CN112093966B - Energy-saving consumption-reducing method based on mine water zero-discharge full process - Google Patents
Energy-saving consumption-reducing method based on mine water zero-discharge full process Download PDFInfo
- Publication number
- CN112093966B CN112093966B CN202011047915.XA CN202011047915A CN112093966B CN 112093966 B CN112093966 B CN 112093966B CN 202011047915 A CN202011047915 A CN 202011047915A CN 112093966 B CN112093966 B CN 112093966B
- Authority
- CN
- China
- Prior art keywords
- water
- temperature
- mine water
- cooling
- flow
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
Images
Classifications
-
- 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
-
- 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
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
- C02F1/048—Purification of waste water by evaporation
-
- 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
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/02—Temperature
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2301/00—General aspects of water treatment
- C02F2301/04—Flow arrangements
- C02F2301/046—Recirculation with an external loop
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2303/00—Specific treatment goals
- C02F2303/10—Energy recovery
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2303/00—Specific treatment goals
- C02F2303/14—Maintenance of water treatment installations
Landscapes
- Life Sciences & Earth Sciences (AREA)
- Hydrology & Water Resources (AREA)
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Separation Using Semi-Permeable Membranes (AREA)
Abstract
The invention relates to a mine water zero-discharge treatment method, in particular to an energy-saving and consumption-reducing method based on a mine water zero-discharge full flow, and belongs to the technical field of water treatment. The method is characterized in that mine water heat energy recycling is carried out on the mine water zero-discharge full-flow process, and the mine water heat energy recycling is divided into a direct flow type and a mixed flow type according to different contents of temperature sensitive substances in mine water. According to the method, the characteristics of low temperature and large specific heat capacity of the mine water are utilized according to the difference between the water temperature and the water quality of the mine water and the cooling return water temperature in the evaporative crystallization process, the high-grade heat generated in the evaporative crystallization process is recovered by changing the process of the mine water medium in the zero emission treatment, and the low-temperature mine water is heated by utilizing the heat, so that the aims of improving the sectional process efficiency in the whole process of the mine water zero emission, saving the energy consumption and operating cost and the like are fulfilled.
Description
Technical Field
The invention relates to a mine water zero-discharge treatment method, in particular to an energy-saving and consumption-reducing method based on a mine water zero-discharge full flow, and belongs to the technical field of water treatment.
Background
Most coal mines in China are in water-deficient and ecological environment-fragile areas such as North China and northwest China, and more than 90% of mine water in the areas is high-salt mine water. The conventional treatment of high-salinity mine water cannot meet the discharge or recycling requirements, and zero-discharge treatment is required. Especially, in recent years, the discharge of high-salt mine water in various mine areas is higher and higher, the pressure of coal enterprises in the aspects of resource constraint and discharge limitation is increased suddenly, and the achievement of accelerating energy conservation and consumption reduction and zero discharge of high-salt water pollutants is a necessary choice.
The temperature of coal mine water in China is usually between 15 ℃ and 20 ℃, the temperature of individual mine water is even lower than 10 ℃ in winter, and how to ensure the necessary temperature of the mine water is a problem to be solved in the process of mine water zero emission treatment. The conventional method is to add a steam heat exchanger, heat mine water by using steam at low temperature, and increase the temperature to meet the treatment requirement of a subsequent membrane concentration working section; or the water pump lift in the membrane concentration stage is increased to realize ultrafiltration and reverse osmosis treatment. Either way, steam consumption and power consumption must be increased, which is not an economical and efficient method.
The zero-emission treatment process of the high-salinity mine water comprises the working procedures of purification treatment, membrane concentration treatment, evaporation crystallization treatment and the like. Wherein, the efficiency of membrane concentration treatment receives the influence of the temperature of intaking, requires to the finite value of the temperature of intaking, and in certain temperature range, the higher the temperature is the higher the treatment effeciency is, and the energy consumption is lower. Taking the Dow ultrafiltration membrane as an example, the allowable range of the water inlet temperature is generally 1-40 ℃. As the viscosity of mine water can change along with the temperature, the filtration flow or the transmembrane pressure difference of the membrane component can change greatly along with the temperature change under any working pressure. The flux of the membrane module is 62L/(m) at 14 DEG C2h) The flux of the membrane module is 80L/(m) at 25 DEG C2h) The flux of the membrane module at 35 ℃ is 95L/(m)2h) The water yield decreases by about 10% for every 5 ℃ drop in temperature. The required osmotic pressure of the same dow reverse osmosis membrane is gradually reduced with increasing temperature. Under the same conditions, the osmotic pressure at 20 deg.C is 68.0bar, the osmotic pressure at 25 deg.C is 64.2bar, the osmotic pressure at 30 deg.C is 62.1bar, and the osmotic pressure at 35 deg.C is 60.5 bar. Although the variation of the process parameter value is a normal phenomenon, the production efficiency is affected. In order to ensure higher membrane concentration efficiency, mine water with too low or too high temperature generally needs to be heated or cooled, which involves the problems of energy consumption management and operation cost.
In addition, evaporative crystallization is bound to become a terminal process for the development of a high-salt mine water pollutant zero-emission treatment technology in the future, wherein high-quality raw steam is required to be used as a heat source in the mechanical recompression evaporative crystallization (MVR) and multiple-effect evaporative crystallization (MED) technologies, and the operation cost is extremely high. Meanwhile, the MVR technology needs electric drive, steam parameters are improved, power consumption is high, and the operating temperature is high. According to statistics, the electricity consumption and the steam cost account for more than 70% of the total operation cost in the zero discharge process of the mine water and even reach more than 85% in northern mining areas in winter, which becomes a key factor influencing the operation cost and needs to provide higher requirements for evaporative crystallization energy consumption management and matched cooling procedures.
Meanwhile, the cooling requirements in evaporative crystallization are also large, and the cooling requirements comprise secondary steam condensation, steam compressor cooling, refrigerating unit cooling, circulating cooling water return cooling, machine seal water heat exchanger cooling and the like. These also all involve energy management issues. If the heat in the cooling return water is not utilized, a great deal of energy is wasted. If the cooling return water flow is small and the heat exchange temperature rise is large, the return water temperature is too high and directly enters the membrane concentration system, so that the membrane element is damaged. Therefore, from the energy-saving and consumption-reducing perspective of reducing the steam demand, the waste of steam condensation and cooling heat exchange waste heat needs to be reduced besides the need of improving the initial temperature of the mine water material. In a word, measures are taken to recycle the low-grade steam waste heat in the evaporation crystallization process, and the method is used for zero-emission all sections, and has practical significance for saving energy, reducing consumption and effectively reducing cost.
In the mine water zero-discharge full flow, the characteristics of zero-discharge process flow complexity, high energy requirement and consumption, high operation management requirement and the like are combined, the characteristics of low temperature and high specific heat capacity of mine water and low-grade heat generated in an evaporative crystallization working section are scientifically and reasonably utilized, and meanwhile, an energy-saving consumption-reducing energy management mode combining the characteristics of a film concentration and evaporative crystallization matched cooling working procedure is less involved. Therefore, how to recover the low-grade heat generated in the evaporation crystallization working section by utilizing the characteristics of low temperature and large specific heat capacity of the mine water, and the utilization of the waste heat by the mine water circulating medium can improve the efficiency of each process in the whole process of the mine water zero discharge and save the operating cost in the aspect of energy consumption, so that the method becomes a problem to be solved urgently in energy and cost management in the whole process of the mine water zero discharge, and is also an important meaning for researching and developing the mine water zero discharge whole-process energy-saving and consumption-reducing technology and method which have good energy-saving and consumption-reducing effects, high operating efficiency, zero discharge of high-salt mine water pollutants and have good environmental protection benefits and economic benefits.
Disclosure of Invention
The invention provides an energy-saving consumption-reducing method based on a mine water zero-discharge full flow aiming at the defects of lack of a mine area cooling water source, high operation energy consumption and operation and maintenance cost, low system production efficiency, serious waste of waste heat of steam condensation and cooling heat exchange and the like in the high-salt mine water pollutant zero-discharge treatment in the prior art.
The technical scheme adopted by the invention for solving the technical problems is as follows:
the method is characterized in that mine water heat energy recycling is carried out on the mine water zero-discharge full-flow process, and the mine water heat energy recycling method is divided into a direct flow type and a mixed flow type according to different contents of temperature sensitive substances in mine water:
the direct-flow process is characterized in that mine water is directly subjected to steam condensation or process cooling after being purified, cooling return water after the temperature of the mine water is increased sequentially enters a membrane concentration treatment process and an evaporation crystallization process to be used as cooling water of the evaporation crystallization process, is used for refrigeration process heat dissipation and secondary steam condensation in the evaporation crystallization process, and forms a closed loop with the mine water cooling return water;
the mixed flow process is characterized in that mine water is divided into two parts after being purified, wherein the first part is used as cooling water of an evaporative crystallization process and is used for steam condensation or process cooling in the evaporative crystallization process; and the second part and the first part of the warmed cooling backwater are mixed and then enter a membrane concentration treatment process and an evaporation crystallization process in sequence, and the cooling water used as the evaporation crystallization process forms a closed loop with the first part of the mine water cooling backwater and the second part of the mine water.
According to the method, the characteristics of low temperature and large specific heat capacity of the mine water are utilized according to the difference between the water temperature and the water quality of the mine water and the cooling return water temperature in the evaporative crystallization process, the high-grade heat generated in the evaporative crystallization process is recovered by changing the process of the mine water medium in the zero emission treatment, and the low-temperature mine water is heated by utilizing the heat, so that the aims of improving the sectional process efficiency in the whole process of the mine water zero emission, saving the energy consumption and operating cost and the like are fulfilled.
The temperature of the mine water after temperature rise does not exceed the highest temperature which can be endured by a reverse osmosis membrane in the subsequent membrane concentration process, and is usually 35 ℃; if the heat quantity required for cooling by evaporative crystallization does not exceed the heat quantity required for raising the mine water to the highest temperature, the mine water can be used as the only cooling medium; if the heat required for cooling the evaporative crystallization exceeds the heat required for raising the mine water to the highest temperature, a small-scale cooling tower needs to be arranged, and the excess heat is dissipated.
The invention combines the mine water zero-discharge treatment process flow, utilizes the characteristics of low temperature and large specific heat capacity of the purified mine water as cooling water of an evaporative crystallization process, and is used for heat dissipation of a freezing process and secondary steam condensation in the evaporative crystallization process. Meanwhile, according to the cooling power required by the process cooling and the requirement of the cooling return water temperature, the flow ratio of the low-temperature mine water and the cooled high-temperature return water is controlled and adjusted, and the mixed low-temperature mine water and the cooled high-temperature return water are subjected to subsequent membrane concentration treatment and evaporation crystallization treatment according to the required temperature.
Preferably, the refrigeration process heat dissipation and secondary steam condensation in the evaporative crystallization process adopt indirect cooling.
Preferably, the water quantity of the first part of mine water in the mixed flow process is determined according to the cooling power and cooling return water temperature requirements of cooling process heat dissipation, secondary steam condensation and the like in the evaporative crystallization process; the water temperature of the mixed mine water of the second part and the mine water of the first part after cooling return water is not more than the highest inlet water temperature of the membrane concentration treatment process in the mixed flow process.
Preferably, in the mixed-flow process, the second part and the cooled return water after the temperature of the first part is increased are mixed and increased in temperature through a mixing device, and the mixing device is a pipeline mixer or a purified water pool.
Preferably, a flow and temperature automatic interlocking feedback valve group is arranged on a pipeline at the front end of the mixing device, so that dynamic association of the mixing proportion of the water temperature and the mine water flow before and after mixing is realized.
Preferably, when the concentration of calcium and magnesium ions in the mine water is 120-200 mg/L, a straight flow process is adopted, and when the concentration of calcium and magnesium ions in the mine water is 30-120 mg/L, a mixed flow process is adopted.
Preferably, the low-temperature mine water Q is used under a straight-flow process0At the water temperature T0After purification treatment at 15-20 ℃, directly cooling in the process or condensing steam; in the evaporative crystallization process, the initial temperature of steam is 102-106 ℃, the steam and low-temperature mine water are indirectly cooled and subjected to steam-liquid phase change heat exchange, and the temperature of the low-temperature mine water is changed from T0Heating to T at 15-20 deg.C1= 25-35 ℃; mine water Q after heating0At the water temperature T1Entering a membrane concentration treatment process at the temperature of 25-35 ℃.
Preferably, the mixed flow process is used for low-temperature mine water Q0At the water temperature T0After purification treatment at 15-20 ℃, the first partial flow Q1At the water temperature T0Directly cooling at 15-20 ℃ or condensing steam; according to the cooling power P and the cooling return water temperature T required by the process cooling1= 35-40 ℃, and regulating and controlling the first partial flow Q of the mine water1(ii) a Low temperature mine water second part flow Q2At the water temperature T0= 15-20 ℃ and the cooling return water flow Q of the first part after process cooling1At the water temperature T1Mixing at 35-45 ℃; mine water Q after mixing0=Q1+Q2At the water temperature T2And (4) sequentially performing a membrane concentration treatment process and an evaporation crystallization process at the temperature of 25-35 ℃.
Preferably, Q1And Q2According to the mixed water temperature T2And (4) regulating and controlling at 25-35 ℃.
Compared with the prior art, the invention has the following beneficial effects:
1. compared with the method for improving the water temperature in the conventional mine water zero discharge process, the method provided by the invention is not simple to heat the mine water by using steam, but utilizes the characteristics of low temperature and large specific heat capacity of the mine water to recover low-grade heat in the evaporative crystallization process, improve the temperature per se and meet the subsequent treatment requirement. Meanwhile, the low-temperature mine water is used as circulating cooling water for zero-emission treatment of the evaporative crystallization process, is used for heat dissipation of a freezing process and secondary steam condensation in the evaporative crystallization process, and ensures normal operation of the evaporative crystallization process.
2. According to the invention, the mine water inlet temperature of the membrane concentration treatment process in the zero-emission treatment process is increased by using the collected external waste heat, so that the mine water inlet temperature meets the inlet temperature requirement of efficient operation of the membrane element, the membrane concentration efficiency is favorably improved, the service life of the membrane element is prolonged, and the stable operation of the membrane concentration process is ensured.
3. The invention can utilize the characteristics of low temperature and large specific heat capacity of mine water raw water as direct cooling mixed water for adjusting the overhigh temperature of cooling return water in the evaporative crystallization process, so that the mine water mixed water meets the requirement of the water inlet temperature for efficient operation of the membrane element and prevents the damage of the membrane element caused by overhigh water inlet temperature.
4. Compared with the conventional process of adopting circulating cooling water and a cooling tower in the mine water zero discharge process, the invention does not need facilities and equipment such as an external cooling water source or the cooling tower and the like, thereby saving the construction investment; meanwhile, after the purified mine water is used as a cooling medium, the water temperature is increased, so that the osmotic pressure of soluble salts is reduced, the solubility is improved, the energy consumption of a high-pressure pump is reduced, the scaling risk is reduced or the concentration recovery rate is improved, and the effects of energy conservation and consumption reduction are remarkable.
Drawings
In order to more clearly illustrate the embodiments or technical solutions of the present invention, the drawings used in the description of the embodiments or the prior art will be briefly described below, and it is obvious that the drawings in the following description are only some embodiments of the present invention, and it is obvious for those skilled in the art that other drawings can be obtained based on these drawings without creative efforts.
FIG. 1 is a schematic process flow diagram of the energy saving and consumption reduction method based on the mine water zero discharge full flow under the straight flow process;
FIG. 2 is a schematic process flow diagram of the mixed flow type process of the energy saving and consumption reduction method based on the mine water zero discharge full flow.
Detailed Description
The technical solution of the present invention will be further specifically described below by way of specific examples. It is to be understood that the practice of the invention is not limited to the following examples, and that any variations and/or modifications may be made thereto without departing from the scope of the invention.
In the present invention, all parts and percentages are by weight, unless otherwise specified, and the equipment and materials used are commercially available or commonly used in the art. The methods in the following examples are conventional in the art unless otherwise specified.
The core of the invention is to provide an energy-saving consumption-reducing method based on a mine water zero-discharge full flow, which is called as a first specific implementation mode, wherein the mine water zero-discharge full flow comprises the working procedures of mine water purification treatment, membrane concentration treatment and evaporative crystallization, the method is to recycle the mine water heat energy on the mine water zero-discharge full flow process, and the method is divided into a direct flow type and a mixed flow type according to different contents of temperature sensitive substances in the mine water: when the concentration of calcium and magnesium ions in the mine water is 120-200 mg/L, a straight flow process is adopted, and when the concentration of calcium and magnesium ions in the mine water is 30-120 mg/L, a mixed flow process is adopted.
The direct-flow process is characterized in that mine water is directly subjected to steam condensation or process cooling after being purified, cooling return water after the temperature of the mine water is increased sequentially enters a membrane concentration treatment process and an evaporation crystallization process to be used as cooling water of the evaporation crystallization process, is used for refrigeration process heat dissipation and secondary steam condensation in the evaporation crystallization process, and forms a closed loop with the mine water cooling return water;
the mixed flow process is characterized in that mine water is divided into two parts after being purified, wherein the first part is used as cooling water of an evaporative crystallization process and is used for steam condensation or process cooling in the evaporative crystallization process; and the second part and the first part of the warmed cooling backwater are mixed and then enter a membrane concentration treatment process and an evaporation crystallization process in sequence, and the cooling water used as the evaporation crystallization process forms a closed loop with the first part of the mine water cooling backwater and the second part of the mine water.
Furthermore, in the mixed flow process, the second part and the cooled return water after the temperature of the first part is increased are mixed and increased in temperature through a mixing device, and the mixing device is a pipeline mixer or a purified water pool. A flow and temperature automatic interlocking feedback valve group is arranged on a pipeline at the front end of the mixing device, and dynamic association of mixing proportion of water temperature and mine water flow before and after mixing is realized.
In actual operation, the temperature of high-salt mine water is generally 10-37 ℃, mostly 15-20 ℃, and the maximum value of the high-efficiency operation temperature of the membrane element is not more than 40 ℃. The suitable temperature required by the efficient operation of the membrane concentration treatment process is about 35 ℃, and the inlet water temperature of the low-temperature mine water cannot meet the optimal inlet water temperature requirement of the membrane concentration treatment.
In the direct-flow process shown in fig. 1, after low-temperature mine water is purified, the initial inlet water temperature is low, which affects the osmotic pressure and solubility of soluble salts in the mine water, and the mine water can not directly enter a membrane concentration process, but enter process cooling or steam condensation for cooling process heat dissipation and secondary steam condensation in an evaporative crystallization process. Meanwhile, the low-temperature mine water can be heated to the temperature required by the efficient operation of the membrane element by the external low-grade waste heat collected in the cooling process, and then the low-temperature mine water enters the membrane concentration treatment and evaporative crystallization processes, so that the membrane concentration efficiency is improved, the service life of the membrane element is protected, the electric energy and steam consumption can be saved by recycling the waste heat, and the operation cost is reduced.
Straight-flow process underground, low-temperature mine water Q0At the water temperature T0And after purification treatment at 15-20 ℃, directly cooling in the process or condensing steam. In the evaporative crystallization process, the initial temperature of steam is 102-106 ℃, the steam and low-temperature mine water are indirectly cooled and subjected to steam-liquid phase change heat exchange, and the temperature of the low-temperature mine water is changed from T0Heating to T at 15-20 deg.C1And = 25-35 ℃. Mine water Q after heating0At the water temperature T1Entering a membrane concentration treatment process at the temperature of 25-35 ℃.
In the mixed-flow process shown in fig. 2, the low-temperature mine water is purified and then divided into two parts, and the first part can influence the osmotic pressure and solubility of soluble salts in the mine water due to low initial water inlet temperature, and can not directly enter a membrane concentration process, but directly enter process cooling or steam condensation for cooling process heat dissipation and secondary steam condensation in an evaporative crystallization process. Meanwhile, the low-temperature mine water can be heated by external low-grade waste heat collected in the cooling process. If the flow of the first part is small or the cooling power of the evaporative crystallization process is high, the temperature of the cooling return water can exceed the maximum value of the efficient operation temperature of the membrane element after cooling. Therefore, the high-temperature cooling backwater needs to be mixed with the second part of low-temperature mine water for cooling, the temperature after mixing can be controlled and adjusted to the temperature required by the efficient operation of the membrane element, and then the membrane element enters the concentration treatment and evaporative crystallization processes, so that the membrane concentration efficiency is improved, the service life of the membrane element is protected, the electric energy and the steam consumption can be saved by recycling the waste heat, and the operation cost is reduced.
Mixed flow type flow path down, low temperature mine water Q0At the water temperature T0After purification treatment at 15-20 ℃, the first partial flow Q1At the water temperature T0And (4) directly cooling or steam condensing at 15-20 ℃. According to the cooling power P and the cooling return water temperature T required by the process cooling1Requirement (T)1Generally 35-40 ℃), and regulating and controlling the first partial flow Q of the mine water1. Low temperature mine water second part flow Q2At the water temperature T0= 15-20 ℃ and the cooling return water flow Q of the first part after process cooling1At the water temperature T1And mixing at 35-45 ℃. The mixing proportion is according to the mixed water temperature T2And (4) regulating and controlling at 25-35 ℃. Mine water Q after mixing0=Q1+Q2At the water temperature T2And (4) sequentially performing a membrane concentration treatment process and an evaporation crystallization process at the temperature of 25-35 ℃.
In the conventional mine water zero-emission treatment process, the mine water is heated by using raw steam in a membrane concentration section, and circulating cooling water and a cooling tower process are adopted in an evaporation crystallization section. Compared with the conventional mine water zero-discharge treatment process, the invention recovers the low-grade heat of the evaporation crystallization section to improve the temperature of the mine water and meets the treatment requirement of the membrane concentration section; meanwhile, the purified mine water is used as a cooling medium of an evaporative crystallization section, raw steam is not consumed in a membrane concentration section, and external cooling water sources or cooling towers and other facilities and equipment are not needed in the evaporative crystallization section, so that the construction investment is saved; meanwhile, after the purified mine water is used as a cooling medium, the water temperature is increased, so that the osmotic pressure of soluble salts is reduced, and the solubility is improved, thereby reducing the energy consumption of a high-pressure pump, reducing the scaling risk and improving the concentration recovery rate. Specifically, the embodiment can save extra cooling water source and electricity consumption cost by about 15-20%, reduce steam cost by about 40-50% in winter, and has obvious energy-saving and consumption-reducing effects.
The embodiments are described in a progressive manner, each embodiment focuses on differences from other embodiments, and the same or similar parts among the embodiments are referred to each other. The device disclosed by the embodiment corresponds to the method disclosed by the embodiment, so that the description is simple, and the relevant points can be referred to the method part for description.
The energy-saving and consumption-reducing method based on the mine water zero-discharge full process is described in detail above. The principles and embodiments of the present invention are explained herein using specific examples, which are presented only to assist in understanding the method and its core concepts. It should be noted that, for those skilled in the art, it is possible to make various improvements and modifications to the present invention without departing from the principle of the present invention, and those improvements and modifications also fall within the scope of the claims of the present invention.
Claims (6)
1. The energy-saving consumption-reducing method based on the mine water zero-discharge full flow comprises the working procedures of mine water purification treatment, membrane concentration treatment and evaporative crystallization, and is characterized in that: the method is used for recycling the heat energy of the mine water on the mine water zero-discharge full-flow process, and is divided into a direct flow type and a mixed flow type according to different contents of temperature sensitive substances in the mine water:
the direct-flow process is that the mine water is directly subjected to steam condensation or process cooling after being purified, and the cooling return water after the temperature of the mine water is increased sequentially enters a membrane concentration treatment process and an evaporation crystallization process;
the mixed flow process is characterized in that mine water is divided into two parts after being purified, wherein the first part is used as cooling water of an evaporative crystallization process and is used for steam condensation or process cooling in the evaporative crystallization process; mixing the second part with the first part of cooled return water after being heated, and then sequentially entering a membrane concentration treatment process and an evaporation crystallization process;
when the concentration of calcium and magnesium ions in the mine water is 120-200 mg/L, a straight-flow process is adopted, and when the concentration of calcium and magnesium ions in the mine water is 30-120 mg/L, a mixed-flow process is adopted;
straight-flow process underground, low-temperature mine water Q0At the water temperature T0After purification treatment at 15-20 ℃, directly cooling in the process or condensing steam; in the evaporative crystallization process, the initial temperature of steam is 102-106 ℃, the steam and low-temperature mine water are indirectly cooled and subjected to steam-liquid phase change heat exchange, and the temperature of the low-temperature mine water is changed from T0Heating to T at 15-20 deg.C1= 25-35 ℃; mine water Q after heating0At the water temperature T1Entering a membrane concentration treatment process at the temperature of 25-35 ℃;
mixed flow type flow path down, low temperature mine water Q0At the water temperature T0After purification treatment at 15-20 ℃, the first partial flow Q1At the water temperature T0Directly cooling at 15-20 ℃ or condensing steam; according to the cooling power P and the cooling return water temperature T required by the process cooling1= 35-40 ℃, and regulating and controlling the first partial flow Q of the mine water1(ii) a Low temperature mine water second part flow Q2At the water temperature T0= 15-20 ℃ and the cooling return water flow Q of the first part after process cooling1At the water temperature T1Mixing at 35-45 ℃; mine water Q after mixing0=Q1+Q2At the water temperature T2And (4) sequentially performing a membrane concentration treatment process and an evaporation crystallization process at the temperature of 25-35 ℃.
2. The energy saving and consumption reduction method based on the mine water zero discharge full flow according to claim 1, characterized in that: the process cooling and steam condensation in the evaporation crystallization process adopt indirect cooling.
3. The energy saving and consumption reduction method based on the mine water zero discharge full flow according to claim 1, characterized in that: the water quantity of the first part of mine water in the mixed flow process is determined according to the requirements of process cooling, steam condensation required power and cooling return water temperature in the evaporative crystallization process;
the water temperature of the mixed mine water of the second part and the mine water of the first part after cooling return water is not more than the highest inlet water temperature of the membrane concentration treatment process in the mixed flow process.
4. The energy saving and consumption reduction method based on the mine water zero discharge full flow according to claim 1, characterized in that: in the mixed flow type process, the second part and the cooled return water after the temperature of the first part is increased are mixed and heated through a mixing device, and the mixing device is a pipeline type mixer or a purified water pool.
5. The energy saving and consumption reduction method based on the mine water zero discharge full flow according to claim 1, characterized in that: a flow and temperature automatic interlocking feedback valve group is arranged on a pipeline at the front end of the mixing device, and dynamic association of mixing proportion of water temperature and mine water flow before and after mixing is realized.
6. The energy saving and consumption reduction method based on the mine water zero discharge full flow according to claim 1, characterized in that: q1And Q2According to the mixed water temperature T2And (4) regulating and controlling at 25-35 ℃.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202011047915.XA CN112093966B (en) | 2020-09-29 | 2020-09-29 | Energy-saving consumption-reducing method based on mine water zero-discharge full process |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202011047915.XA CN112093966B (en) | 2020-09-29 | 2020-09-29 | Energy-saving consumption-reducing method based on mine water zero-discharge full process |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN112093966A CN112093966A (en) | 2020-12-18 |
| CN112093966B true CN112093966B (en) | 2022-03-29 |
Family
ID=73783912
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202011047915.XA Active CN112093966B (en) | 2020-09-29 | 2020-09-29 | Energy-saving consumption-reducing method based on mine water zero-discharge full process |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN112093966B (en) |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114368844B (en) * | 2021-12-15 | 2023-03-21 | 庆阳新庄煤业有限公司新庄煤矿 | Data monitoring method and device for high-salinity mine water treatment |
Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101462809A (en) * | 2008-12-25 | 2009-06-24 | 王俊川 | Comprehensive recovery method for heat energy and water from printing and dyeing industry wastewater and heat-exchanging system |
| DE102009041143A1 (en) * | 2009-09-14 | 2011-03-24 | Frederick Simon Oosthuizen | Processing mining waste water comprises separating sulfur metal ions and sulfate from water, reducing sulfur metal ions and sulfate to sulfide and removing the sulfide from waste water, and oxidizing the waste water loaded with iron salts |
| CN102583861A (en) * | 2012-02-22 | 2012-07-18 | 中国海洋大学 | Method for preheating inflow water of membrane method seawater softening device |
| JP2013215686A (en) * | 2012-04-11 | 2013-10-24 | Jfe Engineering Corp | Method and apparatus for treating accompaniment water from winze |
| CN103523980A (en) * | 2013-10-29 | 2014-01-22 | 中国华电工程(集团)有限公司 | Method and system for high-efficiency recovery of high-salinity mine water |
| CN107117756A (en) * | 2017-05-18 | 2017-09-01 | 北京今大禹环境技术股份有限公司 | A kind of hotting mask couples desalination process |
| CN110451707A (en) * | 2019-07-01 | 2019-11-15 | 浙江工业大学 | A kind of waste water of mine Zero discharge treatment method |
-
2020
- 2020-09-29 CN CN202011047915.XA patent/CN112093966B/en active Active
Patent Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101462809A (en) * | 2008-12-25 | 2009-06-24 | 王俊川 | Comprehensive recovery method for heat energy and water from printing and dyeing industry wastewater and heat-exchanging system |
| DE102009041143A1 (en) * | 2009-09-14 | 2011-03-24 | Frederick Simon Oosthuizen | Processing mining waste water comprises separating sulfur metal ions and sulfate from water, reducing sulfur metal ions and sulfate to sulfide and removing the sulfide from waste water, and oxidizing the waste water loaded with iron salts |
| CN102583861A (en) * | 2012-02-22 | 2012-07-18 | 中国海洋大学 | Method for preheating inflow water of membrane method seawater softening device |
| JP2013215686A (en) * | 2012-04-11 | 2013-10-24 | Jfe Engineering Corp | Method and apparatus for treating accompaniment water from winze |
| CN103523980A (en) * | 2013-10-29 | 2014-01-22 | 中国华电工程(集团)有限公司 | Method and system for high-efficiency recovery of high-salinity mine water |
| CN107117756A (en) * | 2017-05-18 | 2017-09-01 | 北京今大禹环境技术股份有限公司 | A kind of hotting mask couples desalination process |
| CN110451707A (en) * | 2019-07-01 | 2019-11-15 | 浙江工业大学 | A kind of waste water of mine Zero discharge treatment method |
Non-Patent Citations (1)
| Title |
|---|
| 矿井废水处理零排放工艺设计实例;胡林;《净水技术》;20200725;第39卷(第07期);第41-45页 * |
Also Published As
| Publication number | Publication date |
|---|---|
| CN112093966A (en) | 2020-12-18 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN112093966B (en) | Energy-saving consumption-reducing method based on mine water zero-discharge full process | |
| CN107381688B (en) | Water and electricity cogeneration system for low-temperature multi-effect seawater desalination matched with high back pressure unit | |
| WO2023024962A1 (en) | Supercritical carbon dioxide cycle based power generation-brine lithium extraction coupling system | |
| CN103058438B (en) | Hot film coupling seawater desalination system | |
| CN213060793U (en) | Unpowered refrigeration cooling circulation system is used in making wine | |
| CN212609591U (en) | System for extracting sodium sulfate and sodium chloride from wastewater by separating salt based on nanofiltration membrane technology | |
| CN102583861B (en) | Method for preheating inflow water of membrane method seawater softening device | |
| CN210117309U (en) | Landfill leachate discharge to reach standard high-efficiency processing system | |
| CN115369195B (en) | Waste heat recovery system of blast furnace slag flushing water and working method thereof | |
| CN109578973B (en) | Deaerator system and working method | |
| CN211619981U (en) | Vinyl sulfate waste water treatment and recovery system | |
| CN210796508U (en) | Blast furnace slag flushing water independent water taking waste heat recovery system | |
| CN113880172A (en) | Low-temperature multi-effect evaporation seawater desalination energy utilization system and method | |
| CN112441690A (en) | RO seawater desalination device inlet seawater heating system based on waste heat recovery of thermal power generating unit | |
| CN111056580A (en) | Vinyl sulfate waste water treatment and recovery system | |
| CN211926226U (en) | Cooling system is used in soybean milk powder production | |
| CN101823739A (en) | Fine liquid heat exchange process for decomposing and producing sandy alumina in two stages | |
| CN201006401Y (en) | Membrane separation device for removing sulfate radical form salt solution | |
| CN218089644U (en) | Blast furnace slag flushing water waste heat recovery system | |
| CN220845532U (en) | Automatic recovery comprehensive utilization system for polysilicon reduction cooling water | |
| CN203668163U (en) | Device for nitrate removal by membrane method | |
| CN220745457U (en) | Gasification black water waste heat recovery system | |
| CN211546685U (en) | Water resource utilization system for electrolytic workshop | |
| CN216890492U (en) | Device for treating high-salinity wastewater through CPC coupling multiple-effect evaporation-electrodialysis | |
| CN220090925U (en) | Tail gas treatment device is used in stevioside production |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| CB02 | Change of applicant information |
Address after: 311201 Hangzhou, Xiaoshan District, Zhejiang Province Road No. 288 show Applicant after: Hangzhou Research Institute Co.,Ltd. Address before: 311201 Hangzhou, Xiaoshan District, Zhejiang Province Road No. 288 show Applicant before: CHINA COAL TECHNOLOGY & ENGINEERING GROUP HANGZHOU ENVIRONMENTAL PROTECTION INSTITUTE Co.,Ltd. |
|
| CB02 | Change of applicant information | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |