CN107265539A - A kind of processing method of high saliferous methanol waste water - Google Patents
A kind of processing method of high saliferous methanol waste water Download PDFInfo
- Publication number
- CN107265539A CN107265539A CN201710596578.1A CN201710596578A CN107265539A CN 107265539 A CN107265539 A CN 107265539A CN 201710596578 A CN201710596578 A CN 201710596578A CN 107265539 A CN107265539 A CN 107265539A
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- Prior art keywords
- methanol
- waste water
- rectifying column
- sodium chloride
- water
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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
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
- C02F1/06—Flash evaporation
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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
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
-
- 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
- C02F2101/10—Inorganic compounds
- C02F2101/101—Sulfur compounds
-
- 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
- C02F2101/10—Inorganic compounds
- C02F2101/12—Halogens or halogen-containing compounds
-
- 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
- C02F2101/30—Organic compounds
- C02F2101/34—Organic compounds containing oxygen
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- 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)
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Abstract
The present invention relates to a kind of processing method of high saliferous methanol waste water, i.e., using evaporation, crystallization, function of mechanical steam recompression (MVR) heat pump distillation, including rectifying column, tower top stream stock compressor, heat exchanger, separator.High saliferous methanol waste water (methanol, water, sodium chloride and sodium sulphate) is fed with saturated liquid state at ambient pressure, methanol waste water is separated in rectifying column, methanol is from overhead extraction product design up to 99.0% (mass fraction, similarly hereinafter), water is produced from bottom of towe, and methanol product concentration is less than 500ppm；Sodium chloride, saltcake crystallize precipitation respectively.Realize that tower self heat is integrated by MVR heat pumps, save the consumption of cold and hot public work, reduce energy consumption.99.0% methanol, 98.6% sodium chloride and the pure saltcake obtained simultaneously can be sold as product.
Description
Technical field
The invention belongs to chemical separation engineering field, it is related to the processing method of high saliferous methanol waste water, is to pass through specifically
Evaporation and distillation and separation method, to handle high saliferous methanol waste water, and by separating methanol.
Background technology
High salinity, that is, described salinity are more than 10g/L higher than l%, i.e. salinity.And high salinity waste water, not only wrap
Containing inorganic salts, wherein also containing large amount of organic and total dissolved solid thing.
High salt organic waste water is mainly derived from chemical industry, road deicing and food processing field, other sources that can not ignore
Also include dyeing waste water, saponin waste water, petroleum production wastewater, paper waste and waste water of pesticide industry discharge etc..High salt is organic
The total amount of waste water is huge and has increased trend year by year.If do not handled before discharge it, Coal Gas Washing Cycling Water
Soluble inorganic salt and the toxic organic compound of difficult degradation can cause serious environmental pollution.
The processing method of current high salt organic waste water is broadly divided into bioanalysis (halophile organism method) and physical-chemical process (film skill
Art, electrochemical process, burning method).But bioanalysis salinity is higher, the sludge acclimatization time is longer, influences also big on it, can destroy
Normal operation.Membrane technology operating cost is expensive and cases of Industrial Waste Water Treatments are less.Electrochemical process is produced in leather industry
High-salt wastewater effect is fine, but the energy needed for organics removal and salt is relatively low.Burning method is also easy to produce nitrogen oxides, bioxin etc.
Noxious material, while the seriously corroded of salt in waste water to device.Rectifying is the common methods of current separation methanol waste water.
Conventional methanol waste water is operated using rectifying column, and tower top is directly cooled down by condensed water, and tower reactor is carried by high-grade steam
Heating load, and methanol-water solution belongs to big temperature difference separation system, many conservation measures industrialization application technologies are immature, thus
Cause substantial amounts of energy waste.
The content of the invention
The deficiency that the present invention exists for the above method, proposes a kind of rectifying separation side for being concentrated by evaporation coupling MVR heat pumps
Method, that is, be concentrated by evaporation high saliferous methanol waste water, is separated out so that salt be crystallized, and methanol and crystal evaporate separation.This method has back
High income, energy consumption is low, makes full use of the heat in each device, the rational advantage of process organization.
A kind of processing method for high saliferous methanol waste water that the present invention is provided, distillation system includes rectifying column (8), tower top stream
Stock compressor (9,12), condenser (11,13,14).
Raw material enters flash tank (1) and carries out flash separation, and overhead product is the waste water containing methanol, is directly entered strict rectifying
Tower (8) carries out rectifying separation；Tower reactor product is sodium chloride, sodium sulphate mixture, and a small amount of organic wastewater, and is divided into two
Part, a part, which is circulated, gives heat exchanger (2) heat supply, and another part enters solid-liquid separator after condenser (3) condensation
(4), separator (4) overhead product is organic wastewater and a small amount of ion, and tower reactor crystallization separates out saltcake solid；Overhead product enters
Flash tank (6), the tower top methanol waste water of flash distillation is directly separated into rectifying column (8).Tower reactor repeats above-mentioned separation process, by steaming
Hair obtains solid sodium chloride.Organic wastewater and the ion overwhelming majority of residual return to vapo(u)rization system and continue to evaporate, minimal amount of useless
Liquid is discharged from bottom of towe.
The gas-phase methanol and water that flash tank (1) and flash tank (6) are obtained are directly entered rectifying column (8), rectifying column (8) tower top
Compressor (9) is connected, with forming loop by condenser after tower reactor heat exchange；Rectifying column (8) connection compressor (12) gives preheater
(5) by condenser (14) formation loop after exchanging heat；Rectifying column (8) is directly connected to condenser (13) formation loop.
Rectifying column is packed tower or plate column, is made up of rectifying section and stripping section, theoretical number of plates of rectifying tower is 20-50
Block；Operating pressure is normal pressure, and reflux ratio is 10-20；The perforated plate corrugated structured packing of filling tape in tower；The compression of single compressor
Than for 2-3；Overhead extraction mass fraction is more than or equal to 99.0% methanol, and bottom of towe extraction mass fraction is more than or equal to 99.5%
Water.
During conventional rectification, required heat is all inputted by external heating medium by reboiler, unnecessary heat
Amount is removed by the cooling medium of overhead condenser, result in and the demand of energy is greatly increased.The MVR heat pump distillations of the present invention,
By realizing that tower self heat is supplied by compressor, the consumption of substantial amounts of hot public work and cold public work is saved,
Realize energy-saving purpose.Meanwhile, after the processing of waste water, content can be isolated for 99.0% methanol, 98.6% chlorination
Sodium and 100% pure saltcake, can reclaim secondary utilization.
Brief description of the drawings
Fig. 1 is flow chart of the invention
Label is as follows in figure：1,6- gas-liquid separator；2,5- heat exchangers；3,11,13,14- condensers；4,7- separation of solid and liquid
Device；8- rectifying columns；9,12- compressors；10- tower reactor reboilers
Specific embodiment
The present invention is given a detailed account with reference to accompanying drawing：
Example 1：
Using the flow shown in accompanying drawing 1, contain methanol 10% (mass fraction, similarly hereinafter), water in high saliferous methanol waste water 1
77%, sodium chloride 7%, sodium sulphate 6%, inlet amount is 30000kg/h, is carried out at ambient pressure with saturation state into flash tank 1
Flash separation, overhead product is methanol waste water, is directly entered strict rectifying column 8 and carries out rectifying separation；Tower reactor product is sodium chloride,
Sodium sulphate mixture, and a small amount of methanol waste water, and it is divided into two parts, a part, which is circulated, gives the heat supply of heat exchanger 2, another portion
Lease making, which is crossed after condenser 3 (temperature be 15 DEG C) condensation, enters solid-liquid separator 4, the overhead product of separator 4 be organic wastewater and
A small amount of ion, tower reactor crystallization separates out 100% saltcake solid 4005.5kg/hr；Overhead product enters flash tank 6, the first of tower top
Alcohol waste water is directly separated into rectifying column 8.Tower reactor repeats above-mentioned separation process, and evaporation obtains 98.9% solid sodium chloride
1902.8kg/hr.Methanol waste water and the ion overwhelming majority of residual return to vapo(u)rization systems and continue to evaporate, and minimal amount of waste liquid is from tower
Discharge at bottom.The gas phase discharging that flash tank 1,6 is obtained is directly entered rectifying column 8, and rectifying column needs 38 pieces of theoretical plates, and operating pressure is
0.85atm, used filler is mellapak packing with holes, and tower diameter is 2.86 meters.Tower top discharges for methanol vapor phase, is divided into 3
Stock is flowed, partly extraction obtains product after the condensation of condenser 13 for one, and another part is back to rectifying column 8；Part II leads to
Enter compressor 12, compression ratio is 4.9, and compressor power consumption is 409.97kW, improve its pressure and temperature and returned to after the heat supply of preheater 5
It flow to rectifying column 8；Part III is passed through compressor 9, and compression ratio is 6.5, power consumption is 2033.04kW, improve pressure and temperature with
It is back to after tower reactor heat exchange in rectifying column 8.
It is calculated analytically, conventional about 15350.2 tons of mark coal/years of energy consumption under the feed composition, and heat pump distillation is by tower top
The latent heat of steam is used for bottom of towe and preheater is heated, and can save energy consumption, and energy consumption is about 4412.7 tons of mark coal/years, energy consumption reduction
72.01%.
Example 2：
Using the flow shown in accompanying drawing 1, contain methanol 8% (mass fraction, similarly hereinafter), water in high saliferous methanol waste water 2
80%, sodium chloride 7%, sodium sulphate 5%, inlet amount is 30000kg/h, is carried out at ambient pressure with saturation state into flash tank 1
Flash separation, overhead product is methanol waste water, is directly entered strict rectifying column 8 and carries out rectifying separation；Tower reactor product is sodium chloride,
Sodium sulphate mixture, and a small amount of methanol waste water, and it is divided into two parts, a part, which is circulated, gives the heat supply of heat exchanger 2, another portion
Lease making enters solid-liquid separator 4 after crossing condenser 3 (temperature is 15 DEG C) condensation, and separator overhead product is methanol waste water and few
The ion of amount, tower reactor crystallization separates out 100% saltcake solid 3330.4kg/hr；Overhead product enters flash tank 6, the methanol of tower top
Waste water is directly separated into rectifying column 8.Tower reactor repeats above-mentioned separation process, and evaporation obtains 98.6% solid sodium chloride
1921.8kg/hr.Methanol waste water and the ion overwhelming majority of residual return to vapo(u)rization systems and continue to evaporate, and minimal amount of waste liquid is from tower
Discharge at bottom.The gas phase discharging that flash tank 1,6 is obtained is directly entered rectifying column 8, and rectifying column needs 40 pieces of theoretical plates, and operating pressure is
0.85atm, used filler is mellapak packing with holes, and tower diameter is 2.35 meters.Tower top discharges for methanol vapor phase, is divided into 3
Stock is flowed, partly extraction obtains product after the condensation of condenser 13 for one, and another part is back to rectifying column 8；Part II leads to
Enter compressor 12, compression ratio is 4.6, and compressor power consumption is 454.34kW, improve its pressure and temperature and returned to after the heat supply of preheater 5
It flow to rectifying column 8；Part III is passed through compressor 9, and compression ratio is 6.2, and power consumption is 2308.36kW, improve pressure and temperature with
Rectifying column 8 is back to after tower reactor heat exchange.
It is calculated analytically, conventional about 17642.9 tons of mark coal/years of energy consumption under the feed composition, and heat pump distillation is by tower top
The latent heat of steam is used for bottom of towe and preheater is heated, and can save energy consumption, and energy consumption is about 5249.3 tons of mark coal/years, energy consumption reduction
70.25%.
Claims (3)
1. a kind of processing method of high saliferous methanol waste water, with following steps：
1. high saliferous methanol waste water (methanol, water, sodium chloride and sodium sulphate) is fed with saturation state at ambient pressure, by steaming
After hair, cooling, saltcake, sodium chloride crystallization are separated out.
2. evaporate obtained gas phase discharging and be directly entered rectifying column (8), separated first alcohol and water.
2. the method as described in claim 1：Rectifying column is it is characterized in that gas phase mixture is fed, and obtained top gaseous phase logistics divides
For three strands, one is partly produced as product after condenser (13) condensation, and another part is back to rectifying column (8)；Second
Stock is passed through compressor (12) and improves its pressure and temperature to being back to rectifying column (8) by condenser 14 after the heat supply of preheater 5, the
Three parts are passed through compressor (9) and improve its pressure and temperature with being also back to rectifying column (8) after tower reactor heat exchange.
3. the method as described in claim 1, rectifying column are it is characterized in that operating pressure is 0.85atm, tower top operation temperature is
60.7℃。
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| Application Number | Priority Date | Filing Date | Title |
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| CN201710596578.1A CN107265539A (en) | 2017-07-17 | 2017-07-17 | A kind of processing method of high saliferous methanol waste water |
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| CN201710596578.1A CN107265539A (en) | 2017-07-17 | 2017-07-17 | A kind of processing method of high saliferous methanol waste water |
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| CN107265539A true CN107265539A (en) | 2017-10-20 |
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| CN201710596578.1A Pending CN107265539A (en) | 2017-07-17 | 2017-07-17 | A kind of processing method of high saliferous methanol waste water |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109879722A (en) * | 2019-03-05 | 2019-06-14 | 肥城金塔机械有限公司 | Low-concentration ethanol recyclable device and method based on MVR |
| CN113800701A (en) * | 2021-09-27 | 2021-12-17 | 苏州环浩环保设备有限公司 | Method for recycling methanol waste liquid containing magnesium sulfate solid |
| CN114409004A (en) * | 2022-03-05 | 2022-04-29 | 北京中科康仑环境科技研究院有限公司 | Energy-saving recycling process for treating wastewater containing volatile substances |
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| CN103539299A (en) * | 2012-07-10 | 2014-01-29 | 南京大学 | Process for recycling wastewater containing low boiling-point organism such as formaldehyde and high-concentration inorganic salt |
| CN105218315A (en) * | 2015-10-09 | 2016-01-06 | 吴嘉 | A kind of divided-wall distillation column that uses refines method and the device of methyl alcohol in conjunction with heat pump |
| US20160228813A1 (en) * | 2015-02-10 | 2016-08-11 | Joseph M. Schwartz | Integrated process and apparatus for recovery of helium rich streams |
| CN106075947A (en) * | 2016-06-03 | 2016-11-09 | 天津大学 | Methanol four tower double-effect heat pump energy-saving equipment and method |
-
2017
- 2017-07-17 CN CN201710596578.1A patent/CN107265539A/en active Pending
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103539299A (en) * | 2012-07-10 | 2014-01-29 | 南京大学 | Process for recycling wastewater containing low boiling-point organism such as formaldehyde and high-concentration inorganic salt |
| US20160228813A1 (en) * | 2015-02-10 | 2016-08-11 | Joseph M. Schwartz | Integrated process and apparatus for recovery of helium rich streams |
| CN105218315A (en) * | 2015-10-09 | 2016-01-06 | 吴嘉 | A kind of divided-wall distillation column that uses refines method and the device of methyl alcohol in conjunction with heat pump |
| CN106075947A (en) * | 2016-06-03 | 2016-11-09 | 天津大学 | Methanol four tower double-effect heat pump energy-saving equipment and method |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109879722A (en) * | 2019-03-05 | 2019-06-14 | 肥城金塔机械有限公司 | Low-concentration ethanol recyclable device and method based on MVR |
| CN113800701A (en) * | 2021-09-27 | 2021-12-17 | 苏州环浩环保设备有限公司 | Method for recycling methanol waste liquid containing magnesium sulfate solid |
| CN114409004A (en) * | 2022-03-05 | 2022-04-29 | 北京中科康仑环境科技研究院有限公司 | Energy-saving recycling process for treating wastewater containing volatile substances |
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Application publication date: 20171020 |