CN106115821A - A kind of low energy consumption brine waste processes technique - Google Patents
A kind of low energy consumption brine waste processes technique Download PDFInfo
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- CN106115821A CN106115821A CN201610633697.5A CN201610633697A CN106115821A CN 106115821 A CN106115821 A CN 106115821A CN 201610633697 A CN201610633697 A CN 201610633697A CN 106115821 A CN106115821 A CN 106115821A
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- brine waste
- crystallizer
- energy consumption
- low energy
- salt
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- 238000000034 method Methods 0.000 title claims abstract description 34
- 239000012267 brine Substances 0.000 title claims abstract description 32
- HPALAKNZSZLMCH-UHFFFAOYSA-M sodium;chloride;hydrate Chemical compound O.[Na+].[Cl-] HPALAKNZSZLMCH-UHFFFAOYSA-M 0.000 title claims abstract description 32
- 239000002699 waste material Substances 0.000 title claims abstract description 31
- 238000005265 energy consumption Methods 0.000 title claims abstract description 17
- 150000003839 salts Chemical class 0.000 claims abstract description 40
- 239000007791 liquid phase Substances 0.000 claims abstract description 17
- 238000001704 evaporation Methods 0.000 claims abstract description 13
- 238000010438 heat treatment Methods 0.000 claims abstract description 10
- 239000002244 precipitate Substances 0.000 claims abstract description 5
- 229920006395 saturated elastomer Polymers 0.000 claims description 19
- 239000002002 slurry Substances 0.000 claims description 19
- 239000002994 raw material Substances 0.000 claims description 15
- 239000004149 tartrazine Substances 0.000 claims description 12
- 239000007788 liquid Substances 0.000 claims description 6
- 239000012530 fluid Substances 0.000 claims description 5
- 230000008676 import Effects 0.000 claims description 5
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 claims description 4
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims description 4
- 239000011780 sodium chloride Substances 0.000 claims description 4
- 239000007787 solid Substances 0.000 claims description 3
- 238000002485 combustion reaction Methods 0.000 claims description 2
- 239000012141 concentrate Substances 0.000 claims description 2
- -1 crystallizes Substances 0.000 claims description 2
- 238000002309 gasification Methods 0.000 claims description 2
- 239000013529 heat transfer fluid Substances 0.000 claims description 2
- 239000003345 natural gas Substances 0.000 claims description 2
- 239000002151 riboflavin Substances 0.000 claims description 2
- 239000013505 freshwater Substances 0.000 abstract description 14
- 230000008020 evaporation Effects 0.000 abstract description 7
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 abstract description 7
- 239000000243 solution Substances 0.000 abstract description 6
- 239000002351 wastewater Substances 0.000 description 14
- 238000005516 engineering process Methods 0.000 description 6
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 description 4
- FKNQFGJONOIPTF-UHFFFAOYSA-N Sodium cation Chemical compound [Na+] FKNQFGJONOIPTF-UHFFFAOYSA-N 0.000 description 4
- 229910001415 sodium ion Inorganic materials 0.000 description 4
- 238000002425 crystallisation Methods 0.000 description 3
- 230000008025 crystallization Effects 0.000 description 3
- 238000004519 manufacturing process Methods 0.000 description 3
- 239000000463 material Substances 0.000 description 3
- 238000004065 wastewater treatment Methods 0.000 description 3
- 230000008901 benefit Effects 0.000 description 2
- 230000006835 compression Effects 0.000 description 2
- 238000007906 compression Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 230000005611 electricity Effects 0.000 description 2
- 238000000909 electrodialysis Methods 0.000 description 2
- 238000002156 mixing Methods 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 239000002562 thickening agent Substances 0.000 description 2
- 238000004457 water analysis Methods 0.000 description 2
- BHPQYMZQTOCNFJ-UHFFFAOYSA-N Calcium cation Chemical compound [Ca+2] BHPQYMZQTOCNFJ-UHFFFAOYSA-N 0.000 description 1
- JLVVSXFLKOJNIY-UHFFFAOYSA-N Magnesium ion Chemical compound [Mg+2] JLVVSXFLKOJNIY-UHFFFAOYSA-N 0.000 description 1
- 239000003125 aqueous solvent Substances 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 229910001424 calcium ion Inorganic materials 0.000 description 1
- 230000015556 catabolic process Effects 0.000 description 1
- 239000002826 coolant Substances 0.000 description 1
- 238000006731 degradation reaction Methods 0.000 description 1
- 230000001934 delay Effects 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 238000004090 dissolution Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 238000009434 installation Methods 0.000 description 1
- 229910001425 magnesium ion Inorganic materials 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 238000010025 steaming Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 239000002912 waste gas Substances 0.000 description 1
Classifications
-
- 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
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)
- Heat Treatment Of Water, Waste Water Or Sewage (AREA)
Abstract
The invention discloses a kind of low energy consumption brine waste and process technique, it is characterized in that, comprise the following steps: brine waste is carried out after feed preheater heats liquid phase circulation system, the water in circulating-heating evaporation solution, salinity is made to improve constantly, finally crystallize, precipitate, separate, reach fresh water reuse, Gu the purpose of salt treatment, this technique has low energy consumption, reduced investment, the features such as operating cost is low, safe and environment-friendly, solve the high difficult problem high with energy consumption of investment of traditional handicraft.
Description
Technical field
The present invention relates to brine waste and process technique, the brine waste being specifically related to a kind of low energy consumption processes technique.
Background technology
At present, in industrial installation produce organic brine waste, according to salinity be divided into low concentration brine waste and
High-concentration salt-containing wastewater, high-concentration salt-containing wastewater refers to total dissolved solidss salt content TDS ＞ 10000mg/L, this effluent part by
High in salt content, biodegradability can be poor, it is impossible to uses conventional " pretreatment+biochemical treatment+electrodialysis+evaporative crystallization " route.
Then can use the processing mode of routine for low dense salt-containing organic wastewater, biochemical treatment process can effective degradation of organic substances, then
Through electrodialysis, low concentration brine waste is isolated strong brine, fresh water direct reuse, and strong brine is processing through evaporative crystallization,
Reach the requirement of wastewater zero discharge.
Evaporative crystallization technique utilizes heat to be separated by aqueous solvent heating and gasifying exactly, and the solute concentration in solution is continuous
Improving, initially form nucleus after reaching degree of dissolution saturation, along with the degree of supersaturation of solution produces, nucleus is constantly grown up, is assembled,
The visible solid particle of rear formation.Conventional evaporation technique have multiple-effect evaporation (cascaded utilization of energy, the effect the most energy consumptions of number are the lowest),
The types such as MVR technology (function of mechanical steam recompression evaporation), are generally concentrated into brine waste salinity 40 ~ 50% and deliver to thickener,
Further the salt of 40 ~ 50% being starched content in thickener and bring up to about 60%, the most again after centrifuge dewatering, wet salt packs
Process.
According to the existing condition of production, multiple-effect evaporation technology has that investment is low, operating cost is high and wastewater treatment capacity is big etc.
Feature；By vapour compression machine restricted influence when MVR technology has that cost of investment is high, operating cost is low, wastewater treatment capacity is big.How
With reasonably investment, relatively low production run cost, reach the identical current saliferous wastewater processing technology for the treatment of effect cost
Key issue.
Summary of the invention
The technical problem to be solved is to provide a kind of low energy consumption brine waste and processes technique, this technological process letter
Single, easy to control, energy consumption is low, 0.5Mpa saturated vapor consume: 0.06 ~ 0.1 ton of steam/1 ton waste water, power consumption <
6.0kW h/1 ton waste water, economic benefit is obvious, it is simple to commercial Application is promoted.
The present invention solves its technical problem and is adopted the technical scheme that:
A kind of low energy consumption brine waste processes technique, it is characterised in that comprise the following steps:
(a) raw material preheating: brine waste raw material is reduced pressure after indirect steam condensed heat transfer fluid to 68 DEG C by feed preheater
Circulating and evaporating system is entered to normal pressure.
(b) circulating and evaporating: the brine waste raw material after step (a) being heated adds liquid phase circulation system, through heater
After E102 is heated to 73 ~ 80 DEG C, liquid phase continuous gasification evaporates, and salt component constantly concentrates, crystallizes, precipitates.
(c) Secondary-steam heating: utilizing vacuum pump P104 to crystallizer V101 evacuation, keep in crystallizer V101 is true
Reciprocal of duty cycle is-0.055 ~-0.065MPa, and the secondary saturated vapor that crystallizer V101 produces is discharged from crystallizer V101 top, enters
Heater E102 shell side, heats circulating liquid, and the condensed fluid after heating enters back into feed preheater E101 and carries out pre-to raw material
Heat.
D salt slurry that step (b) is obtained by () drains into salt slurry concentration tank V103 bottom crystallizer V101, and salt slurry concentration tank divides
The saline separated out returns head tank V102, and solid wet salt is discharged from salt slurry concentration tank V103.
In technique scheme, described liquid phase circulation system is to be entered with circulating pump P102 by crystallizer V101 loop exit
Mouth pipeline 06 is connected, and circulating pump P102 outlet is connected with heater E102 tube side import pipeline 07, heater E102
Tube side outlet is connected with crystallizer V101 circulation import pipeline 08, so constitutes a liquid phase circulation system.
Preferably, in described step (c), secondary saturated vapor need to be by external heat source by two before entering heater E102
Heater E102 is entered back into after overheated 5 DEG C of secondary saturated vapor.
Described external heat source includes saturated vapor, electrical heating, conduction oil, combustion of natural gas heat release.
The present invention compared with prior art, has the following advantages and beneficial effect:
(1) energy consumption is low: use vacuum flash technology, heats with circulation fluid, the saturated steaming of 0.5Mpa after overheated 5 DEG C of secondary saturated vapor
Vapour consumes: 0.06 ~ 0.1 ton of steam/1 ton waste water, power consumption < 7.0kW h/1 ton waste water.
(2) reduced investment: this technique eliminates vapour compression machine and centrifuge, compared with MVR technique, cost of investment of the present invention
Save more than 40%.
(3) equipment is few, and efficiency is high, easy to operate: whole device is taked to automatically analyze control device, grasps without Field Force
Make, save personnel cost.
(4) single covering device is particularly suitable for processing the production of below waste water scale 5t/h: whole device can make 2-3 sledge
Block, transport, move the most convenient.
(5) environmental protection, safe and reliable: without any waste gas, discharging of waste liquid, it is achieved zero emission of wastewater treatment requirement.
Accompanying drawing explanation
Fig. 1 is present invention process flow chart.
01～22-pipeline, V101-crystallizer, V102-head tank, V103-salt slurry concentration tank, V104-fresh water delays
Rushing tank, E101-feed preheater, E102-heater, E103-vacuum cooler, P101-raw material dosing pump, P102-follows
Ring pump, P103-fresh water pump, P104-vacuum pump.
Detailed description of the invention
Below in conjunction with embodiment and accompanying drawing, the present invention is described in further detail, but embodiments of the present invention are not
It is limited to this.
Embodiment 1
(1) by raw material brine waste component: total dissolving salt content 8500mg/L, sodium ion 2350mg/L, chloride ion 4115mg/L,
Also have the calcium ions and magnesium ions solution of trace, pH value 8.23, temperature 36.4 DEG C, pressure: normal pressure, flow: 2140kg/h, pass through centrifugal pump
It is forced into 0.4MPa (G) and is heated to 68.4 DEG C by feed preheater, after being then passed through being decompressed to normal pressure, enter liquid phase circulation system
System.
(2), in liquid phase circulation system, brine waste heats through heater through circulating pump forced circulation, brine waste
After, continuous steam raising, in crystallizer, vacuum is-0.06Mpa, and the indirect steam of evaporation is discharged from crystallizer top, enters
Heater and shell side, mix after first reducing pressure with the saturated vapor under 0.5Mpa pressure before entering shell side, mixes superheated steam temperature
Degree is 80.09 DEG C.
After mixing superheated steam during (3) (2nd) heats with the brine waste in heater, about 95% is condensed into
Liquid phase, also about 5% is the saturated vapor under the conditions of-0.07Mpa, and now temperature is 69.1 DEG C, enter back into feed preheater with
Raw material brine waste preheats so that material liquid is heated to 68.4 DEG C while being cooled to 60 DEG C by condensed fluid.The coldest
But liquid enters fresh water surge tank and gets fresh water reuse through fresh water pump, and now fresh water analysis indexes is: total dissolving salt content 199mg/
L, sodium ion 21.6mg/L, chloride ion 20.2mg/L, electrical conductivity: 234uS/cm, pH value 6.8, meet recycle-water requirement.
(4) in the crystallizer during (2nd), along with the continuous steam raising of liquid phase water, the salinity in solution by
Gradually improve, when reaching salt saturated mode, initially form nucleus, and gradually grow up, precipitate, be finally enriched at the bottom of the equipment of crystallizer
Portion, now salt slurry content about 40%.
(5) control crystalliser feet salt discharge speed, make the salt slurry content of crystalliser feet about 50%, by salt slurry with
From the streamed salt slurry concentration tank that enters, the salt slurry isolated saline of concentration tank returns head tank circulating and evaporating, and (water content is about for wet salt
10%) can directly pack process.
The energy consumption of the present embodiment is as follows with power consumption:
Steam consumption: 0.5Mpa pressure saturated vapor consumption per hour is 128kg, and unit consumption is 59.81kg/1t waste water.
The total power consumption of device: raw material motors of metering pumps power 0.75kW, fresh water pump power of motor 0.75kW, circulating pump 2.2
KW, vacuum pump 3.0 kW, total power consumption: 6.7 kW.
Steam is according to 200 yuan/ton, and electricity is counted according to 0.8 yuan/kW, equivalent operating cost: 17.32 yuan/1 ton waste water.
Embodiment 2
(1) by raw material brine waste component: total dissolving salt content 27300mg/L, sodium ion 1140mg/L, chloride ion 14260mg/
L, pH value 7.9, temperature 38.2 DEG C, pressure: normal pressure, flow: 5400kg/h, it is forced into 0.4MPa (G) by former by centrifugal pump
Material preheater is heated to 68.0 DEG C, enters liquid phase circulation system after being then passed through being decompressed to normal pressure.
(2), in liquid phase circulation system, brine waste heats through heater through circulating pump forced circulation, brine waste
After, continuous steam raising, in crystallizer, vacuum is-0.061Mpa, and the indirect steam of evaporation is discharged from crystallizer top, enters
Heater and shell side, mix after first reducing pressure with the saturated vapor under 0.5Mpa pressure before entering shell side, mixes superheated steam temperature
Degree is 82.58 DEG C.
After mixing superheated steam during (3) (2nd) heats with the brine waste in heater, about 91% is condensed into
Liquid phase, also about 9% is the saturated vapor under the conditions of-0.069Mpa, and now temperature is 69.86 DEG C, enters back into feed preheater
Preheat with raw material brine waste so that material liquid is heated to 68.0 DEG C while being cooled to 61.12 DEG C by condensed fluid.So
Rear coolant enters fresh water surge tank and gets fresh water reuse through fresh water pump, and now fresh water analysis indexes is: total dissolving salt content
268mg/L, sodium ion 28.8mg/L, chloride ion 24.1mg/L, electrical conductivity: 264uS/cm, pH value 6.6, meet recycle-water requirement.
(4) in the crystallizer during (2nd), along with the continuous steam raising of liquid phase water, the salinity in solution by
Gradually improve, when reaching salt saturated mode, initially form nucleus, and gradually grow up, precipitate, be finally enriched at the bottom of the equipment of crystallizer
Portion, now salt slurry content about 42%.
(5) control crystalliser feet salt discharge speed, make the salt slurry content of crystalliser feet about 50%, by salt slurry with
From the streamed salt slurry concentration tank that enters, the salt slurry isolated saline of concentration tank returns head tank circulating and evaporating, and (water content is about for wet salt
10%) can directly pack process.
The energy consumption of the present embodiment is as follows with power consumption:
Steam consumption: 0.5Mpa pressure saturated vapor consumption per hour is 500kg, and unit consumption is 92.59kg/1t waste water.
The total power consumption of device: raw material motors of metering pumps power 1.1kW, fresh water pump power of motor 1.1kW, circulating pump 11 kW, very
Empty pump 15.0 kW, total power consumption: 28.2 kW.
Steam is according to 200 yuan/ton, and electricity is counted according to 0.8 yuan/kW, equivalent operating cost: 22.69 yuan/1 ton waste water.
Claims (4)
1. a low energy consumption brine waste processes technique, it is characterised in that comprise the following steps:
(a) raw material preheating: brine waste raw material is reduced pressure after indirect steam condensed heat transfer fluid to 68 DEG C by feed preheater
Circulating and evaporating system is entered to normal pressure；
(b) circulating and evaporating: the brine waste raw material after step (a) being heated adds liquid phase circulation system, through heater E102
After being heated to 73 ~ 80 DEG C, liquid phase continuous gasification evaporates, and salt component constantly concentrates, crystallizes, precipitates；
(c) Secondary-steam heating: utilize vacuum pump P104 to crystallizer V101 evacuation, keep the vacuum in crystallizer V101
The secondary saturated vapor produced for-0.055 ~-0.065MPa, crystallizer V101 is discharged from crystallizer V101 top, enters heating
Device E102 shell side, heats circulating liquid, and the condensed fluid after heating enters back into feed preheater E101 and preheats raw material；
D salt slurry that step (b) is obtained by () drains into salt slurry concentration tank V103 bottom crystallizer V101, and salt slurry concentration tank is isolated
Saline return head tank V102, solid wet salt from salt slurry concentration tank V103 discharge.
A kind of low energy consumption brine waste the most according to claim 1 processes technique, it is characterised in that: described step (b)
In, liquid phase circulation system is to be connected with circulating pump P102 import pipeline 06 by crystallizer V101 loop exit, circulating pump
P102 outlet is connected with heater E102 tube side import pipeline 07, and the outlet of heater E102 tube side circulates with crystallizer V101
Import pipeline 08 is connected, and so constitutes a liquid phase circulation system.
A kind of low energy consumption brine waste the most according to claim 1 processes technique, it is characterised in that: described step (c)
In, secondary saturated vapor need to be entered back into heating by external heat source before entering heater E102 after overheated for secondary saturated vapor 5 DEG C
Device E102.
A kind of low energy consumption brine waste the most according to claim 3 processes technique, it is characterised in that: described external heat source
Including saturated vapor, electrical heating, conduction oil, combustion of natural gas heat release.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610633697.5A CN106115821A (en) | 2016-08-05 | 2016-08-05 | A kind of low energy consumption brine waste processes technique |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
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| CN201610633697.5A CN106115821A (en) | 2016-08-05 | 2016-08-05 | A kind of low energy consumption brine waste processes technique |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN106115821A true CN106115821A (en) | 2016-11-16 |
Family
ID=57255113
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106483946A (en) * | 2016-12-22 | 2017-03-08 | 北京憶众联创电气科技有限公司 | A kind of metallurgical production process energy consumption of unit product on-line detecting system and method |
| CN106830142A (en) * | 2017-03-14 | 2017-06-13 | 湖北科林博伦新材料有限公司 | A kind of brine waste concentration technology and device |
| CN109095682A (en) * | 2018-08-31 | 2018-12-28 | 广东粤电靖海发电有限公司 | Desulphurization for Coal-fired Power Plant Waste water concentrating sofening treatment method and device |
| CN112791438A (en) * | 2020-12-28 | 2021-05-14 | 魏永阳 | Cold energy desalination system and process for treating salt water |
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| CN109095682A (en) * | 2018-08-31 | 2018-12-28 | 广东粤电靖海发电有限公司 | Desulphurization for Coal-fired Power Plant Waste water concentrating sofening treatment method and device |
| CN112791438A (en) * | 2020-12-28 | 2021-05-14 | 魏永阳 | Cold energy desalination system and process for treating salt water |
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Application publication date: 20161116 |
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