CN101935077B - Waste acid concentration multistage treatment method - Google Patents
Waste acid concentration multistage treatment method Download PDFInfo
- Publication number
- CN101935077B CN101935077B CN2010102665069A CN201010266506A CN101935077B CN 101935077 B CN101935077 B CN 101935077B CN 2010102665069 A CN2010102665069 A CN 2010102665069A CN 201010266506 A CN201010266506 A CN 201010266506A CN 101935077 B CN101935077 B CN 101935077B
- Authority
- CN
- China
- Prior art keywords
- evaporation heater
- imitated
- heater
- steam
- spent acid
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
Images
Landscapes
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
- Heat Treatment Of Water, Waste Water Or Sewage (AREA)
Abstract
The invention relates to a waste acid concentration multistage treatment method which comprises the following steps of: heating 20-22% waste acid by a preheater, evaporating by a one-effect evaporation heater and a double-effect evaporation heater, cooling by a cooler and crystallizing by a crystallizer; heating by a triple-effect evaporation heater and separating by a separator to obtain 65% concentrated acid. The secondary steam part is used as a heat source part of the next stage heater and is condensed by spraying cooling water, wherein the one-effect evaporation heater and the double-effect evaporation heater are falling film graphite tube array evaporation heaters; the triple-effect evaporation heater is a floating head tube array graphite heat exchange. The water evaporation capability of the method is increased from 2.5 tons to 10 tons, and the stage number is 3 or more. A large amount of steam and cooling water is saved, and the pollution to the environment is reduced. The heat exchange area of equipment is reduced by 30%, and materials are saved and manufacturing cost is reduced correspondingly. The heat of steam is fully utilized, more than 35% of steam is saved, and more than 30% of cooling water can be saved. The condensed water part of the steam is used as the hear source part of the preheater and is recycled for other uses.
Description
Technical field
The present invention relates to a kind of low-concentration waste acid and reclaim discharge-reducing method, relate to a kind of evaporation characteristic of utilizing the body lotion vacuum flashing specifically, the water evaporates in the body lotion is come out, reach the method that spent acid concentrates the concentrated multistep treatment of spent acid of the purpose of recycling.
Background technology
Sulfuric acid is the primary raw material of Titanium White Production By Sulfuric Acid Process, has a large amount of spent acid to produce in the production process.Different according to technology, generally the hydrolysis spent acid with concentration 17%-22% is called the concentrated sulfuric acid, and 4-10% is the bleaching spent acid; Generally speaking; Produce the 1t finished product and can produce the 3.5t dilute sulfuric acid, wherein the 15%-20% of diluted acid total amount returns hydrolysis procedure, in order to the usefulness of the dilution concentrated sulfuric acid.But traditional spent acid concentrates and exists energy consumption height, big, the concentrated back of equipment investment concentration not to reach instructions for use.
Zou builds the new people of grade in " ilmenite prepares the acid of titanium white by product sulfur waste and concentrates Study on reuse " " chemical industry mineral and processing "; 2005 the 3rd phases: 16 pages-18 pages; In one literary composition; Point out to adopt common spent acid enrichment facility to inquire into regard to steam concentrating waste acid method, its equipment mainly is made up of diffuser, mist device, vaporizer, heat exchanger and vapour liquid separator.Implementation step is with squeezing into the spent acid enrichment facility after spent acid sedimentation, filtration, the slagging-off, feeding steam and carry out heat exchange, through making mist, vapor-liquid separation; Discharging carbonated drink obtains 37% concentrated vitriol, and technological process is as shown in Figure 1; And point out hereof can improve the spent acid reclamation rate once again, but can propose very big challenge concentrator and concentration flow path if on 37% concentrated acid basis, improve the quality mark again; Influence the maturity of equipment operation, and will increase cost, because along with the raising of concentrated acid mass fraction; The boiling point of sulfuric acid raises rapidly, and heat energy efficiency reduces.
Summary of the invention
Technical problem to be solved by this invention provides the method that a kind of spent acid concentrates multistep treatment.
For solving the problems of the technologies described above, the present invention realizes like this
Spent acid concentrates the multistep treatment method, comprises the steps:
Spent acid is through after the heating of I effect evaporation heater, after the I effect separator separates; The part of liquid-state material is returned I effect evaporation heater through circulating pump, and another part input II is imitated evaporation heater, after II is imitated evaporation heater and II effect separator separates; A part is returned II effect evaporation heater through circulating pump; Another part cools off through cooler, and filter residue is recycled after crystallizer crystallization, the separator separates, and filtrating input III is imitated the evaporation heater heating, vapor seperator separates the back and discharges concentrated acid;
I is imitated evaporation heater and is made thermal source with saturated vapor, is used to heat spent acid in the condensed water input preheater, and the condensed water of preheater is recycled;
III effect evaporation heater utilizes steam as thermal source, and condensed water is recycled;
II is imitated vapor seperator and after the water quench of spray condenser, is done wastewater treatment with the steam that the evaporation separation chamber discharges.
Aforesaid spent acid concentrates the multistep treatment method, and described I is imitated, II effect evaporation heater is a falling liquid film graphite tubulation evaporation heater; It is tubular graphitic heat-exchanger that III is imitated evaporation heater.
Aforesaid spent acid concentrates the multistep treatment method, it is characterized in that the spent acid amount in the evaporation heater reaches before the internal circulating load, and material only circulates in evaporation heater and vapor seperator through circulating pump,
Aforesaid spent acid concentrates the multistep treatment method, it is characterized in that getting into I at spent acid imitates evaporation heater before through the preheater preheating, and the thermal source of preheater is the condensed water that I is imitated evaporation heater.
The present invention has following positive effect:
The evaporation efficiency of falling film evaporator is higher, and its overall heat-transfer coefficient is the highest can to reach 2000Kcal/m
2H ℃; But the key of its high-efficiency evaporating is must the raw water of cold conditions be formed the layer of even fluid film at the tube interior of evaporimeter; Liquid distribution trough can be forced to form the raw water that gets into evaporimeter along the uniform fluid film of the ring-type of tube wall; This invention is as a Series Design, and the evaporation water ability is from 2.5 tons to 10 tons, and progression is 3 grades or more.Can substitute the single-action or the double-effect evaporation technology of present widespread usage, thereby save a large amount of steam and cooling water, reduce pollution environment.
Reduce equipment heat exchange area 30%, correspondingly saved material and reduced manufacturing cost.The heat of steam is fully used, and saves steam more than 35%, can save cooling water more than 30% simultaneously.
Description of drawings
Fig. 1 is the flow chart of traditional spent acid treatment process;
Fig. 2 concentrates the annexation sketch map of multistep treatment device for spent acid;
But Fig. 3 is the structural representation of replace tubes formula tubulation graphite heat exchanger;
The description of symbols of critical piece among Fig. 3:
A acid outlet, B show on trial, C condensate liquid discharging hole, the outlet of D incoagulable gas, E acid import, F steam inlet, subsequent use mouth of G, the outlet of H incoagulable gas, J condensate outlet, M, deflection plate, K1 vapour-liquid export, the subsequent use mouth of K2 liquid level gauge;
Fig. 4 is the vertical view of Fig. 3;
Fig. 5 is the structural representation of falling liquid film part;
The description of symbols of critical piece among Fig. 5: 1 upper cover, 2, branch spreading liquid dish, 3, ground floor cloth liquid dish, 4, second layer cloth liquid dish, 5, graphite bolt, 6, graphite liquid-dividing head, 7, graphite grazing nut, 8, rubber seal, 10, graphite heat exchanger tube, 11, graphite tube plate, 12, graphite downspout
Fig. 6 is heat exchanger tube and tube sheet sealed structural representation;
The description of symbols of critical piece among Fig. 6: 9, sealing graphite annulus;
Fig. 7 is cylindrical shell and tube sheet sealed structural representation;
The description of symbols of critical piece among Fig. 7: 14, cylindrical shell, 16, pad.
The specific embodiment
Below in conjunction with the specific embodiment the present invention is done further detailed description.
Fig. 2 concentrates the annexation sketch map of multistep treatment device for spent acid.With reference to shown in Figure 2; Spent acid concentrates the multistep treatment device, comprises that preheater, I are imitated evaporation heater, I is imitated between vapor seperator, II effect evaporation heater, II effect vapor seperator, cooler, crystallizer, separator, III effect evaporation heater, vapor seperator, each parts and connected successively with pipeline.
And imitate at I that evaporation heater is imitated between the vapor seperator with I, II imitates the cycling that is provided with circulating pump realization material between evaporation heater and the II effect vapor seperator; Connect circulating pump on the cooler, cooler, enhanced cooling are passed through in the acid that makes II imitate separator output repeatedly; Separator and III are imitated between the evaporation heater, I is imitated vapor seperator and imitated between the evaporation heater with II and circulating pump is set, the quick conveying of realization material.
I is imitated evaporation heater and is heated by saturated vapor, and condensed water is delivered to preheater, as the preheater thermal source.Preheater is a piece cellular type graphite heat exchanger, and the diluted acid temperature of entering is elevated to more than 70 ℃.I is imitated the indirect steam input II effect evaporation heater that vapor seperator is discharged; For II is imitated the evaporation heater heat supply; Condensed water is done wastewater treatment after discharging; The indirect steam that II effect vapor seperator and vapor seperator are discharged is done wastewater treatment after the water quench of spray condenser, III is imitated evaporation heater by Steam Heating, and condensed water is recycled.
Fig. 3 is that I, II are imitated the evaporation heater structural representation, and Fig. 4 is the vertical view of Fig. 3, and with reference to Fig. 3, shown in 4, it is falling liquid film graphite tubulation evaporation heater that I, II are imitated evaporation heater, is single replace tubes formula graphite heat exchanger, and evaporation intensity is high, can reach 50-80kg/m
2.h, heat exchange area reduces more than 30% than common heat exchanger, and solid circulating rate reduces more than 70%.
Fig. 5 is the structural representation of falling liquid film part; With reference to shown in Figure 5; Need by the spent acid that concentrates after the sour import E input at falling liquid film graphite tubulation evaporation heater top, to distribute, get into the graphite heat exchanger tube 10 from graphite liquid-dividing head 6 through cloth ground floor cloth liquid dish 3, second layer cloth liquid dish 4; Get into separator with acid and steam behind the state process graphite heat exchanger tube of film forming; Wherein F gets into the steam of graphite heat exchanger from the steam inlet, exports from condensate outlet behind the baffling repeatedly through deflection plate M in the shell side, and this condensate liquid can be used as the heating thermal source of other equipment.
With reference to Fig. 6, shown in 7, graphite heat exchanger tube 10 adopt graphite products resin dedicated-phenol-formaldehyde resin modified evenly mixes with graphite powder and passes through high pressure (500 tons of pressure) tube extruding machine extruding pipe, passes through high temperature (200-800 ℃) carbonization treatment again.
Housing adopts the carbon steel line with rubber or wards off lead, guarantees its corrosion-resistant and service life.
Fig. 6 is heat exchanger tube and tube sheet sealed structural representation; With reference to shown in Figure 6, graphite heat exchanger tube 10 adopts the sealing of single tube sealing means with tube sheet 11, connects with a cover sealing device; Sealing device comprises O-ring seal 8, sealing graphite annulus 9, sealing nut 7, and O-ring seal adopts the fluorubber material.Fig. 7 is cylindrical shell and tube sheet sealed structural representation, with reference to shown in Figure 7, reaches sealing effectiveness by pad 16 between cylindrical shell 14 and the tube sheet 11.
It is the carbon steel liner graphite-structure of two end ellipse heads that I, II are imitated vapor seperator, has increased the composite impervious barrier between carbon steel and the graphite linings, guarantees the whole Corrosion Protection of equipment.The whole Graphite Machining Piece of external mouth of pipe liner, intensity is high, and the special seal face sealing structure property of design is good.Serviceability temperature 80-180 ℃, working pressure-0.088-0.8MPa.
The structure of graphite cooling cooler is similar basically with heater, but serviceability temperature low-15-80 ℃, working pressure 0.2-0.4MPa.
It is tubular graphitic heat-exchanger that III is imitated graphite heater, is different from I, II is imitated the vapor seperator part and is not to be provided with cloth liquid dish, because acid is imitated concentrating of stage through I, II; Concentration nearly 60%; Be easy in the equipment surface fouling, need not to adopt again the mode of falling liquid film to heat, have accessible unsteady characteristics; Equipment can be worked in the very big scope of the temperature difference, can not cause damage because of expanding with heat and contract with cold of material.Serviceability temperature is up to 220 ℃, 150 ℃ of the temperature difference.
The structure and material of vapor seperator and I, II are imitated the vapor seperator basically identical, but serviceability temperature is higher, and corrosion resistance requires higher.Serviceability temperature 80-220 ℃, working pressure-0.088-0.8MPa.
It is the steel lining fluorine plastics that lining is moulded circulating pump, is big flow low lift circulating pump, and not only corrosion-resistant but also high temperature resistant, power consumption is low.
The fiberglass spray condenser is a kind of spray condensing structure, and there are four layers of tray the inside, and every layer of tray has different apertures, is staggered, and spray is even, and cooling water consumption is few, produces vacuum simultaneously.
Spent acid concentrates multilevel processing technology, comprises the steps:
Spent acid is heated to about 70 ℃ through preheater, and after I was imitated the evaporation heater heating, the acid of heating and steam were after I is imitated separator separates; The part of liquid-state material is returned I effect evaporation heater through circulating pump, and another part input II is imitated evaporation heater, after heating and II effect separator separates; A part is returned II effect evaporation heater through circulating pump; Another part cools off through cooler, and filter residue is recycled after crystallizer crystallization, the separator separates, and filtrating input III is imitated the concentrated acid that evaporation heater heats, vapor seperator separates back simmer down to 65%; III effect evaporation heater utilizes steam as thermal source, and condensed water is recycled.The indirect steam part is as the thermal source of next stage heater, and the condensation of water spray partly is cooled.
Spent acid concentrates multilevel processing technology, specifically is provided with as follows:
20m
3The spent acid of concentration 20% is heated to 70 ℃-80 ℃ through preheater, and input I is imitated evaporation heater, and what carry in the shell side of I effect evaporation heater is the saturated steam heating; The about 120-125 of heating-up temperature ℃; The about 0.25Mpa of pressure, the acid of acquisition and gas-vapor mix are after I is imitated separator separates, and indirect steam input II is imitated evaporation heater; Spent acid is concentrated into 25% spent acid; Temperature is 98-99 ℃, and the part of this spent acid is returned I through circulating pump and imitated evaporation heater, and wherein the circulating pump circulation is conveyed into inventory that II imitates evaporation heater and replenishes the amount that gets into I effect evaporation heater and equate basically; To keep I to imitate the evaporation heater material balance, the spent acid input II of another is imitated and is continued heating and separating in the evaporation heater;
Imitating the evaporation heater shell side at II is that II is imitated the secondary steam that contains acid that separator is discharged, about 86 ℃ of temperature, the about 0.1Mpa of pressure; Spent acid is after II is imitated separator separates; Indirect steam is done wastewater treatment after the water quench of spray condenser, spent acid is that concentration is about 33%, the about 68-69 of temperature ℃, and this spent acid part is imitated evaporation heater circulation heating through circulating pump input II; Another part is delivered to the phase III
In the phase III, the shell side of cooler is a chilled water, and temperature is-6 ℃ to-10 ℃; Material inputs in the crystallizer after circulating pump circulation cooling, and material is at the crystallizer intercrystalline; Filter residue (main component is a ferrous sulfate) is discharged recovery after separator separates again, and filtrating is 0.3 ℃-0 ℃ of temperature, the sulfuric acid of simmer down to 40%; This filtrating is through the next stage of circulating pump input, that is:
Simmer down to concentration is 65% after III is imitated evaporation heater, vapor seperator, temperature is 99.5 ℃ the concentrated sulfuric acid, and the shell side that III is imitated evaporation heater is saturated steam, and operating temperature is 151 ℃, and pressure is 0.4Mpa, and condensed water is recycled.Material obtains about 10m after evaporation separates
3Temperature is 99.5-100.5 ℃, and concentration is 65% concentrated acid, and steam is done wastewater treatment after the spray condenser cooling.
The application cycle pump is back to evaporation heater with partial material, and another part material gets into the explanation in next stage, and the material in evaporation heater reaches internal circulating load (about 150m
3) before, material reaches after the internal circulating load through the circulating pump heating that in evaporation heater, circulates, partial material can get into the next stage.The working condition of the circulating pump that connects on the cooler is identical therewith, and the material in cooler reaches before the internal circulating load, and circulating pump passes through cooler with material repeatedly.
The technical characteristic that I, II, III are imitated operation stage, cooler is shown in table 1, table 2, table 3, table 4.
Table 1 is the list of technical characteristics that I is imitated the stage:
Table 2 is lists of technical characteristics that II is imitated:
Table 3 be cooler list of technical characteristics:
Table 4 is lists of technical characteristics that III is imitated:
The above-mentioned specific embodiment does not limit technical scheme of the present invention in any form, and the technical scheme that mode obtained that every employing is equal to replacement or equivalent transformation all drops on protection scope of the present invention.
Claims (3)
1. spent acid concentrates the multistep treatment method, it is characterized in that comprising the steps:
Ilmenite prepares the acid of titanium white by product sulfur waste through after the heating of I effect evaporation heater, after the I effect separator separates; The part of liquid-state material is returned I effect evaporation heater through circulating pump; Another part input II is imitated evaporation heater; After II was imitated evaporation heater and II effect separator separates, a part was returned II effect evaporation heater through circulating pump, and another part cools off through cooler; Filter residue is recycled after crystallizer crystallization, the separator separates, and filtrating input III is imitated the evaporation heater heating, vapor seperator separates the back and discharges concentrated acid;
I is imitated evaporation heater and is made thermal source with saturated vapor, and condensed water is recycled, as the thermal source of preheater;
II is imitated vapor seperator and after the water quench of spray condenser, is done wastewater treatment with the indirect steam that the evaporation separation chamber discharges;
III is imitated evaporation heater and is utilized steam as thermal source, and condensed water is recycled;
Described I is imitated, II effect evaporation heater is a falling liquid film graphite tubulation evaporation heater; It is tubular graphitic heat-exchanger that III is imitated evaporation heater.
2. spent acid according to claim 1 concentrates the multistep treatment method, it is characterized in that the spent acid amount in the evaporation heater reaches before the internal circulating load, and material only circulates in evaporation heater and vapor seperator through circulating pump.
3. spent acid according to claim 1 concentrates the multistep treatment method, it is characterized in that getting into I at spent acid imitates evaporation heater before through the preheater preheating, and the thermal source of preheater is the condensed water that I is imitated evaporation heater.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2010102665069A CN101935077B (en) | 2010-08-27 | 2010-08-27 | Waste acid concentration multistage treatment method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2010102665069A CN101935077B (en) | 2010-08-27 | 2010-08-27 | Waste acid concentration multistage treatment method |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN101935077A CN101935077A (en) | 2011-01-05 |
| CN101935077B true CN101935077B (en) | 2012-06-20 |
Family
ID=43388685
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2010102665069A Active CN101935077B (en) | 2010-08-27 | 2010-08-27 | Waste acid concentration multistage treatment method |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN101935077B (en) |
Families Citing this family (20)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102730650B (en) * | 2011-04-12 | 2014-08-20 | 安徽理工大学 | Recovery technology of titanium white waste acid |
| CN102249203A (en) * | 2011-04-29 | 2011-11-23 | 南通京通石墨设备有限公司 | Phosphoric acid evaporation process and device thereof |
| JP5572198B2 (en) * | 2011-10-31 | 2014-08-13 | セメス株式会社 | Substrate processing apparatus and chemical solution recycling method |
| CN102633238B (en) * | 2012-04-12 | 2014-09-24 | 中国科学院过程工程研究所 | Process method of concentrating and purifying dilute sulphuric acid |
| CN102774816B (en) * | 2012-08-02 | 2013-12-25 | 潜江方圆钛白有限公司 | Method and device for concentrating waste acid in titanium dioxide production by sulfuric acid process |
| CN102887487A (en) * | 2012-09-27 | 2013-01-23 | 攀枝花学院 | Method for concentrating titanium dioxide waste acid by utilizing solar energy |
| CN103935966B (en) * | 2014-04-09 | 2016-04-20 | 南通职业大学 | A kind of recovery processing technique of electrode foil corrosion Waste Sulfuric Acid |
| CN104445777A (en) * | 2014-11-27 | 2015-03-25 | 大柴旦吉利化工有限公司 | Multi-effect evaporative condensed water recycling method |
| CN104555948B (en) * | 2014-12-28 | 2017-07-14 | 贵州兰鑫石墨机电设备制造有限公司 | A kind of waste acid concentration technique |
| SE539233C2 (en) * | 2015-11-02 | 2017-05-23 | Pharmalundensis Ab | Method and apparatus to reduce waste production in an isolation process |
| CN105399168B (en) * | 2015-12-18 | 2018-01-02 | 许达人 | The Multi-effect evaporation compression apparatus and technique of sulfur acid and its salting liquid |
| CN106178564B (en) * | 2016-07-22 | 2019-04-05 | 钮德明 | A kind of titanium white waste acid external circulating multi-effect evaporator |
| CN106477531B (en) * | 2016-12-01 | 2018-08-21 | 上海佳麟泵阀有限公司 | Prevent from generating the Waste Sulfuric Acid concentrating recovery device of electrochemical corrosion when operation |
| CN108726614A (en) * | 2018-05-31 | 2018-11-02 | 平原中德泰兴环保科技装备有限公司 | A kind of industrial waste treatment process and its device |
| CN110697660B (en) * | 2019-10-31 | 2021-10-08 | 龙佰襄阳钛业有限公司 | Double-effect concentration and recycling method for waste acid in titanium dioxide production enterprises |
| CN111265903A (en) * | 2020-03-30 | 2020-06-12 | 龙岩卓越新能源股份有限公司 | Biodiesel byproduct crude glycerine continuous dealcoholization device |
| CN111517397A (en) * | 2020-06-01 | 2020-08-11 | 江苏泰特联合环保科技有限公司 | Titanium white waste sulfuric acid three-stage type negative pressure evaporation crystallization treatment process and device |
| CN113003545A (en) * | 2021-02-23 | 2021-06-22 | 佛山市景嘉机电设备有限公司 | Method for recycling and treating iron-containing mixed acid waste liquid in steel industry |
| CN113350812A (en) * | 2021-07-08 | 2021-09-07 | 攀钢集团研究院有限公司 | Method and device for concentrating waste acid |
| CN114534285A (en) * | 2022-03-01 | 2022-05-27 | 青岛康景辉环境科技集团有限公司 | Process for treating sucrose fermentation broth by evaporator |
Family Cites Families (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE3632623A1 (en) * | 1986-09-25 | 1988-03-31 | Bayer Ag | METHOD FOR CONCENTRATING SULFURIC ACID |
| JPH0722641B2 (en) * | 1986-10-21 | 1995-03-15 | 日鉄化工機株式会社 | Method for concentrating hygroscopic compound aqueous solution |
| CN101070143B (en) * | 2007-06-11 | 2010-07-14 | 浙江闰土股份有限公司 | Apparatus system for multi-effect concentration utilization of low-concentration waste sulfuric acid |
| CN101475147A (en) * | 2009-01-23 | 2009-07-08 | 陈培豪 | Dilute sulphuric acid concentration method and system |
-
2010
- 2010-08-27 CN CN2010102665069A patent/CN101935077B/en active Active
Also Published As
| Publication number | Publication date |
|---|---|
| CN101935077A (en) | 2011-01-05 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101935077B (en) | Waste acid concentration multistage treatment method | |
| CN203428934U (en) | Concentrating and crystallizing system of copper sulfate solution | |
| WO2006094437A1 (en) | A method and an multi-effect evaporation for waste water of alkylene oxides | |
| CN103127736A (en) | Evaporation and concentration device utilizing heat pump technique | |
| CN202625969U (en) | High-salinity organic wastewater treatment device | |
| CN206304378U (en) | The energy-conservation MVR evaporators that a kind of vapor recompression is utilized | |
| CN102249203A (en) | Phosphoric acid evaporation process and device thereof | |
| CN104788577B (en) | Method for recycling secondary steam generated in corn starch wet milling production process | |
| CN107899261A (en) | Standardize low-temperature evaporation equipment | |
| CN205084431U (en) | Multiple -effect falling film evaporation ware | |
| CN113307433A (en) | Four-effect cross-flow pharmaceutical wastewater evaporative crystallization system with external heat exchanger | |
| CN108905257A (en) | A kind of waste-heat recovery device of product equipment for purifying | |
| CN105692742B (en) | Horizontal tube falling film evaporation high-salt wastewater depth enrichment facility | |
| CN204999762U (en) | Concentrated crystallization equipment of carnallite waste water | |
| CN217961331U (en) | Novel negative pressure MVR evaporation equipment | |
| CN106924985A (en) | Condensing source heat pump drives multi-effect distilling technique | |
| CN113842852B (en) | Process and system for annual production of 20 ten thousand tons of methylamine | |
| CN103991874A (en) | Method and system for purifying trichlorosilane from chlorosilane | |
| CN205386347U (en) | High strong brine of reuse of reclaimed water divides matter crystallization integrated equipment | |
| CN204824207U (en) | Sodium sulphate solution evaporation crystallization equipment | |
| CN106277115B (en) | A kind of saline sewage crystallizing evaporator, purification system and purification process | |
| CN208943475U (en) | Recycle sulfuric acid concentration evaporator in graphite system | |
| CN106809896A (en) | A kind of organic wastewater treating system and method | |
| CN203899171U (en) | Novel waste heat/live steam compound evaporator | |
| CN209809543U (en) | Seven-effect tube type falling film evaporator set |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant |