CN204151176U - The multi-effect evaporation system of coal chemical engineering equipment strong brine - Google Patents
The multi-effect evaporation system of coal chemical engineering equipment strong brine Download PDFInfo
- Publication number
- CN204151176U CN204151176U CN201420494999.5U CN201420494999U CN204151176U CN 204151176 U CN204151176 U CN 204151176U CN 201420494999 U CN201420494999 U CN 201420494999U CN 204151176 U CN204151176 U CN 204151176U
- Authority
- CN
- China
- Prior art keywords
- water
- effect
- condensation
- well heater
- strong brine
- 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
Classifications
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
Abstract
The utility model discloses the multi-effect evaporation system of coal chemical engineering equipment strong brine, solve the strong brine that prior art is difficult to process coal chemical engineering equipment generation, the problems such as system energy consumption is high, running cost is high, technical scheme comprise connect successively mixing tank, the shell-side of water of condensation preheater or pipe side, deoxygenator, static mixer and multi-effect evaporating device, described multi-effect evaporating device is connected with the pipe side of heat pump, salt slurry tripping device and water of condensation preheater or shell-side respectively; The pipe side of described water of condensation preheater or shell-side connect water of condensation storage bucket, and described salt slurry tripping device connects mixing tank, and the pneumatic outlet of described deoxygenator is also connected with heat pump.The utility model system is simple and reliable, flexible operation is easy, running cost is low, energy-saving and cost-reducing.
Description
Technical field
The utility model relates to a kind of industrial wastewater treatment system, specifically a kind of multi-effect evaporation system of coal chemical engineering equipment strong brine.
Background technology
The situation of the rich coal of China, oil starvation, weak breath determines with coal the fast development of the Chemical Industry being main production raw material, and Chemical Industry belongs to high water consumption industry, limited water resources can be utilized rationally and effectively, and reduce discharge of wastewater as far as possible, become an important issue of current Developing Coal Chemical Industry.Wherein, the advanced treatment of a large amount of strong brines that produces of coal chemical engineering equipment and reuse will be importances of enforcement " wastewater zero discharge ".
Multiple-effect evaporation technology at home Salt Industry widely uses, technology maturation, but the experience of successful Application is not also had at present in wastewater treatment industry, mainly because the strong brine that the strong brine of salt industry and coal chemical engineering equipment produce dechlorinates, outside sodium content difference, raw material composition and productive target all there is various difference, thus the direct multiple-effect evaporation technology by Salt Industry directly brings application is infeasible, be in particular in: (1) strong brine composition is different: can produce a large amount of brine waste in Coal Chemical Industry production process, this part waste water is through biochemical treatment, the strong brine obtained after film process needs to reclaim water of condensation further.This part strong brine compares bittern and the seawater of Salt Industry, and its composition is more complicated, and main component is: TDS 18000mg/l, COD 804mg/l, chlorion: 3000mg/l.Sulfate radical: 2558 mg/l, total silicon: 55mg/l, its waste water has following characteristics: organic content is high, complicated component, various difficult degradation and gathering of easily foaming; Easy fouling, mainly based on calcium sulfate; 3 chloride, the extremely strong ions of fluorine corrodibility.(2) processing target product requirements is different: although the strong brine of Coal Chemical Industry generation and the bittern of Salt Industry are all obtain mud salt and water to be separated with brine disposal, but Salt Industry is mainly in order to obtain edible or industrial salt, require high to the crystal salt quality obtained (purity, knot cleanliness), and low to the specification of quality of the water of condensation be separated.The strong brine that Coal Chemical Industry produces is then just in time contrary, because the water of condensation reclaimed can be back to system, therefore has requirement to the saltiness of water of condensation and organic content, and does not do requirement to the quality of crystal salt.(3) facility investment control and energy-saving and cost-reducing require higher: isolating phlegma in the strong brine produced from Coal Chemical Industry production process is lower consumption based on festival energy, the object of saving water resource, obviously direct economic benefit can't be produced, if the facility investment and the running cost that reclaim phlegma are too high, then lose more than gain, the producer that allows that also cannot be real uses this technology.
Summary of the invention
The purpose of this utility model is to solve the problems of the technologies described above, there is provided that a kind of simple and reliable process, flexible operation are easy, system is simple, facility investment and running cost low, energy-saving and cost-reducing coal chemical engineering equipment strong brine evaporation process system, is separated the phlegma obtained and meets the requirement of industrial reuse water.
The multi-effect evaporation system of the utility model coal chemical engineering equipment strong brine, comprise connect successively mixing tank, the shell-side of water of condensation preheater or pipe side, deoxygenator, static mixer and multi-effect evaporating device, described multi-effect evaporating device is connected with the pipe side of heat pump, salt slurry tripping device and water of condensation preheater or shell-side respectively; The pipe side of described water of condensation preheater or shell-side connect water of condensation storage bucket, and described salt slurry tripping device connects mixing tank, and the pneumatic outlet of described deoxygenator is also connected with heat pump.
Described salt slurry tripping device comprises suspension separator and separating centrifuge, the liquid exit of described multi-effect evaporating device is connected with suspension separator, the filtrate outlet at described suspension separator top is connected with mixing tank, the serum outlet of bottom goes out separating centrifuge and connects, and the filtrate outlet of described separating centrifuge is also connected with mixing tank.
Described heat pump comprises barometric condenser, airless injection system and water seal tank, end effect vapor seperator top gas outlet in described multi-effect evaporating device is connected with barometric condenser and airless injection system successively, and the bottom of barometric condenser is provided with water seal tank.
Described multi-effect evaporating device comprises three vapor seperators, and three of correspondence well heaters and three condensate drainings; The outlet of described static mixer is connected with the bottom inlet of three well heaters respectively, and the pneumatic outlet of each described well heater connects with the recycle feed mouth of corresponding vapor seperator, and the mixture outlet of each described well heater connects with corresponding condensate draining; Liquid exit bottom each vapor seperator connects with corresponding well heater and next stage well heater respectively, and wherein, the liquid exit bottom end effect vapour separator is connected with salt slurry tripping device; The pneumatic outlet at described condensate draining top connects with corresponding well heater, and bottom liquid outlet is store bucket through water of condensation preheater and water of condensation and is connected.
Described multi-effect evaporating device comprises I and imitates vapor seperator, II effect vapor seperator and II effect vapor seperator, and the I of correspondence imitates well heater, II effect well heater, III effect well heater, condensate draining, second condensed water groove and III effect condensate draining is imitated with the I of correspondence, I is imitated steam injector and is connected with the steam-in that I imitates well heater, and the flash steam outlet at I effect vapor seperator top imitates steam injector with I respectively and II steam-in of imitating well heater is connected; The flash steam outlet at described II effect vapor seperator top is connected with III steam-in of imitating well heater, and the flash steam outlet at described II effect vapor seperator top is connected with heat pump.
The described I liquid exit of imitating bottom condensate draining is imitated water of condensation shwoot groove with I and is connected, the pneumatic outlet that described I imitates water of condensation shwoot groove is connected with II steam-in of imitating well heater, the liquid exit of bottom is store bucket through water of condensation preheater and water of condensation and is connected, and the pneumatic outlet that described I imitates condensate draining top is connected with the steam-in that I imitates well heater.
The liquid exit of described second condensed water trench bottom is connected with water of condensation preheater through III effect condensate draining.
Described water of condensation preheater comprises I and imitates water of condensation preheater and III effect water of condensation preheater, and described mixing tank imitates water of condensation preheater through III effect water of condensation preheater and I and deoxygenator connects; The liquid exit of described I effect water of condensation shwoot groove is store bucket through I effect water of condensation preheater with water of condensation and is connected, and the liquid exit of described III effect condensate draining is store bucket through III effect water of condensation preheater with water of condensation and is connected.
Described vapor seperator is vertical vapor seperator, recycle feed mouth 500 ~ 600mm below liquid level of described vapor seperator.
The multiple-effect evaporation technique of the utility model coal chemical engineering equipment strong brine, comprise the following steps, behind water of condensation preheater preheats to 50 ~ 65 DEG C, enter deoxygenator coupling vacuum stripping after mixing tank adjust ph 4-5 sent into by the strong brine produced by coal chemical engineering equipment and remove bicarbonate ion in solution, then send into static mixer adjust ph to deliver to multi-effect evaporating device again 8 ~ 9 and carry out consecutive evaporation concentrate and obtain strong brine and phlegma, strong brine after concentrate divides mud device to isolate salt slurry and filtrate through salt slurry, and described filtrate is recycled to mixing tank; Described phlegma send water of condensation to store bucket after water of condensation preheater heat exchange cooling.
Heat pump discharge is sent into together with the non-condensable gas that the flash steam of the end effect vapor seperator top discharge in described multi-effect evaporating device and deoxygenator top are discharged.
Strong brine after described concentrate divides the process isolating salt slurry and filtrate in mud device to be at salt slurry: the strong brine after described concentrate first carries out suspension separation through suspension separator, upper strata filtrate sends into mixing tank, it is that salt slurry sends into feed bin that bottom slurry flows into the isolated solid filter residue of separating centrifuge, and isolated filtrate sends into mixing tank.
Heat pump comprises barometric condenser, airless injection system and water seal tank, at first the flash steam that end effect vapor seperator top in described multi-effect evaporating device is discharged and the non-condensable gas one that deoxygenator top is discharged are sent into after barometric condenser cools and are extracted emptying out through airless injection system, utilize the sealing effectiveness ensureing heat pump with the water seal tank be connected bottom barometric condenser.
Described multi-effect evaporating device comprises three well heaters and three condensate drainings of three vapor seperators and correspondence; Strong brine after described feeding static mixer adjust ph is sent into respectively in three well heaters and is heated up with steam heat-exchanging, the flash steam at each well heater top is sent in corresponding vapor seperator and is carried out circulation shwoot, crystallization, concentrated and vapor-liquid separation, and the steam water interface of bottom enters corresponding condensate draining and carries out vapor-liquid separation; Flash steam in described vapor seperator is discharged by top, liquid major part circulation after bottom is concentrated enters in corresponding well heater and heats up with steam heat-exchanging, rest part is sent in next stage well heater, sends into salt slurry tripping device by the rest part liquid of discharging bottom end effect vapor seperator as the strong brine after concentrate; Described condensate draining top gas is sent in corresponding well heater, and the phlegma of bottom send water of condensation to store bucket after water of condensation preheater heat exchange cooling.
Described multi-effect evaporating device comprises I and imitates vapor seperator, II effect vapor seperator and II effect vapor seperator, and the I of correspondence imitates well heater, II effect well heater, III effect well heater, and the I of correspondence imitates condensate draining, second condensed water groove and III effect condensate draining; Imitate from low-pressure steam out-of-bounds and I and imitate steam injector through I after the part flash steam of discharging at vapor seperator top mixes and send into I and imitate in well heater, the flash steam that the rest part of discharging from device top is sent out in the evaporation of I effect is sent in II effect well heater, the flash steam that II effect vapor seperator top is discharged is sent in III effect well heater, sends into heat pump discharge together with the non-condensable gas that the flash steam that III effect vapor seperator ejects discharge and deoxygenator top are discharged.
Described strong brine major part (80-90%) after static mixer adjust ph is sent in first level heater (namely I imitates well heater), and rest part is then sent in all the other well heaters respectively.Temperature in vapor seperator effectively can be regulated by being mixed into a small amount of strong brine in two effects or triple effect evaporation process.
The steam water interface of described I effect heater base is first sent into I effect condensate draining and is carried out vapor-liquid separation, the flash distillation of I effect water of condensation shwoot groove first sent into by the described I phlegma of imitating bottom condensate draining, the non-condensable gas flashed off sends into II effect well heater, the phlegma of bottom send water of condensation to store bucket after water of condensation preheater heat exchange cooling, and I is imitated condensate draining top expellant gas and sent I to imitate well heater.
The phlegma that the phlegma of described second condensed water trench bottom is first sent into bottom III effect condensate draining neutralization III effect condensate draining send water of condensation to store bucket together after water of condensation preheater heat exchange cooling.
Described water of condensation preheater comprises I and imitates water of condensation preheater and III effect water of condensation preheater, described strong brine is imitated after the heat exchange of water of condensation preheater heats up through III effect water of condensation preheater and I successively and is sent into deoxygenator, and the phlegma that described I imitates water of condensation shwoot trench bottom send water of condensation to store bucket after I effect water of condensation preheater heat exchange cooling; Phlegma bottom described III effect condensate draining send water of condensation to store bucket after III effect water of condensation preheater heat exchange cooling.
Described vapor seperator is vertical, adopts axial admission method, and controls recycle feed mouth 500 ~ 600mm below liquid level of vapor seperator.
Adopt crystal seed method scale removal, control solid content 20 ~ 25wt% in vapor seperator.
Contriver, while employing multiple-effect evaporation technique, for the feature of the strong brine that coal chemical industry produces, has carried out following improvement:
For the problem of high, the easy fouling of strong brine organic content that coal chemical industry produces, contriver has done following improvement:
1. adopt crystal seed method descalling technique, control often to imitate service temperature in vapor seperator and exist, solid load, at 20 ~ 25wt%, effectively can alleviate the generation of well heater scale problems, reaches long-cycle production and runs object.Maintain certain solids content in circulation fluid in vapor seperator, to ensure crystal seed quantity, normal production does not need plus seed, both can reduce chemical cost, additionally reduces the generation of solid waste, is conducive to environment protection.
2. in mixing tank, add dilute sulphuric acid to regulate pH value 4 ~ 5, strong brine Central Plains bicarbonate ion is converted into carbanion, strong brine temperature is made to enter deoxygenator temperature higher than the boiling point under its vacuum through water of condensation preheater preheats to 50 ~ 65 DEG C, reach coupling vacuum stripping degassed, bicarbonate ion in effective elimination strong brine, reaches the object of the fouling preventing heating tube.
3. regulate the pH value of strong brine to send into vapor seperator again after 8 ~ 9 at static mixer, can effectively prevent strong brine to the corrosion of equipment, the work-ing life of further raising equipment.
Ensureing that under the prerequisite to the multiple-effect evaporation effect of strong brine, in order to energy-saving and cost-reducing as much as possible, contriver has made following improvement to the utility model technique:
1. adopt triple effect evaporation technique, the flash steam that last vapor seperator top is discharged is introduced the thermal source as next effect vapor seperator in the well heater of next effect, achieve the step Appropriate application of energy, have that material heated time is short, velocity of evaporation is fast, concentration ratio is great, energy-saving effect remarkable advantage, and only this just can save quantity of steam and reaches 70%, further, the isolated gas in condensate draining top also introduces supplementing further as thermal source in corresponding well heater.
2. after heat exchange condensation, water of condensation after treatment can reuse, and effectively saved with water, achieve the requirement of wastewater zero discharge, the water of condensation indices of recovery meets industrial reuse water water quality requirement.
3. meeting for II effect vapor seperator provides on the basis of thermal source, the flash steam that I imitates vapor seperator Base top contact part pumpback can also be imitated steam injector through I and sends into I imitate as thermal source in well heater, to reclaim the consumption of heat minimizing from low-pressure steam out-of-bounds after mixing from low-pressure steam out-of-bounds.
4. after I imitates condensate draining, be also furnished with I imitate water of condensation shwoot groove, reclaim heat further and provide supplemental heat source for I effect vapor seperator, the heat energy in whole process system is reclaimed as much as possible.
5. adopt the flashed vapour that heat pump suction III effect vapor seperator top is discharged, to reach the higher vacuum tightness of end effect, increase evaporation effective temperature difference, improve the thermo-efficiency of whole system.
The strong brine produced for solving coal chemical industry easily foams the problem of gatherings, impact recovery phlegma purity, and contriver makes following improvement:
1. the design of three vapor seperators is independent is separately arranged, and is vertical, and adopts axial admission mode, and this feeding manner can the flash distillation of strong brine short mix, thus avoids a large amount of generations of foam.
2. because vapor seperator is vertical, the circulation discharge port connected with corresponding well heater is positioned at bottom vapor seperator, recycle feed mouth is controlled 500 ~ 600mm below liquid level, the short circuit temperature loss of vapor seperator internal recycle mother liquor can be reduced like this, improve effective heat transfer temperature difference, make strong brine rapid flash by the circulation impellent of large discharge, avoid a large amount of generations of foam, ensure distilled water quality.Simultaneously, due in the upper circular tube that well heater is connected with the recycle feed mouth of vapor seperator for liquid-vapor mixture, its density is less than the density of liquid phase in lower circulation tube that well heater is connected with the circulation discharge port of vapor seperator, thus circulation impellent can be increased, decrease the power consumption of this recycle circuit cocycle pump, save energy and reduce the cost further.
Beneficial effect:
System flow of the present utility model is simple, flexible operation is easy, and running cost is low, safe and reliable, energy conservation and consumption reduction effects obvious, and the area being adapted at lack of water serious is promoted the use of, and is particularly suitable for the chemical enterprise of low-pressure steam more than needed.Adopt technical solutions of the utility model, the pollution of waste water to environment can be reduced, and the higher reuse water of quality can be obtained, realize while waste water " zero " discharges, chemical plant installations water can being saved.
Accompanying drawing explanation
Fig. 1 is the utility model system diagram.
Wherein: 1-mixing tank; 2-contactor pump; 3-III effect water of condensation preheater; 4-I imitates water of condensation preheater; 5-deoxygenator; 6-static mixer; 7-charge pump; 8-I imitates recycle pump; 9-I imitates well heater; 10-I imitates vapor seperator; 11-I imitates steam injector; 12-I imitates condensate draining; 13-I imitates water of condensation shwoot groove; 14-I imitates condensate pump; 15-II effect recycle pump; 16-II effect well heater; 17-II effect vapor seperator; 18-second condensed water groove; 19-III effect recycle pump; 20-III effect well heater; 21-III effect vapor seperator; 22-III effect condensate draining; 23-III effect condensate pump; 24-discharge pump; 25-suspension separator; 26-separating centrifuge; 27-barometric condenser; 28-airless injection system; 29-water seal tank; 30-water of condensation storage bucket; 31-water of condensation transferpump, 32-upper circular tube, 33-lower circulation tube.
Embodiment
Below in conjunction with accompanying drawing, explanation is further explained to the utility model:
The utility model system is specially: mixing tank 1 is imitated the shell-side of water of condensation preheater 3 or pipe side, the shell-side of I water of condensation preheater 4 or pipe side, deoxygenator 5, static mixer 6, charge pump 7 and multi-effect evaporating device through contactor pump 2 and III and is connected, described multi-effect evaporating device comprise I ~ III effect well heater 9,16,20, I ~ III imitate condensate draining 12,18,22, I ~ III imitate vapor seperator 10,17,21, I ~ III imitate recycle pump 8,15,19, I imitates steam injector 11, I imitates water of condensation shwoot groove 13, I imitates condensate pump 14 and III effect condensate pump 23.
Wherein, steam injector 11 is imitated with I respectively in the steam-in that described I imitates well heater 9, I imitates the pneumatic outlet of condensate draining 12, the flash steam outlet that I imitates vapor seperator 10 connects, the recycle feed mouth of pneumatic outlet in the middle part of upper circular tube 32 imitates vapor seperator 10 with I that described I imitates well heater 9 top is connected, the liquid-inlet that described I is imitated bottom well heater 9 imitates the circulation discharge port bottom vapor seperator 10 through lower circulation tube 33 and I effect recycle pump 8 with I, form a pump circulation heat transfer process, the liquid-inlet that described I is imitated bottom well heater 9 is also connected with charge pump 7, strong brine is added for imitating in well heater 9 to I, the described I liquid exit of imitating bottom well heater 9 is imitated condensate draining 12 with I and is connected, described I is imitated vapor seperator 10 and is adopted axial admission, for vertical, recycle feed mouth in the middle part of it is positioned at I and imitates 500 ~ 600mm under vapor seperator 10 liquid level, the I of circulation discharge port on lower circulation tube 33 of bottom is imitated recycle pump 8 and imitate liquid-inlet bottom well heater 9 respectively with I and II liquid-inlet of imitating bottom well heater 16 is connected, and the flashed vapour at top exports imitates steam injector 11 and II vapour inlet of imitating well heater 16 is connected respectively with I, the described I liquid exit of imitating bottom condensate draining 12 is imitated water of condensation shwoot groove 13 with I and is connected, the vapour inlet that pneumatic outlet and the I at top imitate well heater 9 is connected, the pneumatic outlet that described I imitates water of condensation shwoot groove 13 top is connected with II gas feed of imitating well heater 16, and liquid exit is store bucket 30 through the pipe side of I effect condensate pump 14, I effect water of condensation preheater 4 or shell-side with water of condensation and is connected.
The annexation that described II effect well heater 16, II imitates vapor seperator 17 and second condensed water groove 18 is imitated with I, only have following difference: the liquid exit bottom second condensed water groove 18 is connected with III liquid-inlet of imitating condensate draining 22, the flash steam outlet at II effect vapor seperator 17 top is connected with III gas feed of imitating well heater 20.
Described III effect well heater 16, III imitates the annexation of vapor seperator 17 and III effect condensate draining 18 with II effect, only has following difference: the flashed vapour outlet at III effect vapor seperator 21 top is all connected heat pump with the pneumatic outlet at deoxygenator 5 top; Liquid exit bottom described III effect vapor seperator 21 imitates well heater 20 with III respectively and salt slurry tripping device is connected; Liquid exit bottom described III effect condensate draining 18 is store bucket 30 through the pipe side of III effect water of condensation preheater 3 or shell-side with water of condensation and is connected.
Described salt slurry tripping device comprises suspension separator 25 and separating centrifuge 26, liquid exit bottom described III effect vapor seperator 21 is connected with suspension separator 25, the filtrate outlet at described suspension separator 25 top is connected with mixing tank 1, the serum outlet of bottom goes out and is connected with separating centrifuge 26, and the filtrate outlet of described separating centrifuge 26 is also connected with mixing tank 1.
Described heat pump comprises barometric condenser 27, airless injection system 28 and water seal tank 29, the pneumatic outlet at described III effect vapor seperator 21 top is connected with barometric condenser 27 and airless injection system 28 successively, and the bottom of barometric condenser 27 is provided with water seal tank 29.
Process example:
Be treated to example with the strong brine that Inner Mongol coal chemical engineering equipment is discharged, strong brine normal amount is 80m
3/ h, maximum is 100m
3/ h, influent quality is shown in Table 1:
Table 1 strong brine influent quality
| Sequence number | Interventions Requested | Unit | Design water quality |
| 1 | Chemical oxygen demand (COD) | mg/L | 804 |
| 2 | pH | 7.5～9 | |
| 3 | Temperature | ℃ | ＜40 |
| 4 | Turbidity | ＜80 | |
| 5 | Saltiness | mg/L | 18000 |
| 6 | Ammonia nitrogen | mg/L | 15 |
| 7 | Volatile phenol (in phenol) | mg/L | 2 |
| 8 | Chlorine root | mg/L | 3000 |
| 9 | Sulfate radical | mg/L | 2558 |
| 10 | Fluorochemical | mg/L | 50 |
| 11 | Total alkalinity | mg/L | 1600 |
| 12 | Calcium | mg/L | 133 |
| 13 | Magnesium | mg/L | 50 |
| 14 | Soluble silicon | mg/L | 50 |
| 15 | Colloidal silicon | mg/L | 5 |
With reference to Fig. 1, described strong brine enters after mixing tank 1 regulates PH to 4 ~ 5 together with 10% (v) dilute sulphuric acid, after contactor pump 2 pressurizes, after the shell-side two-stage of imitating water of condensation preheater 3 and I effect water of condensation preheater 4 through III is successively preheated to 50 ~ 65 DEG C, deliver to deoxygenator 5 coupling vacuum stripping and remove bicarbonate ion in solution, again with NaOH alkali lye after static mixer 6 mixes and regulates PH to 8 ~ 9, after charge pump 7 pressurize, be divided into three stocks do not deliver to I ~ III well heater 9,16,20 in and steam carries out heat exchange intensification.
First burst of strong brine (accounting for the 80-90% of strong brine cumulative volume) imitates steam in well heater 9 at I carries out heat exchange intensification, the described I of entering imitates the 0.6MPA from battery limit (BL) that the steam in well heater 9 sprays into from I effect steam injector 11, the low-pressure steam of 158 DEG C and the part flash steam (accounting for 10% percent by volume that I imitates vapor seperator 10 top flash steam amount) from I effect vapor seperator 10, flash steam after heat exchange heats up constantly to be circulated by the I recycle feed mouth of imitating in the middle part of vapor seperator 10 through upper circular tube 32 and enters I and imitate vapor seperator 10 and carry out shwoot, crystallization, concentrate and vapor-liquid separation, I is imitated vapor seperator 10 top secondary flash gas major part and is entered II single-effect evaporator, I effect steam injector 11 supplementing as the low-pressure steam from battery limit (BL) is sent in small portion pumpback, to reduce the consumption of steam, I imitate vapor seperator 10 bottom part from liquid imitate the circulation of recycle pump 8 major part by circulation discharge port through I and send into I and imitate heat exchange in well heater 9, small portion is sent in II effect well heater 16.Steam water interface after I imitates well heater 9 steam heat-exchanging enters I effect condensate draining 12 and carries out vapor-liquid separation, top gas and heating steam are mixed together rear suction and enter in I effect well heater 9 as heat source, bottom liquid enters I imitates water of condensation shwoot groove 13 and carries out flash distillation, the flash steam flashed off send II effect well heater 16 as heat source with enter second strand of strong brine (accounting for the 5-10% of strong brine cumulative volume) of II effect well heater 16 and imitate by II the liquid that vapor seperator 17 bottom cycle sends into and carry out heat exchange intensification; I is imitated phlegma bottom water of condensation shwoot groove 13 and is imitated through I the pipe side indirect preheating strong brine that I effect water of condensation well heater 4 delivered to by condensate pump 14, and the phlegma after heat exchange cooling is delivered to water of condensation storage bucket 30 and collected.
Described I imitate vapor seperator 10 bottom part from small amount of liquids mix with second strand of strong brine (accounting for the 5-10% of strong brine cumulative volume) after imitate well heater 16 II and carry out heat exchange Posterior circle from the flash steam that I imitates vapor seperator 10 top and enter II effect vapor seperator 17 and carry out shwoot, crystallization, concentrate and vapor-liquid separation, II effect vapor seperator 17 bottom part from liquid send into II effect well heater 16 through II effect recycle pump 15 major part and carry out cycle heat exchange, small portion is sent in III effect well heater 20.The flash steam at II effect vapor seperator 17 top enters III effect well heater 20 as heat source.Steam water interface after II effect well heater 16 steam heat exchange enters second condensed water groove 18 and carries out vapor-liquid separation; The gas at second condensed water groove 18 top enters II effect vapor seperator 17 supplementing as heat source, and bottom liquid delivers to III effect condensate draining 22.
Described II effect vapor seperator 10 bottom part from small amount of liquids and the 3rd burst of strong brine (accounting for the 5-10% of strong brine cumulative volume) send into III effect well heater 20 and imitate from II and enter III effect vapor seperator 21 after vapor seperator 17 top flash steam carries out heat exchange and carry out shwoot, crystallization, concentrate and vapor-liquid separation, III effect vapor seperator 21 bottom part from liquid portion imitate well heater 20 heat up with steam heat-exchanging through III effect recycle pump 19 feeding III that circulates, rest part is delivered to suspension separator 25 through discharge pump 24 and is carried out suspension separation, mixing tank 1 is entered in overhead-liquid overflow, bottom slurry is sent from centrifugal separator 26 and carries out centrifugation, solid filter residue delivers to salt slurry feed bin, filtrate flows into mixing tank 1.After non-condensable gas feeding barometric condenser 27 cooling at described III effect vapor seperator 21 top flashed vapour and deoxygenator 5 top, emptying is extracted out by airless injection system 28, barometric condenser 27 outlet at bottom is connected with water seal tank 29, ensures the sealing effectiveness of pumped vacuum systems.Steam water interface after III effect well heater 20 steam heat-exchanging enters III effect condensate draining 22 and carries out vapor-liquid separation, top gas enters III effect well heater 20 as heat source together with the flash steam of III single-effect evaporator, phlegma bottom III effect condensate draining 22 delivers to the pipe side indirect preheating strong brine of III effect water of condensation preheater 3 through III effect condensate pump 23 pressurization, and the phlegma after heat exchange is delivered to water of condensation storage bucket 30 and collected.
Adopt crystal seed method descalling technique in the utility model vapor seperator, in vapor seperator, temperature controls at 110-45 DEG C.Control solid load 20 ~ 25%wt, normal production does not need plus seed, both can reduce chemical cost, additionally reduces the generation of solid waste, is conducive to environment protection.Meanwhile, can effectively alleviate heating tube fouling, reach the object that long-cycle production runs.
The phlegma that water of condensation storage bucket 30 is collected can send out-of-bounds reuse pool reuse after subsequent handling process after water of condensation transferpump 31 pressurizes.
Wherein, it is 97KPa (A), service temperature 100-110 DEG C that control I imitates working pressure in vapor seperator 10, in II effect vapor seperator 17, working pressure is 33KPa (A), service temperature 70-80 DEG C, and in III effect vapor seperator 21, working pressure is 10KPa (A), service temperature 45-55 DEG C.Water of condensation water quality after the utility model art breading is as shown in table 2 below:
The water of condensation water quality that table 2 strong brine evaporates
| Project | Unit | Index |
| PH value | 6-9 |
| COD(KMnO 4Method) | mg/L,O2 | ＜5 |
| Total organic carbon (TOC) | mg/L | ＜2 |
| Ammonia nitrogen | mg/L | ＜5 |
| Saltiness | mg/L | 100 |
The utility model is per hour reduces low-pressure steam consumption 4.3 tons, cooling water amount 260 tons, can obtain the higher reuse water of quality simultaneously, can effectively save coal chemical engineering equipment water, energy-saving and water-saving Be very effective after the utility model evaporative condenser.
In year effective production time 8000 hours, single Analysis of Nested Design processing power is by 100m
3/ h counts, and adopts saving in multiple-effect evaporation technique year that the utility model technique is more traditional to mark 7.68 ten thousand tons, coal, can obtain significant environmental benefit and economic benefit.
Claims (9)
1. the multi-effect evaporation system of a coal chemical engineering equipment strong brine, it is characterized in that, comprise connect successively mixing tank, the shell-side of water of condensation preheater or pipe side, deoxygenator, static mixer and multi-effect evaporating device, described multi-effect evaporating device is connected with the pipe side of heat pump, salt slurry tripping device and water of condensation preheater or shell-side respectively; The pipe side of described water of condensation preheater or shell-side connect water of condensation storage bucket, and described salt slurry tripping device connects mixing tank, and the pneumatic outlet of described deoxygenator is also connected with heat pump.
2. the multi-effect evaporation system of coal chemical engineering equipment strong brine as claimed in claim 1, it is characterized in that, described salt slurry tripping device comprises suspension separator and separating centrifuge, the liquid exit of described multi-effect evaporating device is connected with suspension separator, the filtrate outlet at described suspension separator top is connected with mixing tank, the serum outlet of bottom is connected with separating centrifuge, and the filtrate outlet of described separating centrifuge is also connected with mixing tank.
3. the multi-effect evaporation system of coal chemical engineering equipment strong brine as claimed in claim 1, it is characterized in that, described heat pump comprises barometric condenser, airless injection system and water seal tank, end effect vapor seperator top gas outlet in described multi-effect evaporating device is connected with barometric condenser and airless injection system successively, and the bottom of barometric condenser is provided with water seal tank.
4. the multi-effect evaporation system of the coal chemical engineering equipment strong brine as described in any one of claim 1-3, is characterized in that, described multi-effect evaporating device comprises three vapor seperators, and three of correspondence well heaters and three condensate drainings; The outlet of described static mixer is connected with the bottom inlet of three well heaters respectively, and the pneumatic outlet of each described well heater connects with the recycle feed mouth of corresponding vapor seperator, and the mixture outlet of each described well heater connects with corresponding condensate draining; Liquid exit bottom each vapor seperator connects with corresponding well heater and next stage well heater respectively, and wherein, the liquid exit bottom end effect vapour separator is connected with salt slurry tripping device; The pneumatic outlet at described condensate draining top connects with corresponding well heater, and bottom liquid outlet is store bucket through water of condensation preheater and water of condensation and is connected.
5. the multi-effect evaporation system of coal chemical engineering equipment strong brine as claimed in claim 4, it is characterized in that, described multi-effect evaporating device comprises I and imitates vapor seperator, II effect vapor seperator and II effect vapor seperator, and the I of correspondence imitates well heater, II effect well heater, III effect well heater, condensate draining, second condensed water groove and III effect condensate draining is imitated with the I of correspondence, I is imitated steam injector and is connected with the steam-in that I imitates well heater, and the flash steam outlet at I effect vapor seperator top imitates steam injector with I respectively and II steam-in of imitating well heater is connected; The flash steam outlet at described II effect vapor seperator top is connected with III steam-in of imitating well heater, and the flash steam outlet at described III effect vapor seperator top is connected with heat pump.
6. the multi-effect evaporation system of coal chemical engineering equipment strong brine as claimed in claim 4, it is characterized in that, the described I liquid exit of imitating bottom condensate draining is imitated water of condensation shwoot groove with I and is connected, the pneumatic outlet that described I imitates water of condensation shwoot groove is connected with II steam-in of imitating well heater, the liquid exit of bottom is store bucket through water of condensation preheater and water of condensation and is connected, and the pneumatic outlet that described I imitates condensate draining top is connected with the steam-in that I imitates well heater.
7. the multi-effect evaporation system of coal chemical engineering equipment strong brine as claimed in claim 4, is characterized in that, the liquid exit of described second condensed water trench bottom is connected with water of condensation preheater through III effect condensate draining.
8. the multi-effect evaporation system of coal chemical engineering equipment strong brine as claimed in claim 4, it is characterized in that, described water of condensation preheater comprises I and imitates water of condensation preheater and III effect water of condensation preheater, and described mixing tank imitates water of condensation preheater through III effect water of condensation preheater and I and deoxygenator connects; The liquid exit of described I effect water of condensation shwoot groove is store bucket through I effect water of condensation preheater with water of condensation and is connected, and the liquid exit of described III effect condensate draining is store bucket through III effect water of condensation preheater with water of condensation and is connected.
9. the multi-effect evaporation system of coal chemical engineering equipment strong brine as claimed in claim 3, it is characterized in that, described vapor seperator is vertical vapor seperator, recycle feed mouth 500 ~ 600mm below liquid level of described vapor seperator.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201420494999.5U CN204151176U (en) | 2014-08-29 | 2014-08-29 | The multi-effect evaporation system of coal chemical engineering equipment strong brine |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201420494999.5U CN204151176U (en) | 2014-08-29 | 2014-08-29 | The multi-effect evaporation system of coal chemical engineering equipment strong brine |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN204151176U true CN204151176U (en) | 2015-02-11 |
Family
ID=52509311
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201420494999.5U Active CN204151176U (en) | 2014-08-29 | 2014-08-29 | The multi-effect evaporation system of coal chemical engineering equipment strong brine |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN204151176U (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104193060A (en) * | 2014-08-29 | 2014-12-10 | 中国五环工程有限公司 | Multiple-effect evaporation technique and system for coal chemical industry device concentrated brine |
| CN105217703A (en) * | 2015-11-05 | 2016-01-06 | 陕西省石油化工研究设计院 | A kind of sextuple-effect evaporation crystallization apparatus and technique thereof being applied to zero discharge of industrial waste water |
| CN112891973A (en) * | 2021-01-15 | 2021-06-04 | 中国科学院上海应用物理研究所 | Method for reducing oxygen content in halide molten salt |
-
2014
- 2014-08-29 CN CN201420494999.5U patent/CN204151176U/en active Active
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104193060A (en) * | 2014-08-29 | 2014-12-10 | 中国五环工程有限公司 | Multiple-effect evaporation technique and system for coal chemical industry device concentrated brine |
| CN105217703A (en) * | 2015-11-05 | 2016-01-06 | 陕西省石油化工研究设计院 | A kind of sextuple-effect evaporation crystallization apparatus and technique thereof being applied to zero discharge of industrial waste water |
| CN112891973A (en) * | 2021-01-15 | 2021-06-04 | 中国科学院上海应用物理研究所 | Method for reducing oxygen content in halide molten salt |
| CN112891973B (en) * | 2021-01-15 | 2022-09-13 | 中国科学院上海应用物理研究所 | Method for reducing oxygen content in halide molten salt |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN104829026B (en) | High salt high concentration cellulose ether sewage disposal system | |
| CN106630332B (en) | Landfill leachate reverse osmosis concentration liquid processing method | |
| WO2006094437A1 (en) | A method and an multi-effect evaporation for waste water of alkylene oxides | |
| CN107902822A (en) | The recovery and treatment method of the high-salt wastewater of sodium chloride-containing and sodium sulphate | |
| CN102701303B (en) | Liquid-film low-temperature-evaporation zero-emission saline wastewater treatment method | |
| CN107902823A (en) | The recovery and treatment method of the high-salt wastewater of sodium chloride-containing and sodium sulphate | |
| CN104003422B (en) | Disposing mother liquor method new technology | |
| CN104310687B (en) | Efficient MVR integrated seawater desalination device and seawater desalination method | |
| CN107161965A (en) | A kind of wet-process phosphoric acid concentration waste gas recovering device and its technique | |
| CN102557317A (en) | Zero-discharge treatment process for salt-containing waste water | |
| CN204151176U (en) | The multi-effect evaporation system of coal chemical engineering equipment strong brine | |
| CN105236651A (en) | Technology for evaporating and crystallizing high concentration salt-containing wastewater in pulping and papermaking industries | |
| CN100577570C (en) | Method for producing salt by directly vacuum vaporizing bittern which is not being duplicate dried in field | |
| CN106830010A (en) | Methyl alcohol and ammonium chloride extraction equipment and extraction process in a kind of glycine production | |
| CN113185048A (en) | Triple-effect evaporation system and process for evaporating and extracting salt from coking wastewater | |
| CN202605748U (en) | Cycling concentration plant | |
| CN202193691U (en) | Equipment for triple-effect waste water desalination process | |
| CN104193060A (en) | Multiple-effect evaporation technique and system for coal chemical industry device concentrated brine | |
| CN105110396B (en) | Method and device for continuously separating low-boiling point substances in wastewater produced by extraction of natural gas and shale gas | |
| CN111003717A (en) | Device and method for preparing alkali salt by evaporating and crystallizing sea water desalination strong brine | |
| CN106145487A (en) | A kind of technique processing rare-earth trade high-concentration ammonia nitrogenous wastewater reuse | |
| CN104310514A (en) | Efficient mechanical vapor recompression seawater desalination method | |
| CN211971803U (en) | Novel materialized wastewater triple-effect evaporation system | |
| CN105129890A (en) | Evaporating crystallizer | |
| CN103043841B (en) | ADCA (Azodicarbonamide) foaming agent liquid waste disposal process |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant |