CN203807618U - Device for acid bath low-temperature evaporation and continuous crystallization of viscose - Google Patents
Device for acid bath low-temperature evaporation and continuous crystallization of viscose Download PDFInfo
- Publication number
- CN203807618U CN203807618U CN201420216836.0U CN201420216836U CN203807618U CN 203807618 U CN203807618 U CN 203807618U CN 201420216836 U CN201420216836 U CN 201420216836U CN 203807618 U CN203807618 U CN 203807618U
- Authority
- CN
- China
- Prior art keywords
- heat exchanger
- acid bath
- output
- connects
- evaporation
- 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.)
- Withdrawn - After Issue
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
- Y02P70/00—Climate change mitigation technologies in the production process for final industrial or consumer products
- Y02P70/50—Manufacturing or production processes characterised by the final manufactured product
- Y02P70/62—Manufacturing or production processes characterised by the final manufactured product related technologies for production or treatment of textile or flexible materials or products thereof, including footwear
Landscapes
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Abstract
The utility model discloses a device for acid bath low-temperature evaporation and continuous crystallization of viscose, which comprises an acid bath intermediate barrel for evaporation and crystallization, wherein the output of the acid bath intermediate barrel is connected with a steam preheater through a feed pump and a condensate water preheater; the output of the steam preheater is connected with an evaporation crystallizer and a heat exchanger B through a heat exchanger A; the evaporation crystallizer is connected in series with the heat exchanger B; the output of the evaporation crystallizer is connected with a crystal slurry tank through a discharge pump; the output of the crystal slurry tank is connected with a separator; the output of the separator is connected with a mother liquid tank. The energy is greatly saved, the evaporation and crystallization are integrated, and stable evaporation and continuous crystallization are realized; meanwhile, the whole set of equipment is compact and reliable, the investment in civil engineering is saved, the floor area is small, a few operators are needed, the operation is more stable and reliable, and the whole system can be made into configuration control to realize high automation.
Description
Technical field
The utility model relates to the device of a kind of viscose acid bath low-temperature evaporation and continuous crystallisation.
Background technology
Viscose is regenerated celulose fibre, it take native cellulose as raw material, after series of physical chemical process is processed, spin and form, viscose is similar to natural cotton fiber, there is good hygroscopicity, gas permeability, dyeability, antistatic, comfortable and easy to wear, be that synthetic fiber cannot be compared, its textiles is subject to liking of consumers in general deeply, has stronger competitiveness on market.Viscose is since suitability for industrialized production, and along with the development of viscose technology and green technology, perfect, viscose output constantly increased with more than 10% speedup in recent years, and domestic viscose production capacity is over 3,500,000 tons so far.
The production of viscose, be first through soaking, make qualified viscose glue after the operation such as squeezing, pulverizing, experienced, yellow, dissolving, filtration, deaeration at stoste workshop raw material pulp, viscose glue is solidification forming in acid bath, and after the drawing-off of spinning machine and scouring machine post processing, drying machine drying, viscose is made in packing.Acid station is to spinning machine, continuously to supply with a certain amount of department that meets technological requirement specially, coagulating bath or spinning bath are named again in acid bath, acid bath is the solution with sulfuric acid, sodium sulphate, zinc sulfate preparation, the main task at acid station is formed constant acid bath, continuously flow at a certain temperature spinning machine, to guarantee that spinning is produced normally, move, whether the composition of acid bath and temperature stabilization and transparency have very important impact to viscose quality.In fibre forming process, to generate a certain amount of water and sodium sulphate, being back to sulfuric acid concentration in sour body lotion of standing reduces, must the moisture evaporation in backflow acid bath is a part of, in acid bath after evaporation, sodium sulfate concentration raises, sulfate crystal in acid bath should be separated out to a part, therefore, the evaporation of acid bath and crystallization are the vital tasks at acid station.
Continuous expansion along with viscose production capacity, the technology of viscose and equipment equipment are also in continuous progress, as the production capacity of viscose staple fibre production line single line is increased to 50,000 tons/year even 100,000 tons/year by 0.5 ten thousand tons/year, acid station acid bath evaporation mode also even 14 is imitated evaporation by single effect evaporation to 11 effects, evaporability also increases to 25 tons/hour by singly overlapping 10 tons/hour, evaporation efficiency improves greatly, and evaporation liquid to steam ratio reaches 1:0.27 ~ 0.33.
Viscose industry generally adopts efficient 11 effect flash distillation plant and continuous crystallizing systems at present.Evaporating principle: body lotion is injected into vaporific under vacuum state, utilizes self liberated heat through decompression cooling, and the part moisture content in body lotion is evaporated, thereby reaches concentrated body lotion and energy-conservation object.Technological process: filter qualified body lotion and enter the flash liberation of horizontal-type evaporator V10 section after flowmeter metering, enter again V11 section and continue degassed evaporation, then by circulating pump, be delivered to A8～A1 preheating, finally by entering V1V2 after A0 and H heating, spray flash distillation, entering V3～V9 further evaporates again, obtain qualified concentrated body lotion, through liquid bath, overflow back acid bath mixing channel.The steam producing in V1V2 and V3～V8, for pre-heater A1～A8, carries out preheating to the body lotion passing through, and meanwhile, self is condensed into condensed water and gets rid of; The thermal source of A0 and H is fresh saturated vapor; The evaporation vapour producing in evaporimeter V9～V11 is inhaled in mixing condenser MK1, MK2, and this cooling water of cooling water-cooled can be recycled after treatment.The exhaust of this device is through steam jet pump, to enter the second condenser HK respectively by each blast pipe, the water condensation that is cooled, more further by water ring vacuum pump suction, through blast pipe, enter atmosphere or remove emission-control equipment.The advantage of 11 effect flash distillations: because body lotion is not the outer thermal source heating coming when the explosive evaporation, but the damp and hot heat required while supplying with evaporation that utilizes self, and the process of flash heating is carried out step by step respectively in the vaporization chamber of series connection at different levels, cascade raising temperature, make full use of temperature difference, maximally utilise heat, thereby save heat energy.Weak point: (1) acid bath is through 11 effect vaporising devices, the evaporated vapor that moisture produces in evaporimeter V9～V11 is inhaled into and is condensed into water after mixing condenser MK1, MK2 and discharges, and still has certain heat energy not to be fully utilized in evaporated vapor;
(2) evaporated vapor is condensed into water also needs a large amount of cooling waters, need to consume a large amount of power; (3) vacuum is had relatively high expectations, generally want Water-ring vacuum to add steam-jet vacuum pump and just can reach requirement;
(4) package unit tank body is many, and volume is larger, and pipeline is complicated, and floor space is larger;
(5) due to the overboard problem of condensation that will overcome vacuum and bring, overcome acceleration of gravity, package unit is installed should be higher than drain gully 9.8M, and the building cost of device is higher;
(6) pipeline is complicated, and it is many that valve etc. are controlled node, and maintenance load is larger.
Utility model content
Its object of the utility model is just to provide the device of a kind of viscose acid bath low-temperature evaporation and continuous crystallisation, greatly saved the energy, and evaporation and crystallization are integrated, realized steady-state evaporation and continuous crystallisation, outfit is compact reliable simultaneously, saves construction investment, floor space is little, operating personnel are few, operate more reliable and more stablely, total system can be made configuration and control, increasingly automated.
The technical scheme that realizes above-mentioned purpose and take, the middle bucket of acid bath that comprises crystallization to be evaporated, in the middle of acid bath, bucket output connects steam pre-heater through feeding engine, condensed water preheater, described steam pre-heater output connects crystallizing evaporator and B heat exchanger through A heat exchanger, crystallizing evaporator and B heat exchanger are for being connected in series, crystallizing evaporator output connects magma tank through discharging pump, and the output of magma tank connects seperator, and seperator output connects mother liquor tank; Described crystallizing evaporator vacuum port connects vavuum pump through vacuum cooler, crystallizing evaporator steam (vapor) outlet connects the steam inlet of A heat exchanger and B heat exchanger through vapour compression machine, A heat exchanger is connected condensate pump with the condensation-water drain of B heat exchanger through condensate water pot, and condensate pump output connects condensed water preheater; Between described A heat exchanger input and B heat exchanger output, be connected in series circulating pump.
Compared with prior art the utlity model has following advantage.
This device can utilize steam completely, does not lose steam thermal energy, and removal apparatus starts to be needed outside a small amount of nascent steam, is in operation without supplementing nascent steam again; Evaporating temperature is low to moderate 50 ~ 60 ℃, and evaporation efficiency is 30 times of tradition evaporation; Do not need cooling water, therefore greatly saved energy consumption, evaporating one ton of water only needs power consumption 50KWH.The 11 effect flash evaporation technologies that Yu Xian viscose glue factory is generally used are compared, and have greatly saved the energy; And evaporation and crystallization can be integrated, realize steady-state evaporation and continuous crystallisation, outfit is compact reliable simultaneously, saves construction investment.Floor space is little, operating personnel are few; Supporting public work project is few; Operate more reliable and more stablely, total system can be made configuration and control, increasingly automated.
Accompanying drawing explanation
Below in conjunction with accompanying drawing, the utility model is described in further detail.
Fig. 1 is this apparatus structure principle schematic.
The specific embodiment
The middle bucket 1 of acid bath that comprises crystallization to be evaporated, in the middle of acid bath, bucket 1 output connects steam pre-heater 20 through feeding engine 2, condensed water preheater 3, as shown in Figure 1, described steam pre-heater 20 outputs connect crystallizing evaporator 11 and B heat exchanger 5 through A heat exchanger 6, crystallizing evaporator 11 and B heat exchanger 5 are for being connected in series, crystallizing evaporator 11 outputs connect magma tank 17 through discharging pump 16, and 17 outputs of magma tank connect seperator 18, and seperator 18 outputs connect mother liquor tank; Described crystallizing evaporator 11 vacuum port a connect vavuum pump 15 through vacuum cooler 14, crystallizing evaporator 11 steam (vapor) outlet b connect the steam inlet c of A heat exchanger 6 and B heat exchanger 5 through vapour compression machine 12, the condensation-water drain d of A heat exchanger 6 and B heat exchanger 5 is connected condensate pump 9 through condensate water pot 8, and condensate pump 9 outputs connect condensed water preheater 3; Between described A heat exchanger 6 inputs and B heat exchanger 5 outputs, be connected in series circulating pump 7.
Described condensate pump 9 outputs connect vapour compression machine 12 through spray pump 10, spray cooler 13.
Between described seperator 18 outputs and mother liquor tank, be provided with overflow launder 19, described magma tank overfall e connects overflow launder 19.
The pipeline rake ratio that described discharging pump 16 connects magma tank 17 is 10%.
Operation principle
This device comprises evaporation and two processes of crystallization, as shown in Figure 1, its path is the middle bucket---feeding engine---pre-heater---heat exchanger A---evaporimeter---vapour compression machine---A heat exchanger of acid bath---acid bath, B heat exchanger---discharging pump---magma tank---centrifuge to be evaporated.
Feeding engine 2 is sent the acid solution of crystallization to be evaporated in bucket 1 in the middle of acid bath into A heat exchanger 6 after steam pre-heater 20, and enter crystallizing evaporator 11, under vacuum state, acid bath is evaporated with low boiling, the steam of evaporation enters the steam-water mixing body that vapour compression machine 12 is compressed into high enthalpy, steam-water mixing body enters A heat exchanger 6, B heat exchanger 5, chuck by heat exchanger heats acid bath, acid bath is heated and evaporates between A heat exchanger 6---crystallizing evaporator 11---B heat exchanger 5 through circulating pump 7, the steam evaporating enters vapour compression machine 12 compressions again, steam-water mixing body after compression condenses into water and is collected into condensate water pot 8 in heat exchanger chuck, now condensed water still has uniform temperature, with pump, condensed water being delivered to 3 pairs of acid bath liquid to be evaporated of condensed water preheater preheats, the interior part acid bath liquid after evaporation of crystallizing evaporator 11 is gone out to magma tank 17 by discharging pump 16, through seperator 18, isolates saltcake and mother liquor, and mother liquor is for preparing new spinning acid bath, and saltcake is further produced glauber salt, evaporate so continuously and crystallization.
Claims (4)
1. the device of a viscose acid bath low-temperature evaporation and continuous crystallisation, the middle bucket of acid bath (1) that comprises crystallization to be evaporated, in the middle of acid bath, bucket (1) output is through feeding engine (2), condensed water preheater (3) connects steam pre-heater (20), it is characterized in that, described steam pre-heater (20) output connects crystallizing evaporator (11) and B heat exchanger (5) through A heat exchanger (6), crystallizing evaporator (11) and B heat exchanger (5) are for being connected in series, crystallizing evaporator (11) output connects magma tank (17) through discharging pump (16), magma tank (17) output connects seperator (18), seperator (18) output connects mother liquor tank, described crystallizing evaporator (11) vacuum port (a) connects vavuum pump (15) through vacuum cooler (14), crystallizing evaporator (11) steam (vapor) outlet (b) connects the steam inlet (c) of A heat exchanger (6) and B heat exchanger (5) through vapour compression machine (12), the condensation-water drain (d) of A heat exchanger (6) and B heat exchanger (5) is connected condensate pump (9) through condensate water pot (8), and condensate pump (9) output connects condensed water preheater (3), between described A heat exchanger (6) input and B heat exchanger (5) output, be connected in series circulating pump (7).
2. the device of a kind of viscose acid bath low-temperature evaporation according to claim 1 and continuous crystallisation, is characterized in that, described condensate pump (9) output connects vapour compression machine (12) through spray pump (10), spray cooler (13).
3. the device of a kind of viscose acid bath low-temperature evaporation according to claim 1 and continuous crystallisation, it is characterized in that, between described seperator (18) output and mother liquor tank, be provided with overflow launder (19), described magma tank overfall (e) connects overflow launder (19).
4. the device of a kind of viscose acid bath low-temperature evaporation according to claim 1 and continuous crystallisation, is characterized in that, the pipeline rake ratio that described discharging pump (16) connects magma tank (17) is 10%.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201420216836.0U CN203807618U (en) | 2014-04-30 | 2014-04-30 | Device for acid bath low-temperature evaporation and continuous crystallization of viscose |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201420216836.0U CN203807618U (en) | 2014-04-30 | 2014-04-30 | Device for acid bath low-temperature evaporation and continuous crystallization of viscose |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN203807618U true CN203807618U (en) | 2014-09-03 |
Family
ID=51446401
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201420216836.0U Withdrawn - After Issue CN203807618U (en) | 2014-04-30 | 2014-04-30 | Device for acid bath low-temperature evaporation and continuous crystallization of viscose |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN203807618U (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103952798A (en) * | 2014-04-30 | 2014-07-30 | 九江恒生化纤有限公司 | Glue fiber acid bath low temperature evaporation and continuous crystallization process and device thereof |
-
2014
- 2014-04-30 CN CN201420216836.0U patent/CN203807618U/en not_active Withdrawn - After Issue
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103952798A (en) * | 2014-04-30 | 2014-07-30 | 九江恒生化纤有限公司 | Glue fiber acid bath low temperature evaporation and continuous crystallization process and device thereof |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN103952798B (en) | Glue fiber acid bath low temperature evaporation and continuous crystallization process and device thereof | |
| CN106669207A (en) | MVR (mechanical vapor recompression) evaporation crystallization system and method for high-salinity wastewater | |
| CN204952342U (en) | Concentrated crystal system of carnallite solution | |
| CN204588905U (en) | Ammonia type flue gas desulfurizing waste water evaporated crystallization device | |
| CN106390496A (en) | Energy-saving evaporation equipment of mixed salt solution and control method of equipment | |
| CN206103380U (en) | Energy -conserving evaporation equipment of mixed salt solution | |
| CN103510166B (en) | Koplon coagulating bath process streamline | |
| CN206508573U (en) | A kind of function of mechanical steam recompression evaporation and crystallization system of high-salt wastewater | |
| CN105536277B (en) | A kind of evaporating and concentrating process and device of the cellulose solvent NMMO aqueous solution | |
| CN204824506U (en) | Special processing apparatus of sulfur acid sodium waste water in plumbous recovery production | |
| CN106422399A (en) | Energy-efficient evaporative concentration and crystallization system for salt solution and control method of system | |
| CN106310704A (en) | Continuous single-effect vacuum evaporation crystallization system as well as application and technology | |
| CN207002498U (en) | A kind of vanadium wastewater Zero discharging system | |
| CN109809437A (en) | Novel energy-saving environment-friendly heavy soda ash production technology and system | |
| CN107670323A (en) | Sulphur ammonium crystallization recovery energy saving technique and device in acrylonitrile process | |
| CN106422385A (en) | Energy-saving vaporization system for calcium nitrate solution and control method thereof | |
| CN112516619B (en) | Forced circulation evaporation device and method for slurry with crystals | |
| CN203807618U (en) | Device for acid bath low-temperature evaporation and continuous crystallization of viscose | |
| CN105833705A (en) | Saturated-reactor-process ammonia waste gas treatment device and process thereof | |
| CN208182650U (en) | Ammonium sulphate waste liquor desalting processing equipment | |
| CN216513307U (en) | Ferric phosphate effluent disposal system | |
| CN104528770A (en) | Mirabilite dehydration method based on gas-liquid direct heat exchange | |
| CN205760549U (en) | Saturator method ammonia emission-control equipment | |
| CN104724776A (en) | Device and method for mixing secondary steam into pressurized water in pressurized evaporation | |
| CN213790052U (en) | High salt water concentration and crystallization system |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| AV01 | Patent right actively abandoned |
Granted publication date: 20140903 Effective date of abandoning: 20150211 |
|
| RGAV | Abandon patent right to avoid regrant |