CN205023892U - Recovery unit is handled to crystallization salt - Google Patents
Recovery unit is handled to crystallization salt Download PDFInfo
- Publication number
- CN205023892U CN205023892U CN201520735142.2U CN201520735142U CN205023892U CN 205023892 U CN205023892 U CN 205023892U CN 201520735142 U CN201520735142 U CN 201520735142U CN 205023892 U CN205023892 U CN 205023892U
- Authority
- CN
- China
- Prior art keywords
- crystallizer
- adopts
- crystal salt
- cylindrical shell
- retrieving arrangement
- 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
- 150000003839 salts Chemical class 0.000 title claims abstract description 26
- 238000002425 crystallisation Methods 0.000 title claims abstract description 12
- 238000011084 recovery Methods 0.000 title claims abstract description 8
- 230000008025 crystallization Effects 0.000 title abstract description 8
- 239000013078 crystal Substances 0.000 claims abstract description 21
- 238000010438 heat treatment Methods 0.000 claims abstract description 11
- 238000002156 mixing Methods 0.000 claims abstract description 8
- 239000007788 liquid Substances 0.000 claims abstract description 5
- 238000000034 method Methods 0.000 claims description 31
- 239000002918 waste heat Substances 0.000 claims description 12
- 239000006200 vaporizer Substances 0.000 claims description 11
- 238000001704 evaporation Methods 0.000 claims description 7
- 230000008020 evaporation Effects 0.000 claims description 7
- 239000007789 gas Substances 0.000 claims description 5
- 238000009835 boiling Methods 0.000 claims description 4
- 238000007906 compression Methods 0.000 claims description 4
- 239000010408 film Substances 0.000 claims description 4
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 3
- 239000003546 flue gas Substances 0.000 claims description 3
- 230000004907 flux Effects 0.000 claims description 3
- 239000012528 membrane Substances 0.000 claims description 3
- 230000006835 compression Effects 0.000 claims description 2
- 239000011552 falling film Substances 0.000 claims description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 abstract description 14
- 125000004122 cyclic group Chemical group 0.000 abstract 1
- 239000002351 wastewater Substances 0.000 description 16
- 239000002699 waste material Substances 0.000 description 9
- 239000012267 brine Substances 0.000 description 7
- HPALAKNZSZLMCH-UHFFFAOYSA-M sodium;chloride;hydrate Chemical compound O.[Na+].[Cl-] HPALAKNZSZLMCH-UHFFFAOYSA-M 0.000 description 7
- 239000007787 solid Substances 0.000 description 5
- 238000005516 engineering process Methods 0.000 description 4
- 238000002203 pretreatment Methods 0.000 description 4
- 239000006002 Pepper Substances 0.000 description 2
- 230000000903 blocking effect Effects 0.000 description 2
- 238000003763 carbonization Methods 0.000 description 2
- 238000003889 chemical engineering Methods 0.000 description 2
- 238000009833 condensation Methods 0.000 description 2
- 230000005494 condensation Effects 0.000 description 2
- 230000007613 environmental effect Effects 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 238000003756 stirring Methods 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 229910002651 NO3 Inorganic materials 0.000 description 1
- NHNBFGGVMKEFGY-UHFFFAOYSA-N Nitrate Chemical compound [O-][N+]([O-])=O NHNBFGGVMKEFGY-UHFFFAOYSA-N 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 230000002950 deficient Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 239000000374 eutectic mixture Substances 0.000 description 1
- 239000002737 fuel gas Substances 0.000 description 1
- 238000005065 mining Methods 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 238000001223 reverse osmosis Methods 0.000 description 1
- 239000010865 sewage Substances 0.000 description 1
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
- Y02P10/00—Technologies related to metal processing
- Y02P10/25—Process efficiency
Landscapes
- Heat Treatment Of Water, Waste Water Or Sewage (AREA)
Abstract
The utility model discloses a recovery unit is handled to crystallization salt, include interconnect's evaporimeter, crystallizer and carbide furnace in proper order, the crystallizer adopts the forced circulation crystallizer, and the barrel intersegmental part of this forced circulation crystallizer adds establishes a two tubaeform barrel, macrostoma end position in the upper portion of crystallizer export of two tubaeform barrels is provided with in the bottom of forced circulation crystallizer and eluriates the pipe, be provided with the feed inlet and eluriate the mouth on eluriating the pipe, be provided with the viewing aperture on the barrel and wash the mouth, still set up the control appearance simultaneously, the control appearance links to each other at the central mixing stirrer of crystallizer with the setting for control liquid level, crystallization concentration and crystal size of a dimension, mixing stirrer has heating device, still has impeller or blade or spring leaf simultaneously. The utility model discloses steady operation that can the long period is difficult for causing the jam, and its heat and recycle -water can obtain cyclic utilization, and green, efficiency are higher, and no secondary pollution is safer.
Description
Technical field
The utility model relates to a kind of retrieving arrangement, is specifically related to a kind of crystal salt process retrieving arrangement.
Background technology
Along with the attention more of Environmental protection, start to control total emission volumn, general sewage can meet qualified discharge by the treatment technology such as biological, chemical.But, the a large amount of high slat-containing wastewaters produced for the national mainstay industry such as petrochemical complex, Coal Chemical Industry, electric power, oil recovery, mining pass through the waste water that the traditional means such as chemistry, film, reverse osmosis can only reclaim 75% ~ 85%, up to the present the remaining high-concentration salt-containing wastewater through concentrated 15% ~ 25% can not be effectively addressed, what have stores by tanning by the sun pond, as run into the disaster such as mountain torrents, geology, high-concentration salt-containing wastewater is once leak, by polluted surface, lithic drainage, bring endless trouble, particularly western water-deficient area.Therefore, the process of high slat-containing wastewater has become the great difficult problem that China's water resources and environment problem faces.
Crystal salt treatment process in this device is for China's shortage of water resources, recycling rate of water used by the industries is low, the problem that environmental pollution is serious, by trade effluent by techniques such as pre-treatment, evaporation, crystallizations, highly enriched, the high slat-containing wastewater of 15% ~ 25% after traditional water technology process are processed further, make the rate of recovery of water reach more than 95%, salt-pepper noise becomes solid salt simultaneously, realizes high slat-containing wastewater zero release.
In addition, different from traditional salt chemical engineering evaporation and crystal process, the crystal salt process of high slat-containing wastewater is due to the complicacy of waste component and water yield fluctuation, the physical parameter of waste water system is difficult to Obtaining Accurate, process design parameter is caused to depart from practical systems, in operational process, device can not long-period stable operation, especially crystallization apparatus, often because blocking causes stopping production.
Summary of the invention
For overcoming the deficiencies in the prior art, the utility model provides a kind of crystal salt process retrieving arrangement.
The technical scheme that the utility model is taked is: a kind of crystal salt process retrieving arrangement, comprise interconnective vaporizer, crystallizer and carbide furnace successively, described crystallizer adopts pump circulation crystallizer, the cylinder section inside of this pump circulation crystallizer adds a double horn shape cylindrical shell, the big opening end of described double horn shape cylindrical shell is positioned at the top of crystallizer outlet, the osculum end diameter 20-2000cm less of crystallizer diameter of double horn shape cylindrical shell; Be provided with in the bottom of pump circulation crystallizer and eluriate pipe, described elutriation pipe be provided with opening for feed and eluriate mouth, described cylindrical shell is provided with porthole and Butterworth Hatch, also monitor is set simultaneously, described monitor is connected with the mixing agitator being arranged on crystallizer center, for controlling liquid level, crystallisation concentration and crystalline size size; Described mixing agitator with heating unit, simultaneously also with paddle wheel or blade or spring piece.
Further, this device also comprises the pretreatment unit be made up of whipping appts, film treater, preheating apparatus and de-gassing vessel.
Further, described vaporizer adopts the wherein one in pump feed evaporator, vertically moving membrane vaporizer, horizontal falling-film evaporator.Vaporizer adopts single-action or multiple-effect evaporation, and adopts the combination of a kind of or three kinds of modes in external steam supply, mechanical vapor-compression, thermodynamic steam compression.
Further, described carbide furnace adopts rotary kiln type or pushed bat kiln formula or electric furnace, and its type of heating adopts gas heating or electrically heated.The high-temperature flue gas heat of carbide furnace adopts waste heat boiler to carry out waste heat recovery, and the low-pressure steam that waste heat boiler produces is used for the outer for steam of crystallizer; And described waste heat boiler adopts little temperature difference boiling heat transfer, its heat transfer tube adopts T-slot deferent or indent barrel or threaded pipe or tube with high flux.
The beneficial effects of the utility model are: highly enriched, the high slat-containing wastewater of 15% ~ 25% after traditional water technology process process by this device further, the rate of recovery of water is made to reach more than 95%, salt-pepper noise becomes solid salt simultaneously, realizes high slat-containing wastewater zero release.This device can macrocyclic steady running in addition, and not easily result in blockage, its heat and recycle-water can obtain recycle, and environmental protection, efficiency are higher, and non-secondary pollution is safer.Crystallizer adopts pump circulation to add elutriation tank, can improve product quality, and carbide furnace adopts rotary kiln, and the residence time is low.
Accompanying drawing explanation
Fig. 1 is structured flowchart of the present utility model.
Fig. 2 is the one-piece construction schematic diagram of crystallizer.
Embodiment
Below in conjunction with the drawings and specific embodiments, the utility model is described in detail.
As Fig. 1, shown in Fig. 2, a kind of crystal salt process retrieving arrangement, comprise interconnective vaporizer, crystallizer and carbide furnace successively, described crystallizer adopts pump circulation crystallizer, cylindrical shell 1 intersegmental part of this pump circulation crystallizer adds a double horn shape cylindrical shell 2, and the big opening end of described double horn shape cylindrical shell 2 is positioned at the top of crystallizer outlet 3, the osculum end diameter 20-2000cm less of crystallizer diameter of double horn shape cylindrical shell 2; Be provided with in the bottom of pump circulation crystallizer and eluriate pipe 4, described elutriation pipe 4 be provided with opening for feed 5 and eluriate mouth 6, described cylindrical shell 1 is provided with porthole 7 and Butterworth Hatch 8, monitor 11 is also set simultaneously, described monitor 11 is connected with the mixing agitator 10 being arranged on crystallizer center, for controlling liquid level, crystallisation concentration and crystalline size size; Described mixing agitator 10 with heating unit, simultaneously also with paddle wheel or blade or spring piece.
This device is different from traditional salt chemical engineering evaporation and crystal process, it will evaporate and be coupled with crystallization, by solid-liquid equilibrium principle, be separated azeotrope, eutectic mixture, homologue and the isolate that volatilization is all close relatively, different according to the Tc under different concns, break the restriction of azeotropic or equilibrium region, solve the crystal salt process of high slat-containing wastewater due to the complicacy of waste component and water yield fluctuation, the physical parameter of waste water system is difficult to Obtaining Accurate, process design parameter is caused to depart from practical systems, in operational process, device can not the problem such as long-period stable operation, especially crystallization apparatus, often because blocking causes stopping production.Crystallizer adopts pump circulation to add elutriation tank, can improve product quality, and heating adopts electrically heated or adopts vapour compressor (also can adopt four-effect evaporation and TVR).Described carbide furnace adopts rotary kiln type or pushed bat kiln formula or electric furnace, and its type of heating adopts gas heating or electrically heated.The high-temperature flue gas heat of carbide furnace adopts waste heat boiler to carry out waste heat recovery, and the low-pressure steam that waste heat boiler produces is used for the outer for steam of crystallizer; And described waste heat boiler adopts little temperature difference boiling heat transfer, its heat transfer tube adopts T-slot deferent or indent barrel or threaded pipe or tube with high flux.
Working process of the present utility model is:
(1) pre-treatment is carried out to high slat-containing wastewater, obtain pre-treatment brine waste;
(2) evaporated in vaporizer by described pretreated brine waste, and reclaim the water of condensation in evaporative process, the TDS of the brine waste wherein in vaporizer is greater than 150000mg/L;
(3) brine waste after evaporation carries out crystallization through crystallizer, and the water of condensation in crystallisation process is reclaimed, obtain crystal salt solid, wherein the TDS of brine waste is in a crystallizer greater than 300000mg/L, and crystal salt solid SS is at 100000-300000mg/L;
(4) crystal salt solid in crystallizer is carried out carbonization through carbide furnace, organics removal and nitrate, obtain crystal salt, and wherein the temperature of charring furnace controls at 600-700 DEG C, carbonization time 5-30min, and carbide furnace tail gas enters fuel gas combustion system and reclaims.
Wherein, described pre-treatment comprises dosing stirring, film process, preheats with degassed, first brine waste enters in whipping appts, dosing stirs, and adjust its pH value between 5 ~ 6, then make the brine waste after pH value adjustment enter in membrane treatment appts to process, then the waste water after process is sent in heat-exchanger rig and preheat, control temperature is heated to close to boiling point from normal temperature, finally will carry out degassed in pre-warmed waste water feeding degasser, to remove the gas wherein generated.
The utility model does not relate to the part prior art that maybe can adopt all same as the prior art and is realized.
Claims (6)
1. a crystal salt process retrieving arrangement, comprise interconnective vaporizer, crystallizer and carbide furnace successively, it is characterized in that: described crystallizer adopts pump circulation crystallizer, cylindrical shell (1) intersegmental part of this pump circulation crystallizer adds a double horn shape cylindrical shell (2), the big opening end of described double horn shape cylindrical shell (2) is positioned at the top of crystallizer outlet (3), the osculum end diameter 20-2000cm less of crystallizer diameter of double horn shape cylindrical shell (2); Be provided with in the bottom of pump circulation crystallizer and eluriate pipe (4), described elutriation pipe (4) be provided with opening for feed (5) and eluriate mouth (6), described cylindrical shell (1) is provided with porthole (7) and Butterworth Hatch (8), monitor (11) is also set simultaneously, described monitor (11) is connected with the mixing agitator (10) being arranged on crystallizer center, for controlling liquid level, crystallisation concentration and crystalline size size; Described mixing agitator (10) with heating unit, simultaneously also with paddle wheel or blade or spring piece.
2. crystal salt process retrieving arrangement according to claim 1, is characterized in that: also comprise the pretreatment unit be made up of whipping appts, film treater, preheating apparatus and de-gassing vessel.
3. crystal salt process retrieving arrangement according to claim 1, is characterized in that: described vaporizer adopts the wherein one in pump feed evaporator, vertically moving membrane vaporizer, horizontal falling-film evaporator.
4. the crystal salt process retrieving arrangement according to claim 1 or 3, is characterized in that: described vaporizer adopts single-action or multiple-effect evaporation, and adopts the combination of a kind of or three kinds of modes in external steam supply, mechanical vapor-compression, thermodynamic steam compression.
5. crystal salt process retrieving arrangement according to claim 1, is characterized in that: described carbide furnace adopts rotary kiln type or pushed bat kiln formula or electric furnace, and its type of heating adopts gas heating or electrically heated.
6. crystal salt process retrieving arrangement according to claim 1 or 5, is characterized in that: the high-temperature flue gas heat of described carbide furnace adopts waste heat boiler to carry out waste heat recovery, and the low-pressure steam that waste heat boiler produces is used for the outer for steam of crystallizer; And described waste heat boiler adopts little temperature difference boiling heat transfer, its heat transfer tube adopts T-slot deferent or indent barrel or threaded pipe or tube with high flux.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201520735142.2U CN205023892U (en) | 2015-09-22 | 2015-09-22 | Recovery unit is handled to crystallization salt |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201520735142.2U CN205023892U (en) | 2015-09-22 | 2015-09-22 | Recovery unit is handled to crystallization salt |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN205023892U true CN205023892U (en) | 2016-02-10 |
Family
ID=55256442
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201520735142.2U Active CN205023892U (en) | 2015-09-22 | 2015-09-22 | Recovery unit is handled to crystallization salt |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN205023892U (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106362568A (en) * | 2016-08-26 | 2017-02-01 | 江苏中圣高科技产业有限公司 | Overturn-type ammonia-process desulfurization device |
| CN107098416A (en) * | 2017-06-29 | 2017-08-29 | 合众高科（北京）环保技术股份有限公司 | A kind of Waste Water Treatment and its method of wastewater treatment with buffer unit |
-
2015
- 2015-09-22 CN CN201520735142.2U patent/CN205023892U/en active Active
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106362568A (en) * | 2016-08-26 | 2017-02-01 | 江苏中圣高科技产业有限公司 | Overturn-type ammonia-process desulfurization device |
| CN107098416A (en) * | 2017-06-29 | 2017-08-29 | 合众高科（北京）环保技术股份有限公司 | A kind of Waste Water Treatment and its method of wastewater treatment with buffer unit |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN105198148B (en) | High slat-containing wastewater zero-emission crystallizes salt treatment process and device | |
| CN109292797A (en) | A kind of brine waste sub-prime recovery method | |
| CN104973726A (en) | Recovery processing method of high salinity wastewater containing sodium chloride and sodium sulfate | |
| WO2006094437A1 (en) | A method and an multi-effect evaporation for waste water of alkylene oxides | |
| CN105152443A (en) | Method and system for recycling crystallized salt resources in high-salt-content wastewater zero discharge | |
| CN204417272U (en) | A kind of crystallization treatment device of high slat-containing wastewater | |
| CN104926011B (en) | The evaporative crystallization zero-discharge treatment system and processing method of a kind of high-COD waste water | |
| CN102515207A (en) | Method for recovering sulfate radicals from dechlorinated light salt brine to prepare anhydrous sodium sulfate | |
| CN113185048A (en) | Triple-effect evaporation system and process for evaporating and extracting salt from coking wastewater | |
| CN205023892U (en) | Recovery unit is handled to crystallization salt | |
| CN108585089A (en) | A kind of sodium chloride ammonium chloride divides salt crystallization processes and device | |
| CN104761009B (en) | A kind of Industrial sewage treatment system | |
| CN204779206U (en) | High COD evaporation of water crystallization zero release processing system that gives up | |
| CN210117305U (en) | Heat pump low temperature divides effluent treatment plant of salt | |
| CN103613106B (en) | Technique for preparing ammonium chloride by employing sodium bicarbonate production wastewater as raw material | |
| CN110228888B (en) | System and method for quality-separating purification of potassium sodium salt of fly ash water washing liquid | |
| CN103833092B (en) | A kind of concentration method of brine waste | |
| CN111003867A (en) | Salt-containing low-viscosity wastewater evaporation pretreatment process | |
| CN211310912U (en) | Landfill leachate membrane concentrate evaporation concentration system | |
| CN103833094A (en) | Method for treating high-salinity wastewater | |
| CN104014144A (en) | Multiple-effect evaporation system evaporation condensation water heat energy reutilizationoun device | |
| CN115259518A (en) | System and method for treating percolate concentrated solution | |
| CN203935630U (en) | Multi-effect evaporation system evaporation condensed water heat energy recycling device | |
| CN102701505A (en) | Equipment for treating H-acid production wastewater | |
| CN105016553A (en) | High-salinity wastewater treatment method |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CB03 | Change of inventor or designer information | ||
| CB03 | Change of inventor or designer information |
Inventor after: Guo Hongxin Inventor after: Xu Hao Inventor after: Li Dong Inventor after: Liu Feng Inventor after: Peng Yanmei Inventor after: Chen Fei Inventor after: Liu Dongming Inventor after: Yu Liangyong Inventor after: Wang Wei Inventor after: Guo Yanyong Inventor before: Guo Hongxin Inventor before: Li Dong Inventor before: Liu Feng Inventor before: Peng Yanmei Inventor before: Chen Fei |
|
| TR01 | Transfer of patent right | ||
| TR01 | Transfer of patent right |
Effective date of registration: 20180312 Address after: 211112 Jiangning City, Nanjing Province, the integrity of the road No. 2111, Co-patentee after: China Shenhua Coal to Liquid and Chemical Co., Ltd. Ordos Coal to Liquid Branch Patentee after: Zhongsheng High Science & Technology Industry Co., Ltd., Jiangsu Address before: 211112 Jiangning City, Nanjing Province, the integrity of the road No. 2111, Patentee before: Zhongsheng High Science & Technology Industry Co., Ltd., Jiangsu |