt a storage tank type deironing filter made of filter materials (such as manganese sand and quartz sand), and iron can be filtered when process condensate water passes through the filter materials.
3. And the intercepting and deoiling treatment unit is used for carrying out deoiling intercepting treatment on the process condensate water obtained after the deironing treatment, so that oil pollutants or other related organic matters in the process condensate water can be removed. The oil impurities in the process condensate water are mainly polluted by oil in different degrees in the process condensate water caused by pipeline leakage and the like. The intercepting and deoiling treatment unit can adopt an intercepting oil-water separation membrane formed by special functional fibers to realize the separation of hydrophobic dispersoids in water. The oil-water separating barrier film has extremely strong oil-repelling property. When the process condensed water containing oil pollutants is to penetrate through the activated oil-water separation blocking membrane, proper pressure is applied to the process condensed water, water molecules on the incoming water side can be replaced and penetrated with water molecules in the membrane, and hydrophobic dispersoids such as oil pollutants and the like are selectively blocked because the hydrophobic dispersoids cannot be replaced with associated water in the membrane, so that oil-water separation is realized. Intercepting and deoiling treatment process flow: the water firstly enters a contact coagulation high-speed filter, passes through a porous ceramic filler layer in a tank in a downward flow mode, effectively filters suspended impurities in the sewage, and carries out surface contact adsorption and coagulation on oil particles (high mechanical dispersed oil and emulsified oil) in a high dispersion mode in the water to form coarse particles; the effluent of the filter enters the intercepting oil-water separator under self pressure, an intercepting oil-water separation membrane is arranged in the tank, the sewage entering the intercepting oil-water separator forms a large-scale circulating flow state in the tank under the action of a forced water flow circulating machine, and a part of the sewage circulating in the tank intercepts the oil-water separation membrane and is collected in a water purifying chamber at the bottom of the tank, flows out of a water outlet pipe and is conveyed to the next treatment unit by utilizing the selective intercepting function of the intercepting oil-water separation membrane, wherein the water passing is not excessive. The deoiled water can be directly conveyed to a biochemical treatment tank, or can enter a primary air floatation tank for protective treatment and then enter a sewage biochemical treatment system.
4. The active carbon filtration treatment unit is used for further treating pollutants in the process condensate water obtained after the interception and oil removal treatment, and can further reduce oil pollutants or other related organic matters in the process condensate water. The active carbon filtering treatment unit completes pollutant treatment mainly through carbon bed. The active carbon particles forming the carbon bed have very many micropores and huge specific surface area, and have very strong physical adsorption capacity. As the process condensate passes through the carbon bed, oil contaminants or other related organics in the process condensate are adsorbed to the activated carbon. In addition, the non-crystalline part of the surface of the activated carbon has some oxygen-containing functional groups, so that the oil pollutants in the process condensate passing through the carbon bed can be effectively adsorbed by the activated carbon. The active carbon filtration treatment is beneficial to ensuring the service life of the post-stage unit.
5. The turbine condensate water pretreatment unit collects turbine condensate water recovered by a chemical device into a turbine condensate water tank, and the turbine condensate water in the turbine condensate water tank can be pressurized and conveyed to the next treatment unit through a turbine condensate water pump.
6. And the precise filtering treatment unit is used for removing iron and intercepting and deoiling the turbine condensate water, and can remove iron pollutants and suspended impurities in the turbine condensate water.
7. And the mixed ion exchange treatment unit is used for obtaining primary pure water meeting the inlet water quality requirement of primary desalted water after being treated by the activated carbon filtration treatment unit and the precise filtration treatment unit, wherein anions and cations of salts contained in the primary pure water pass through the mixed ion exchange treatment unit to be exchanged by resin, and qualified condensate water is produced and is conveyed into a desalted water tank of the full-membrane chemical water treatment station.
And the clean wastewater such as ultrafiltration backwashing wastewater, reverse osmosis device cleaning wastewater, self-cleaning filter backwashing water, factory sampled water, EDI system unqualified discharge water and the like obtained in the treatment process are uniformly discharged into a reuse water tank, and are distributed to a reuse water ultrafiltration device of a full-membrane chemical water treatment station through a reuse water pump part or are sent out of a boundary area to an ethylene third cycle plant.
Wherein the positive washing water generated by the mixed ion exchange treatment unit is conveyed back to the process condensed water tank in the condensed water pretreatment unit.
Wherein, acid and alkali regeneration waste liquid generated in the treatment process is completely discharged to a neutralization tank, and is discharged to a sewage treatment plant by a neutralization water pump after neutralization. Backwash water obtained by ultrafiltration of reuse water, chemical cleaning water obtained by ultrafiltration and reverse osmosis, and chemical cleaning water obtained by an electric demineralizer are discharged to a neutralization tank and discharged to a sewage treatment plant by a corresponding wastewater pump.
Wherein, the concentrated water of the concentrated water reverse osmosis is directly sent out by utilizing the residual pressure or sent to a periodic pollution discharge cooling pool.
And backwashing oily sewage and the like generated in the iron removal filtering treatment unit, the oil interception and removal treatment unit and the activated carbon filtering treatment unit are discharged into an oily sewage tank and are pumped out of the oil tank to a sewage treatment plant through an oily sewage pump.
Wherein, a pH analyzer is arranged on an outlet pipeline of the neutralization water pump, and the neutralization tank can automatically add acid and alkali liquor according to the pH value so as to maintain the pH value of the discharged water at 6.5-8.5.
Example 2
This embodiment may be a further improvement and/or a supplement to embodiment 1, and repeated contents are not described again. The preferred embodiment of example 1 can be supplemented in whole and/or in part by this example without causing conflicts or inconsistencies.
This embodiment has proposed a condensate recovery processing system, and this system can mainly be provided with complex film deoiling deironing device. The embodiment also provides a condensed water treatment method, a condensed water oil-removing and iron-removing process or a condensed water oil-removing and iron-removing device. The composite membrane oil and iron removal device mainly comprises a first pollutant removal device and a second pollutant removal device which are connected with each other. The water is firstly treated primarily by a first pollutant removing device to remove most of oil pollutants and iron pollutants, and the primarily treated effluent treated by the main composite membrane enters a second pollutant removing device for desalination treatment, so that a small amount of residual oil pollutants and iron pollutants in the primarily treated effluent are completely removed. Under the arrangement, most of oil pollutants and iron pollutants can be removed in advance by the aid of the first pollutant removing device, and on one hand, the first pollutant removing device is long in service cycle and can fully utilize the high-temperature characteristic of water to realize energy conservation and low consumption; on the other hand, for the short and limited single complex film deoiling deironing equipment that only adopts of complex film change cycle that faces among the prior art, this application has alleviateed the unit of second pollutant removal device and has handled the burden volume, and second pollutant removal device receives the pollution speed and change cycle and all greatly reduce for complex film deoiling deironing device can realize longer life cycle when satisfying the water quality requirement of the play water after handling, is favorable to reducing the condensate recovery processing system cost.
The first pollutant removing device can self-regulate the membrane treatment capacity of the device depending on the temperature change of the incoming water, thereby achieving the purpose of removing oil and iron from the incoming water. The first pollutant removing device has a cylindrical treatment part composed of a main composite membrane, and incoming water introduced into the cylindrical treatment part can directly contact with the main composite membrane to transfer heat, so that the main composite membrane can self-regulate membrane treatment capacity depending on the change of the temperature of the incoming water. At least part of oil pollutants and at least part of iron pollutants in the incoming water introduced into the first pollutant removing device can be intercepted by the main composite membrane and are left in the treatment process stage of the main composite membrane, and the first pollutant removing device can output the incoming water after the incoming water is subjected to oil removing and iron removing treatment.
After the incoming water is introduced into the first pollutant removing device, the oil pollutants in the incoming water can be intercepted and separated by the main composite membrane. The first pollutant removing device can obtain the oil pollutants intercepted in the water in the treatment process stage of the main composite membrane in the oil pollutant collecting gap arranged on the first pollutant removing device. The oil contaminant collecting gap is disposed outside the main composite membrane. The oil contaminant collecting gap surrounds the main composite membrane to form an outer sleeve-like structure. At least part of the oil pollutants in the incoming water can be trapped by the main composite membrane and collected to the oil pollutant collecting gap. The primary composite membrane is configured to allow one-way passage of oil contaminants but not water molecules. The main composite membrane can be mainly prepared from a high polymer material with temperature-sensitive performance.
After the incoming water in a very warm state is introduced into the first pollutant removing device, the temperature of the incoming water is higher in the initial stage, and the oil pollutants which belong to the same size distribution in the incoming water can be intercepted by the main composite membrane. In the later period, along with the proceeding of the main composite membrane treatment process, the temperature of the incoming water is gradually reduced, and the main composite membrane can further intercept oil pollutants belonging to the other size distribution. Namely, the temperature of the incoming water in a very warm state is gradually reduced, so that the main composite membrane can intercept oil pollutants in different size distributions.
Under the condition of changing the ambient temperature condition, the conformation of the polymer molecular chain in the main composite membrane is changed, so that the volume of the polymer in the main composite membrane is changed, the pore size of a membrane channel is changed, and the membrane flux and/or the intercepted target volume of the main composite membrane are influenced. Preferably, the pore size of the membrane channels in the main composite membrane may be positively or negatively correlated with ambient temperature conditions. Further preferably, the pore size of the membrane channel in the main composite membrane is in positive correlation with the ambient temperature condition. Under the condition that the ambient temperature condition is changed, the main composite membrane does not allow water molecules to pass through all the time. Preferably, the main composite membrane can be configured with a polymer material with super-hydrophobic property.
The main composite membrane has a certain attraction effect on the oil pollutants in the water, however, in the cylindrical structure, only depending on the small acting force, for most of the oil pollutants in the water, the main composite membrane is difficult to be contacted with, and is difficult to be actively trapped by the main composite membrane so as to be separated to the oil pollutant collecting gap. In this respect, in the present application, the main composite membrane forms a certain attraction effect on the oil pollutants in the incoming water, and the main composite membrane and the incoming water provide a mechanical actuating force to jointly realize the interception of most of the oil pollutants.
The cylindrical treatment part formed by the main composite membrane is connected with the mechanical actuating mechanism, and the mechanical actuating mechanism can drive the cylindrical treatment part to rotate relatively, so that oil pollutants and iron pollutants in incoming water in the cylindrical treatment part are subjected to the action of centrifugal force, and the contact chance between the cylindrical treatment part and the main composite membrane is increased.
After the incoming water is introduced into the first pollutant removing device, the mechanical actuating mechanism provides mechanical actuating acting force for the incoming water, oil pollutants and iron pollutants in the incoming water are subjected to centrifugal force, and the oil pollutants and the iron pollutants can be intercepted and separated by the main composite membrane.
In the event of a change in ambient temperature conditions, the amount of mechanical actuation force provided by the mechanical actuation mechanism to the incoming water changes. The mechanical actuating mechanism utilizes a temperature sensor to realize the temperature-sensitive performance of the mechanical actuating mechanism. The temperature sensor may detect the internal ambient temperature of the cylindrical processing portion, and feed back the detected temperature data to the mechanical actuation mechanism. The mechanical actuating structure is configured to adjust the operation parameters of the structure thereof in accordance with the change of the temperature of the incoming water, so that the mechanical actuating force provided by the mechanical actuating structure to the incoming water is changed.
Under the condition that the mechanical actuating mechanism operates, the volume size distribution ranges of different oil pollutants in the running water are different, namely, the centrifugal force applied to the different oil pollutants is different. The centrifugal force is much greater than the gravitational force. Substances with different specific gravities are subjected to different centrifugal forces. The mechanical actuating mechanism can regulate and control the time of different oil pollutants contacting the main composite membrane. Under the condition that the centrifugal force is relatively small, the oil pollutants with relatively large volume are subjected to relatively large centrifugal force and can contact the main composite membrane, and the oil pollutants with relatively small volume are subjected to relatively small centrifugal force and basically maintain the original positions of the oil pollutants. After the oil pollutants with relatively large volume are intercepted and separated by the main composite membrane, the centrifugal force action can be increased, and the oil pollutants with relatively small volume in the incoming water can be further intercepted and separated.
The first contaminant removing device can obtain oil contaminants with different size distributions from each other, so that one or more of floating oil, emulsified oil and dissolved oil in water can be separated. Preferably, the first contaminant removal device can separately obtain the floating oil and the emulsified oil in the incoming water, and most of the oil contaminants are only the incoming water with dissolved oil. The floating oil is the main component of oil pollutant in the water, for example, the floating oil in the waste water of oil refinery can account for about 60-80% of the oil content. The oil droplets of the tall oil have a large particle size, typically greater than 100 μm. The particle size of oil droplets of the emulsified oil is smaller, generally between 0.1 and 2 microns, and the emulsified oil refers to an oil substance which is difficult to separate from the wastewater after standing for a long time in the oily wastewater and can be separated only after being converted into floating oil through demulsification treatment. The oil bead diameter of the dissolved oil is smaller than that of the emulsified oil, and some oil beads can be as small as several nanometers and are oil particles dissolved in water. And the solubility of dissolved oils in water is very low, typically only a few milligrams per liter.
When the incoming water is introduced into the first pollutant removing device, the mechanical brake mechanism adjusts operation parameters based on the internal environment temperature detected by the temperature sensor, so that the incoming water and/or pollutants in the incoming water are subjected to centrifugal force, and the floating oil with larger oil droplet size in the incoming water can passively move towards the main composite membrane. Meanwhile, the main composite membrane is influenced by the temperature of the incoming water to self-regulate the pore diameter of the membrane channel of the main composite membrane, and the pore diameter is enough to allow floating oil which is in contact with the main composite membrane to pass through. Oil pollutants with larger oil drop particle sizes can smoothly pass through the main composite membrane and enter the oil pollutant gaps under the synergistic action of the centrifugal force action provided by the mechanical actuating mechanism and the attraction force action provided by the main composite membrane. The temperature of the incoming water itself is the greatest among the temperature variations of the overall main composite membrane treatment process when the incoming water is introduced into the first pollutant removal device.
The first pollutant removing device can regulate and control the operating parameters of the non-contact demulsification equipment by means of the non-contact demulsification equipment assembled outside the cylindrical treatment part, and demulsify the emulsified oil in the cylindrical treatment part at a preset time to convert the emulsified oil into oil substances capable of being intercepted by the main composite membrane. The non-contact demulsification device can be a microwave device or an ultrasonic device.
The temperature sensor can continuously detect the internal environment temperature, and when the temperature of the incoming water is detected to be gradually reduced to the pore diameter of a membrane channel in the main composite membrane and is not enough to pass through oil pollutants at least comprising floating oil, the operation parameters of the non-contact demulsification equipment are regulated and controlled, and the oil substances at least comprising emulsified oil in the cylindrical processing part are subjected to demulsification treatment. The mechanical brake mechanism adjusts operation parameters based on the internal environment temperature detected by the temperature sensor, so that the pollutants in the incoming water and/or the incoming water are acted by centrifugal force, and the demulsified oil pollutants with moderate oil droplet particle size in the incoming water can passively move towards the main composite membrane. Meanwhile, the main composite membrane is influenced by the temperature of the incoming water to self-regulate the pore diameter of the membrane channel of the main composite membrane, and the pore diameter is enough to allow the demulsified oil pollutants which are in contact with the main composite membrane to pass through. The demulsified oil pollutants with moderate oil drop particle size can smoothly pass through the main composite membrane and enter the oil pollutant gaps under the synergistic action of the centrifugal force action provided by the mechanical actuating mechanism and the attraction force action provided by the main composite membrane.
A large number of composite membranes are proposed in the prior art, and iron pollutants are actively intercepted through the processes of bridging, intercepting, adsorbing, filtering and the like, but the composite membranes have the problems of being not high in temperature resistance, only being used for carrying out iron removal treatment on low-temperature incoming water, and being incapable of being applied to high-temperature incoming water. In this application, main complex film can utilize the self temperature of coming water to realize the interception effect to the iron class pollutant in this first pollutant device that removes. Preferably, the active interception effect of the composite material on the iron pollutants can be selected, so that a more excellent iron removal effect is realized.
In the treatment process stage of the main composite membrane, the temperature of high-temperature incoming water is gradually reduced, the main composite membrane correspondingly adjusts the membrane treatment capacity of the incoming water depending on the change of the temperature of the incoming water, and forms an attractive effect of non-active interception on iron pollutants in the incoming water in a mode that the pore diameter of a membrane channel is changed therewith, so that the effects of removing oil and iron from the incoming water are realized simultaneously.
The ferrous contaminants are subject to greater gravitational forces relative to the less dense oil contaminants, and thus less contact between the ferrous contaminants and the main composite membrane occurs when the centrifugal force provided by the mechanical actuation mechanism is less during the initial stages of introduction of the incoming water into the first contaminant removal device. Under the condition that the centrifugal force provided by the later mechanical actuating mechanism is gradually increased, the ferrous pollutants are contacted with the membrane channels of the main composite membrane but cannot pass through the membrane channels under the effective centrifugal force. As the temperature is continuously reduced, the aperture of the membrane channel in the main composite membrane is shrunk along with the temperature, and the iron pollutants which are contacted with the membrane channel of the main composite membrane are kept in the main composite membrane under the action of a certain attractive force applied to the iron pollutants in the aperture shrinking process. After the main composite membrane treatment process is completed, most of the oil pollutants and the iron pollutants are intercepted by the main composite membrane, and effluent with low content of the oil/iron pollutants can be discharged.
The oil and iron removing composite membrane provided by the prior art is indiscriminately used for removing oil pollutants and iron pollutants in various areas, and is extremely easy to be blocked by the oil pollutants or the iron pollutants with larger oil drop particle sizes, so that the membrane treatment capacity is rapidly reduced. The iron pollutants are more greatly suspended in the middle and lower layers of the incoming water than the oil pollutants with lower density due to the gravity, and the oil pollutants with lower density are suspended in the middle and upper layers of the incoming water. Correspondingly, different processing capacities of the regions of the main composite film are not required to be set, namely, the regions of the main composite film have the same structure and performance, so that the process difficulty and the process steps for preparing the main composite film can be reduced. The cross section of the main composite membrane can have the same membrane treatment capacity along the incoming water direction, and the interception effect on oil pollutants and iron pollutants can be still met under the arrangement.
The main complex film that this application provided mainly utilizes the self temperature of coming water to realize the interception effect to the iron class pollutant to this interception in-process main complex film can not bridge, intercepts, processes such as absorption, filtration initiatively intercept the iron class pollutant, and the iron class pollutant is kept on main complex film surface all the time. In the back flushing process/periodic oil discharge through the oil pollutant gap, the mixed waste liquid containing the oil pollutants in the oil pollutant gap can be recovered for treatment. The iron-based contaminants retained on the surface of the main composite membrane can be recovered by the backwashing process of the cylindrical treatment section.
As a preferred embodiment, the process condensate water recovered by the chemical plant and returned by other steam users has a large temperature difference, i.e. the process condensate water can be directly and actively introduced into the main composite membrane treatment process stage when the temperature of the incoming water is low (very-warm condition). When the temperature of the incoming water is too high, the incoming water can be introduced into the first ammonia nitrogen removal treatment device, and ammonia nitrogen pollutants in the incoming water can be removed by utilizing the high temperature of the incoming water. The temperature of the incoming water treated by the first ammonia nitrogen removal treatment device is reduced, and then the incoming water is introduced into the first pollutant removal device for further removing oil and iron. Under the condition that the temperature of the incoming water is low and is not at normal temperature, the incoming water can be introduced into the first pollutant removing device, and the oil/iron pollutants in the incoming water are removed by utilizing the temperature of the incoming water. The temperature of the incoming water treated by the first pollutant removing device is reduced, and then the incoming water is introduced into a second ammonia nitrogen removing treatment device for further ammonia nitrogen removal treatment. The first ammonia nitrogen removal treatment device can remove ammonia nitrogen from high-temperature incoming water, and the second ammonia nitrogen removal treatment device can remove ammonia nitrogen from incoming water at a relatively low temperature but in a very high temperature condition.
As a preferred embodiment, the process condensate water recovered by the chemical plant and returned by other steam users enters the condensate water recovery and treatment system provided by the application through the condensate water conveying channel. The outlet of the condensed water conveying pipeline is connected with one end of a three-way control device, and the two ends of the three-way control device are respectively connected with a first ammonia nitrogen removal treatment device and a first pollutant removal device. The outlet end of the first ammonia nitrogen removal treatment device is connected with the second first pollutant removal device, and the outlet end of the first pollutant removal device is connected with the second ammonia nitrogen removal treatment device. The outlet end of the first pollutant removing device of the second and the outlet end of the ammonia nitrogen removing treatment device of the second are both connected with the inlet end of the second pollutant removing device through a three-way control device.
It should be noted that the above-mentioned embodiments are exemplary, and that those skilled in the art, having benefit of the present disclosure, may devise various arrangements that are within the scope of the present disclosure and that fall within the scope of the invention. It should be understood by those skilled in the art that the present specification and figures are illustrative only and are not limiting upon the claims. The scope of the invention is defined by the claims and their equivalents. The present description contains several inventive concepts, such as "preferably", "according to a preferred embodiment" or "optionally", each indicating that the respective paragraph discloses a separate concept, the applicant reserves the right to submit divisional applications according to each inventive concept.
Claims (10)
1. A condensate recovery processing system, characterized in that the system comprises at least:
a condensed water delivery conduit;
the pollutant removing subsystem is used for introducing the condensed water to be recovered and treated through the condensed water conveying pipeline under the condition that the condensed water is not reduced to the normal temperature and treating and removing pollutants at least comprising oil and/or iron in the condensed water;
and the mixed ion exchange treatment subsystem is used for desalting the condensed water which is obtained after the treatment of the pollutant removal subsystem and is in a non-high temperature state so as to enable the obtained effluent to reach the indexes of primary desalted water or secondary desalted water.
2. The system of claim 1, wherein the contaminant removal subsystem is capable of introducing the turbine condensate to be recycled through the turbine condensate delivery pipe and removing contaminants including at least oils and/or irons in the turbine condensate without cooling the turbine condensate to normal temperature, and the mixed ion exchange treatment subsystem is capable of desalting the process condensate and the turbine condensate in a non-high temperature state obtained after the treatment by the contaminant removal subsystem.
3. The system as claimed in any one of claims 1 to 2, wherein the contaminant removal subsystem comprises at least an iron removal filtration unit, and the iron removal filtration unit can be used for removing iron contaminants or suspended impurities in the process condensate.
4. The condensate water recovery processing system according to any one of claims 1 to 3, further comprising a blocking and deoiling unit for deoiling and blocking the process condensate water obtained after the deironing process, and removing oil pollutants in the process condensate water.
5. The condensate water recovery processing system according to any one of claims 1 to 4, further comprising a blocking and deoiling unit for deoiling and blocking the process condensate water obtained after the deironing process, and removing the oil contaminants in the process condensate water.
6. The condensate recovery processing system according to any one of claims 1 to 5, wherein the deoiled effluent obtained by the intercepting deoiling processing unit can be directly conveyed to the biochemical treatment tank, or conveyed to the primary air floatation tank for protective treatment and then enters the biochemical treatment tank.
7. The condensate recovery processing system according to any one of claims 1 to 6, further comprising a turbine condensate pretreatment unit for collecting turbine condensate recovered from the chemical plant into a turbine condensate tank, wherein the turbine condensate in the turbine condensate tank can be pressurized and sent to the next processing unit by a turbine condensate pump.
8. The condensate water recovery processing system according to any one of claims 1 to 7, further comprising a microfiltration unit, wherein the microfiltration unit is used for removing iron and oil from the turbine condensate water, and removing iron-based pollutants or suspended impurities from the turbine condensate water.
9. A condensate recovery processing system, characterized in that the system comprises at least:
a condensed water delivery conduit;
the pollutant removing subsystem is used for introducing the condensed water to be recovered and treated through the condensed water conveying pipeline under the condition that the condensed water is not reduced to the normal temperature and treating and removing pollutants at least comprising oil and/or iron in the condensed water;
a mixed ion exchange processing subsystem for desalting the condensed water which is obtained after the treatment of the pollutant removing subsystem and is in a non-high temperature state so as to enable the obtained effluent to reach the index of primary desalted water or secondary desalted water,
wherein, the pollutant removing subsystem at least comprises a first pollutant removing device and a second pollutant removing device which are used for removing iron pollutants or oil pollutants in the condensed water.
10. A condensate treatment method is characterized by at least comprising one or more of the following steps: introducing the condensed water to be recycled through a condensed water conveying pipeline under the condition that the condensed water is not reduced to normal temperature; treating and removing pollutants at least comprising oil and/or iron in the condensate by using a pollutant removing subsystem; and a mixed ion exchange treatment subsystem is utilized to carry out desalination treatment on the condensate water which is obtained after the treatment of the pollutant removal subsystem and is in a non-high temperature state so as to enable the obtained effluent water to reach the index of primary desalted water or secondary desalted water.
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