CN107686204A - A kind of method of heat integration during processing viscose rayon acid waste water - Google Patents
A kind of method of heat integration during processing viscose rayon acid waste water Download PDFInfo
- Publication number
- CN107686204A CN107686204A CN201710892626.1A CN201710892626A CN107686204A CN 107686204 A CN107686204 A CN 107686204A CN 201710892626 A CN201710892626 A CN 201710892626A CN 107686204 A CN107686204 A CN 107686204A
- Authority
- CN
- China
- Prior art keywords
- waste water
- acid waste
- acid
- viscose rayon
- cooling
- 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.)
- Granted
Links
Classifications
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
Landscapes
- Life Sciences & Earth Sciences (AREA)
- Hydrology & Water Resources (AREA)
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Separation Using Semi-Permeable Membranes (AREA)
Abstract
The present invention relates to a kind of method of the heat integration during processing viscose rayon acid waste water, comprise the following steps：Acid waste water is cooled into membrane filtration concentration systems to carry out handling required temperature；Acid waste water after cooling carries out filtering and concentrating using membrane filtration concentration systems, obtains acid waste water concentrate；The acid waste water concentrate is further concentrated by evaporation after preheating into vapo(u)rization system；Wherein, acid waste water concentrate Cooling and Heat Source each other in acid waste water and step (3) in step (1), carries out heat exchange, while realize the cooling of acid waste water and the preheating of acid waste water concentrate.The present invention sufficiently realizes the comprehensive utilization of heat energy in viscose rayon high-temperature acidic wastewater treatment process, reduces energy consumption and the cost of operation.
Description
Technical field
The present invention relates to a kind of method of the heat integration during processing viscose rayon acid waste water, belong to viscose glue
The process field of fiber production field, especially viscose rayon acid waste water.
Background technology
Viscose rayon factory spins the acid waste water discharged between practice and contains sulfuric acid, sodium sulphate, zinc sulfate, present processing side
Formula is：Acid waste water is uniformly processed after being emitted into sewage treatment plant and the mixing of other sewage, and the outer row of a large amount of brine wastes is not only
The Biochemical Treatment of follow-up waste water is influenceed, also wastes the energy.Research changes acid water treatment technology, reclaims the sulphur in acid water
Acid, sodium sulphate and zinc sulfate, acid and salt content in outer draining can be not only reduced, reduces biochemical treatment difficulty, is reduced at sewage
Cost is managed, more meets the development trend of environmental protection and energy saving and cost lowering.With industry competition and increasingly strict, the viscose glue enterprise of environmental protection policy
Industry starts to pay attention to the Treatment for Reuse of acid waste water.There is now viscose glue enterprise using evaporation by the way of acid waste water is concentrated
There is the shortcomings that investment is big, and operating cost is high in reuse, vapo(u)rization system, cost high energy consumption turns into greatly acid water concentration reuse technology hair
The maximum restriction of exhibition.At present, membrane filtration concentration technique is low with its energy consumption, is obtained in processing brine waste field the advantages of efficiency high
Extensive use, but this technology is not suitable for processing and contains highly concentrated salt waste water.Meanwhile film filter requires that the temperature of filter medium will drop
To less than 40 DEG C, and the medium temperature for entering vapo(u)rization system is higher, and system energy consumption is lower.
The content of the invention
The technical problems to be solved by the invention be to provide it is a kind of handle viscose rayon acid waste water during heat energy it is comprehensive
The method utilized is closed, feasible process is stable effective, fully can effectively utilize the heat energy of high-temperature acidic waste water, reduce and utilize evaporation
The steam consumption of system treatment of acidic wastewater.The production technology that the present invention is combined using membrane filtration and evaporation is carried out to acid water
Concentration, the technical advantage of membrane filtration and evaporation to the processing of high-concentration and low-concentration acid waste water is given full play to, equipment throwing can be saved
Money and operating cost, improve operational efficiency.And the present invention is comprehensive to high-temperature acidic waste water membrane filtration and the progress of the heat energy of evaporation process
Close and utilize, make full use of high-temperature acidic waste water heat energy, save system entirety energy consumption.
The technical scheme that the present invention solves above-mentioned technical problem is as follows：During a kind of processing viscose rayon acid waste water
The method of heat integration, comprises the following steps：
(1) acid waste water is cooled into membrane filtration concentration systems to carry out handling required temperature；
(2) acid waste water after cooling carries out filtering and concentrating using membrane filtration concentration systems, obtains acid waste water concentrate；
(3) the acid waste water concentrate is further concentrated by evaporation after preheating into vapo(u)rization system；
Wherein, acid waste water concentrate Cooling and Heat Source each other in acid waste water and step (3) in step (1), carries out heat exchange,
Realize the cooling of acid waste water and the preheating of acid waste water concentrate simultaneously.
On the basis of above-mentioned technical proposal, the present invention can also do following improvement.
Further, the viscose rayon acid waste water is the fiber for the entrainment acid bath discharged in production process of viscose fiber
Flushing water, exhaust position is before fibre cutting or after fibre cutting.
The preparation method of viscose rayon generally includes three preparation of viscose glue, spinning moulding, post processing steps, usually by
Cellulosic material extracts pure alpha-cellulose (being referred to as pulp), with caustic soda, carbon disulfide processing, obtains orange-yellow fibre
Plain sodium xanthogenate is tieed up, is re-dissolved in diluted sodium hydroxide solution, turns into sticky spinning solution, referred to as viscose glue.Viscose glue is filtered,
After maturation (about 18~30h being placed at a certain temperature, to reduce the esterification degree of cellulose xanthate ester), deaeration, wet method is carried out
Spinning, coagulating bath (acid bath) are made up of sulfuric acid, sodium sulphate and zinc sulfate.In sodium cellulose xanthate and coagulating bath in viscose glue
Effect of sulfuric acid and decompose, it is cellulose regenerated and separate out, gained cellulose fibre through washing, desulfurization, bleaching, dry after turn into viscose glue
Fiber.The waste water that the present invention is handled is in the production line of viscose rayon plant produced viscose rayon, and wet method is carried out between spinning practice
The Fiber wash water of entrainment acid bath caused by spinning, the waste water is from spinning the fibre of the position that is emitted between practice in wet spinning
Before dimension cut-out or after fibre cutting.
Further, the temperature of the viscose rayon acid waste water is 85-98 DEG C, and each component concentration is sulfuric acid 5-13g/L, sulphur
Sour sodium 15-40g/L, zinc sulfate 0.3-1.1g/L, turbidity 30-50ntu.
Because coagulating bath is made up of sulfuric acid, sodium sulphate and zinc sulfate, its flushing water also contains these materials naturally.And turbidity
Refer to the obstruction degree occurred when suspension passes through to light in water.Suspension in water is usually soil, sand grains, fine
Organic matter and inorganic matter, planktonic organism, microorganism and colloidal substance etc..Content of the turbidity of water not only with suspended material in water has
Close, and it is relevant with their size, shape and refraction coefficient etc..As can be seen here, substantially also contain in viscose rayon acid waste water
There is a certain amount of suspension.
Further, before step (1) cooling, the acid waste water can also be pre-processed：Acid waste water is concentrated
After collection, constant temperature stirring and natural subsidence, suspension in water removal is then filtered off.
More specifically, by viscose rayon acid waste water with centralized collection in collecting tank is pumped into, keep constant temperature stirring pre-
After the time first set, stop stirring, by Action of Gravity Field natural subsidence.
Further, the collecting tank is that carbon steel serves as a contrast high temperature gluing equipment, and carries agitator.
The collecting tank of the present invention can be transformed by resistant to elevated temperatures carbon steel line with rubber storage tank and formed, and its temperature resistant range is in 100-110
DEG C, install agitator additional thereon, and coordinate some existing detecting systems and control system, step of the present invention (1) can be carried out.Tool
Body, agitator is frame or paddle agitator, the rotating speed 50-100rpm of agitator.
Further, the temperature of acid waste water constant temperature stirring is 85-95 DEG C, time 1.5-3h；The time of natural subsidence is
1-2h, the temperature of acid waste water is down to 30-38 DEG C after natural subsidence；Filtering is set using the microfiltration in 0.1um-10um apertures
It is standby.
Microfiltration refers to a kind of technology for separating particle from fluid (gas or liquid), belongs in filtering technique
One kind, it is different with other separation methods and the scope of application, between conventional filtration and ultrafiltration.
The pretreatment of acid waste water comprises the concrete steps that before step (1) of the present invention：Viscose rayon acid waste water is by collection
Middle collect to after with the equipment stirred is stirred, and then by natural subsidence, dissolved gum body material in water and other impurity are analysed
Go out and settle down, the precipitum of precipitation and suspension are filtered off with filter plant and removed.Its principle is：It is molten in acid waste water
Colloidal substance and other impurity can be agglomerated into bulky grain with stirring constantly collision, stop stirring natural subsidence 1-2 hours, formed
Bulky grain colloidal particle can separate out and be deposited on collection pot bottom, then remove the precipitum separated out and suspension by filter plant
Thing, the turbidity of water is down to 8-15ntu.
The present invention removes colloidal substance in viscose rayon acid waste water and other using stirring, sedimentation and by the way of filtering
Suspension, the turbidity of waste water is reduced, improve the operational efficiency being further processed in next step using membrane filtration concentration systems, drop
Low operating cost, extend film service life, shorten the Membrane cleaning time, viscose rayon spent acidic is applied to membrane filtration concentration technique
Water process has promotion and directive significance.
Further, the cooling of acid waste water described in step (1), will by the way of heat exchange cooling and the cooling of vacuum shwoot
Acid waste water is cooled to 30-38 DEG C.
Cooling can specifically select to carry out in pretreatment, after natural subsidence cool, can also select pre-
Processing is cooled again after all terminating.The purpose of cooling makes acid waste water reach by required for membrane filtration concentration systems
Temperature, too high temperature can produce destruction to membrane filtration concentration systems, and be unfavorable for the progress of filtering and concentrating.Further, institute
Heat exchange cooling is stated using heat exchanger, provides low-temperature receiver for heat exchanger is to pass through membrane filtration concentration systems in step (2) to handle
The acid waste water concentrate obtained afterwards, the vacuum shwoot cooling use multi-stage vacuum shwoot, and caused indirect steam is used to walk
Suddenly the vapo(u)rization system of (3).
Further, the heat exchange cooling is using heat exchanger, and provide low-temperature receiver for heat exchanger is to pass through film in step (2)
The acid waste water concentrate obtained after the processing of filtering and concentrating system, the vacuum shwoot cooling use multi-stage vacuum shwoot, produced
Indirect steam be used for step (3) vapo(u)rization system.
When it is implemented, the temperature-fall period of the higher acid waste water of temperature is using heat exchange cooling and true in step 1)
The mode of empty shwoot cooling, will be divided into two parts, Part I high-temperature acidic waste water by pretreated high-temperature acidic waste water
Cooled using multi-stage vacuum shwoot technique, the indirect steam caused by after shwoot uses into vapo(u)rization system, Part II high temperature
Acid waste water heat exchange be using heat exchanger cool, for its low-temperature receiver is provided be membrane filtration concentration systems filtering and concentrating handle after acid
Property Waste water concentrating liquid.And the ratio of the treating capacity of specific two ways can be adjusted according to the needs of actual production and heat exchange
It is whole.So, acid waste water temperature-fall period does not additionally introduce low-temperature receiver, and fully collects heat energy utilization when cooling to vapo(u)rization system.
Further, membrane filtration concentration systems described in step (2) are using ultrafiltration, counter-infiltration or ultrafiltration, electrodialytic film group
Processing mode is closed, or, using ceramic membrane, counter-infiltration or ceramic membrane, electrodialytic film combined treatment mode.
Membrane filtration concentration systems in the present invention can use the membrane filtration condensing mode based on ultrafiltration, i.e., using ultrafiltration
+ counter-infiltration or ultrafiltration+electrodialytic film combined treatment mode, can also use the membrane filtration concentration side based on ceramic membrane
Formula, i.e. ceramic membrane+counter-infiltration or ceramic membrane+electrodialytic film combined treatment mode.
Further, the temperature of the acid waste water concentrate after the processing of membrane filtration concentration systems is 33-38 DEG C；Each component concentration
For sulfuric acid 25-30g/L, sodium sulphate 75-90g/L, zinc sulfate 2-2.5/L.And the filtrate that the processing of membrane filtration concentration systems is isolated
As industrial water reuse to viscose rayon production system.
Further, the preheating of acid waste water concentrate described in step (3) is by the way of heat exchange heats up, the temperature after preheating
Spend for 82-90 DEG C.
Further, the heat exchange heating is using heat exchanger, and provide thermal source for heat exchanger is acidity in step (1)
Waste water.
The initial temperature for the acid waste water concentrate that step (2) obtains is not high, is preferably evaporated in order to subsequently dense
Contracting is, it is necessary to first be preheated, and thermal source used in preheating is the higher acid waste water of temperature in step (1) before, that is to say, that step
Suddenly the higher acid waste water of temperature in (1) acid waste water relatively low with the temperature after the processing of membrane filtration concentration systems here concentrates
Liquid Cooling and Heat Source each other, liquid at two is exchanged heat by heat exchanger, there is provided the comprehensive utilization of heat energy, reduce energy consumption and operation into
This.
Further, the vapo(u)rization system uses multi-effect evaporating device, multistage flash distillation device or MVR evaporators, through pervaporation
Each component concentration is sulfuric acid 115-120g/L, sodium sulphate 345-360g/L, sulfuric acid in the final concentrate obtained after system processing
Zinc 9.5-12g/L.And the acid in final concentrate reuse to the viscose rayon production system obtained after vapo(u)rization system is handled
Step is bathed, condensed water caused by vapo(u)rization system is as industrial water reuse to viscose rayon production system.
Membrane filtration concentration systems are adapted to the acid waste water for handling low concentration, first to pretreated production process of viscose fiber
The Fiber wash water of the entrainment acid bath of middle discharge carries out membrane filtration concentration, preliminary lifting acidity and salinity.And vapo(u)rization system is fitted
The acid waste water of processing high concentration is closed, can further improve acid and salinity in waste water so that the acid waste water after concentration
The acid bath system that can be used in viscose rayon workshop.Caused filtrate and condensed water can also be used as life in two systems
Fisheries water reuse is to viscose rayon production system.
Concentration is carried out to acid waste water using the production technology that membrane filtration concentration systems and vapo(u)rization system are combined, filled
Distribution waves vapo(u)rization system and membrane filtration concentration systems respectively to the technical advantage of high-concentration and low-concentration wastewater treatment, can save equipment throwing
Money and operating cost, improve operational efficiency.The present invention can both reduce outer draining salt content, realize that resources circulation uses, reduce
Cost of sewage disposal and production cost, the benign development to whole viscose rayon industry have promotion and directive significance.
The beneficial effects of the invention are as follows：Low-temperature receiver is not additionally introduced during high-temperature acidic waste water cools, fully balance
High-temperature acidic waste water cools and the heat energy of temperature-rise period, reduces the technical finesse high temperature for being concentrated and being evaporated using membrane filtration and be combined
The energy consumption of acid waste water, the comprehensive utilization of heat energy is sufficiently realized, reduce energy consumption and the cost of operation.
Embodiment
The principles and features of the present invention are described below, and the given examples are served only to explain the present invention, is not intended to limit
Determine the scope of the present invention.
The object that the present invention is directed to is the Fiber wash water that the entrainment acid bath discharged between practice is spun by viscose rayon factory, is discharged
Position is before fibre cutting or after fibre cutting, 85-98 DEG C of water temperature, sulfur acid 5-13g/L, sodium sulphate 15-40g/L, zinc sulfate
0.3-1.1g/L, turbidity 30-50ntu.Acid waste water is cooled into membrane filtration concentration systems to carry out handling required temperature, can
30-38 DEG C is cooled in a manner of using heat exchange cooling and the cooling of vacuum shwoot；Acid waste water after cooling is dense using membrane filtration
Compression system carries out filtering and concentrating, obtains acid waste water concentrate, the temperature of acid waste water concentrate is 33-40 DEG C, and each component is dense
Spend for sulfuric acid 25-30g/L, sodium sulphate 75-90g/L, zinc sulfate 2-2.5g/L；The acid waste water concentrate is heated up using heat exchange
Mode preheated after, be further concentrated by evaporation into vapo(u)rization system, the temperature after preheating be 82-90 DEG C.
The filtrate that the processing of membrane filtration concentration systems is isolated is passed through as industrial water reuse to viscose rayon production system
Acid bath step in final concentrate reuse to the viscose rayon production system obtained after vapo(u)rization system processing, vapo(u)rization system produce
Condensed water as industrial water reuse to viscose rayon production system.
Heat exchange cooling and heat exchange heating are realized by heat exchanger, and the higher acid waste water of temperature is with membrane filtration concentration
The relatively low acid waste water concentrate of temperature after system processing Cooling and Heat Source each other, liquid at two is exchanged heat by heat exchanger；Very
Empty shwoot cooling uses multi-stage vacuum shwoot, and caused indirect steam is used for vapo(u)rization system.
Illustrate above mentioned problem with specific embodiment and comparative example below.
Embodiment 1
By 85 DEG C of temperature, water 200m3/ h acid waste water (after testing, sulfur acid 5g/L, sodium sulphate 15g/L, zinc sulfate
0.3g/L, turbidity 50ntu) turbidity is 10ntu after pretreating process removes colloid and suspension, it is divided into two parts in proportion
Cooling processing is not carried out, and the mode using multi-stage vacuum shwoot for accounting for the high-temperature acidic waste water of total release 75% is cooled to 30
DEG C, indirect steams of the 5.6t caused by vacuum shwoot more than 60 DEG C uses into multi-effect evaporation system, accounts for total release 25%
High-temperature acidic waste water is cooled to 35 DEG C with 33 DEG C of the concentrate that membrane filtration concentration systems are isolated using heat exchanger heat exchange.
Acid waste water after two parts cooling enters membrane filtration concentration systems and is further processed jointly, by film mistake
40m is obtained after filter concentration systems processing3/ h acid waste water concentrate, temperature are 33 DEG C；Each component concentration be sulfuric acid 25g/L,
Sodium sulphate 75g/L, zinc sulfate 2g/L, the 160m that the processing of membrane filtration concentration systems is isolated3/ h filtrates are as industrial water reuse
To viscose rayon production system.
Acid waste water concentrate enters back into vapo(u)rization system after first passing through preheating, and preheating is passed through by the way of heat exchange heats up
High-temperature acidic water reuse heat exchanger with accounting for total release 25%, which exchanges heat, is warming up to 82 DEG C, is obtained after vapo(u)rization system is handled
8.5m3/ h sulfur acid 115g/L, sodium sulphate 345g/L, zinc sulfate 9.5g/L final concentrate reuse to viscose rayon produces
Acid bath step in system, 31.5m caused by vapo(u)rization system3/ h condensed water produces as industrial water reuse to viscose rayon
System.
Embodiment 2
By 85 DEG C of temperature, water 200m3/ h acid waste water (after testing, sulfur acid 5g/L, sodium sulphate 15g/L, zinc sulfate
0.3g/L, turbidity 50ntu) turbidity is 10ntu after pretreating process removes colloid and suspension, it is divided into two parts in proportion
Cooling processing is not carried out, and the mode using multi-stage vacuum shwoot for accounting for the high-temperature acidic waste water of total release 80% is cooled to 30
DEG C, indirect steams of the 5.6t caused by vacuum shwoot more than 60 DEG C uses into multi-effect evaporation system, accounts for total release 20%
High-temperature acidic waste water is cooled to 35 DEG C with 33 DEG C of the concentrate that membrane filtration concentration systems are isolated using heat exchanger heat exchange.
Acid waste water after two parts cooling enters membrane filtration concentration systems and is further processed jointly, by film mistake
33m is obtained after filter concentration systems processing3/ h acid waste water concentrate, temperature are 33 DEG C；Each component concentration be sulfuric acid 30g/L,
Sodium sulphate 90g/L, zinc sulfate 2.5g/L, the 167m that the processing of membrane filtration concentration systems is isolated3/ h filtrates are returned as industrial water
With to viscose rayon production system.
Acid waste water concentrate enters back into vapo(u)rization system after first passing through preheating, and preheating is passed through by the way of heat exchange heats up
High-temperature acidic water reuse heat exchanger with accounting for total release 20%, which exchanges heat, is warming up to 82 DEG C, is obtained after vapo(u)rization system is handled
8.4m3/ h final concentrate the reuse of sulfur acid 118g/L, sodium sulphate 354g/L, zinc sulfate 9.5g/L produces to viscose rayon
Acid bath step in system, 24.6m caused by vapo(u)rization system3/ h condensed waters produce as industrial water reuse to viscose rayon
System.
Embodiment 3
By 90 DEG C of temperature, water 200m3/ h acid waste water (after testing, sulfur acid 10g/L, sodium sulphate 30g/L, sulfuric acid
Zinc 0.8g/L, turbidity 40ntu) turbidity is 10ntu after pretreating process removes colloid and suspension, it is divided into two in proportion
Cooling processing is carried out respectively, and the mode using multi-stage vacuum shwoot for accounting for the high-temperature acidic waste water of total release 52% is cooled to 30
DEG C, indirect steams of the 4.6t caused by vacuum shwoot more than 60 DEG C uses into multi-effect evaporation system, accounts for total release 48%
High-temperature acidic waste water is cooled to 38 DEG C with 35 DEG C of the concentrate that membrane filtration concentration systems are isolated using heat exchanger heat exchange.
Acid waste water after two parts cooling enters membrane filtration concentration systems and is further processed jointly, by film mistake
80m is obtained after filter concentration systems processing3/ h acid waste water concentrate, temperature are 33 DEG C；Each component concentration be sulfuric acid 25g/L,
Sodium sulphate 75g/L, zinc sulfate 2g/L, the 120m that the processing of membrane filtration concentration systems is isolated3/ h filtrates are as industrial water reuse
To viscose rayon production system.
Acid waste water concentrate enters back into vapo(u)rization system after first passing through preheating, and preheating is passed through by the way of heat exchange heats up
High-temperature acidic water reuse heat exchanger with accounting for total release 48%, which exchanges heat, is warming up to 85 DEG C, is obtained after vapo(u)rization system is handled
17.4m3/ h sulfur acid 117g/L, sodium sulphate 351g/L, zinc sulfate 10g/L final concentrate reuse to viscose rayon produces
Acid bath step in system, 62.6m caused by vapo(u)rization system3/ h condensed waters produce as industrial water reuse to viscose rayon
System.
Embodiment 4
By 90 DEG C of temperature, water 200m3/ h acid waste water (after testing, sulfur acid 10g/L, sodium sulphate 30g/L, sulfuric acid
Zinc 0.8g/L, turbidity 40ntu) turbidity is 10ntu after pretreating process removes colloid and suspension, it is divided into two in proportion
Cooling processing is carried out respectively, and the mode using multi-stage vacuum shwoot for accounting for the high-temperature acidic waste water of total release 60% is cooled to 30
DEG C, indirect steams of the 5.4t caused by vacuum shwoot more than 60 DEG C uses into multi-effect evaporation system, accounts for total release 40%
High-temperature acidic waste water is cooled to 38 DEG C with 35 DEG C of the concentrate that membrane filtration concentration systems are isolated using heat exchanger heat exchange.
Acid waste water after two parts cooling enters membrane filtration concentration systems and is further processed jointly, by film mistake
66.5m is obtained after filter concentration systems processing3/ h acid waste water concentrate, temperature are 35 DEG C；Each component concentration is sulfuric acid 30g/
L, sodium sulphate 90g/L, zinc sulfate 2.5g/L, the 133.5m that the processing of membrane filtration concentration systems is isolated3/ h filtrates are used as production
Water circulation is to viscose rayon production system.
Acid waste water concentrate enters back into vapo(u)rization system after first passing through preheating, and preheating is passed through by the way of heat exchange heats up
High-temperature acidic water reuse heat exchanger with accounting for total release 40%, which exchanges heat, is warming up to 85 DEG C, is obtained after vapo(u)rization system is handled
16.5m3/ h sulfur acid 120g/L, sodium sulphate 351g/L, zinc sulfate 10g/L final concentrate reuse to viscose rayon produces
Acid bath step in system, 50m caused by vapo(u)rization system3/ h condensed waters produce as industrial water reuse to viscose rayon
System.
Embodiment 5
By 98 DEG C of temperature, water 200m3/ h acid waste water (after testing, sulfur acid 13g/L, sodium sulphate 40g/L, sulfuric acid
Zinc 1.1g/L, turbidity 30ntu) turbidity is 8ntu after pretreating process removes colloid and suspension, it is divided into two in proportion
Cooling processing is carried out respectively, and the mode using multi-stage vacuum shwoot for accounting for the high-temperature acidic waste water of total release 40% is cooled to 30
DEG C, indirect steams of the 4.7t caused by vacuum shwoot more than 60 DEG C uses into multi-effect evaporation system, accounts for total release 60%
High-temperature acidic waste water is cooled to 38 DEG C with 35 DEG C of the concentrate that membrane filtration concentration systems are isolated using heat exchanger heat exchange.
Acid waste water after two parts cooling enters membrane filtration concentration systems and is further processed jointly, by film mistake
104m is obtained after filter concentration systems processing3/ h acid waste water concentrate, temperature are 35 DEG C；Each component concentration be sulfuric acid 25g/L,
Sodium sulphate 75g/L, zinc sulfate 2g/L, the 96m that the processing of membrane filtration concentration systems is isolated3/ h filtrates as industrial water reuse extremely
Viscose rayon production system.
Acid waste water concentrate enters back into vapo(u)rization system after first passing through preheating, and preheating is passed through by the way of heat exchange heats up
High-temperature acidic water reuse heat exchanger with accounting for total release 60%, which exchanges heat, is warming up to 90 DEG C, is obtained after vapo(u)rization system is handled
22.5m3/ h sulfur acid 115g/L, sodium sulphate 345g/L, zinc sulfate 9.5g/L final concentrate reuse to viscose rayon is given birth to
Acid bath step in production system, 73.5m caused by vapo(u)rization system3/ h condensed waters produce as industrial water reuse to viscose rayon
System.
Embodiment 6
By 98 DEG C of temperature, water 200m3/ h acid waste water (after testing, sulfur acid 13g/L, sodium sulphate 39g/L, sulfuric acid
Zinc 1.1g/L, turbidity 30ntu) turbidity is 8ntu after pretreating process removes colloid and suspension, it is divided into two in proportion
Cooling processing is carried out respectively, and the mode using multi-stage vacuum shwoot for accounting for the high-temperature acidic waste water of total release 50% is cooled to 30
DEG C, indirect steams of the 5.9t caused by vacuum shwoot more than 60 DEG C uses into multi-effect evaporation system, accounts for total release 50%
High-temperature acidic waste water is cooled to 38 DEG C with 35 DEG C of the concentrate that membrane filtration concentration systems are isolated using heat exchanger heat exchange.
Acid waste water after two parts cooling enters membrane filtration concentration systems and is further processed jointly, by film mistake
Filter 86.5m after concentration systems are handled3/ h acid waste water concentrate, temperature are 35 DEG C；Each component concentration is sulfuric acid 30g/L, sulphur
Sour sodium 90g/L, zinc sulfate 2.5g/L, the 113.5m that the processing of membrane filtration concentration systems is isolated3/ h filtrates are returned as industrial water
With to viscose rayon production system.
Acid waste water concentrate enters back into vapo(u)rization system after first passing through preheating, and preheating is passed through by the way of heat exchange heats up
High-temperature acidic water reuse heat exchanger with accounting for total release 50%, which exchanges heat, is warming up to 90 DEG C, is obtained after vapo(u)rization system is handled
21.5m3/ h sulfur acid 120g/L, sodium sulphate 360g/L, zinc sulfate 10g/L final concentrate reuse to viscose rayon produces
Acid bath step in system, 65m caused by vapo(u)rization system3/ h condensed waters produce as industrial water reuse to viscose rayon
System.
Comparative example 1
By 85 DEG C of temperature, water 200m3/ h acid waste water (after testing, sulfur acid 5g/L, sodium sulphate 15g/L, zinc sulfate
0.3g/L, turbidity 50ntu) turbidity is 10ntu after pretreating process removes colloid and suspension, utilize multi-stage vacuum shwoot
Mode be cooled to 30 DEG C, 7t caused by vacuum shwoot more than 60 DEG C indirect steam enter multi-effect evaporation system use.
Acid waste water after cooling enters membrane filtration concentration systems and is further processed, by membrane filtration concentration systems
40m is obtained after processing3/ h acid waste water concentrate, temperature are 31 DEG C；Each component concentration is sulfuric acid 25g/L, sodium sulphate 75g/
L, zinc sulfate 2g/L, into vapo(u)rization system, further evaporation and concentration is handled.8.5m is obtained after vapo(u)rization system is handled3/ h's contains
Sulfuric acid 118g/L, sodium sulphate 354g/L, zinc sulfate 9.5g/L final concentrate reuse to viscose rayon production system in acid
Bathe step, the 160m that the processing of membrane filtration concentration systems is isolated331.5m caused by/h filtrates and vapo(u)rization system3/ h condensed water conducts
Industrial water reuse is to viscose rayon production system.
Comparative example 2
By 85 DEG C of temperature, water 200m3/ h acid waste water (after testing, sulfur acid 5g/L, sodium sulphate 15g/L, zinc sulfate
0.5g/L, turbidity 50ntu) it is directly entered the processing of vapo(u)rization system evaporation and concentration.The 8.5m obtained after vapo(u)rization system is handled3/h
Sulfur acid 118g/L, sodium sulphate 354g/L, the final concentrate reuses of zinc sulfate 9.5g/L are into viscose rayon production system
Acid bath step, 191m caused by vapo(u)rization system3/ h condensed waters are as industrial water reuse to viscose rayon production system.
Comparative example 3
By 90 DEG C of temperature, water 200m3/ h acid waste water (after testing, sulfur acid 10g/L, sodium sulphate 30g/L, sulfuric acid
Zinc 0.8g/L, turbidity 40ntu) turbidity is 10ntu after pretreating process removes colloid and suspension, dodged using multi-stage vacuum
The mode of hair is cooled to 30 DEG C, and indirect steams of the 8t caused by vacuum shwoot more than 60 DEG C uses into multi-effect evaporation system.
Acid waste water after cooling enters membrane filtration concentration systems and is further processed jointly, is concentrated by membrane filtration
80m is obtained after system processing3/ h acid waste water concentrate, temperature are 31 DEG C；Each component concentration is sulfuric acid 25g/L, sodium sulphate
75g/L, zinc sulfate 2g/L, into vapo(u)rization system, further evaporation and concentration is handled.17m is obtained after vapo(u)rization system is handled3/h
Sulfur acid 117g/L, sodium sulphate 351g/L, zinc sulfate 9.8g/L final concentrate reuse is into viscose rayon production system
Acid bath step, the 120m that isolates of membrane filtration concentration systems processing323m caused by/h filtrates and vapo(u)rization system3/ h condensed waters are made
For industrial water reuse to viscose rayon production system.
Comparative example 4
By 90 DEG C of temperature, water 200m3/ h acid waste water (after testing, sulfur acid 10g/L, sodium sulphate 30g/L, sulfuric acid
Zinc 0.8g/L, turbidity 40ntu) it is directly entered the processing of vapo(u)rization system evaporation and concentration.17m is obtained after vapo(u)rization system is handled3/h
Sulfur acid 117g/L, sodium sulphate 351g/L, zinc sulfate 9.8g/L final concentrate reuse is into viscose rayon production system
Acid bath step, 183m caused by vapo(u)rization system3/ h condensed waters are as industrial water reuse to viscose rayon production system.
Comparative example 5
By 98 DEG C of temperature, water 200m3/ h acid waste water (after testing, sulfur acid 13g/L, sodium sulphate 40g/L, sulfuric acid
Zinc 1.1g/L, turbidity 30tu) turbidity is 8ntu after pretreating process removes colloid and suspension, utilize multi-stage vacuum shwoot
Mode be cooled to 30 DEG C, 10t caused by vacuum shwoot more than 60 DEG C indirect steam enter multi-effect evaporation system use.
Acid waste water after cooling enters membrane filtration concentration systems and is further processed jointly, is concentrated by membrane filtration
104m is obtained after system processing3/ h acid waste water concentrate, temperature are 31 DEG C；Each component concentration is sulfuric acid 25g/L, sodium sulphate
75g/L, zinc sulfate 2g/L, into vapo(u)rization system, further evaporation and concentration is handled.21.5m is obtained after vapo(u)rization system is handled3/
H sulfur acid 120g/L, sodium sulphate 360g/L, zinc sulfate 10g/L final concentrate reuse are into viscose rayon production system
Acid bath step, the 96m that isolates of membrane filtration concentration systems processing382.5m caused by/h filtrates and vapo(u)rization system3/ h condensed waters
As industrial water reuse to viscose rayon production system.
Comparative example 6
By 90 DEG C of temperature, water 200m3/ h acid waste water (after testing, sulfur acid 10g/L, sodium sulphate 30g/L, sulfuric acid
Zinc 0.8g/L, turbidity 40ntu) turbidity is 10ntu after pretreating process removes colloid and suspension, steamed into vapo(u)rization system
Send out concentration.16.5m is obtained after vapo(u)rization system is handled3/ h sulfur acid 120g/L, sodium sulphate 360g/L, zinc sulfate
Acid bath step in 10g/L final concentrate reuse to viscose rayon production system, 183.5m caused by vapo(u)rization system3/ h is cold
Condensate is as industrial water reuse to viscose rayon production system.
Comparative analysis is tested
Interpretation of result：
By to membrane filtration concentration systems in embodiment 1-6 and the energy consumption analysis of vapo(u)rization system, membrane filtration concentration systems point
Cost from 1 ton of filtrate is 5.8 yuan, makes full use of rear vapo(u)rization system to evaporate 1 ton of waste water cost the heat in acid waste water and exists
25 yuan -30 yuan.Therefore as far as possible more filtrate is isolated in membrane filtration concentration systems in the waste water treatment process of the application to be advantageous to
Reduce overall energy consumption.
And in comparative example 1,3,5, acid waste water only cools, and film concentrate does not preheat, into the fluid temperature of vapo(u)rization system
At 31 DEG C, the operation of membrane filtration concentration systems is costly constant, and the fluid temperature for entering vapo(u)rization system too low can cause to evaporate
System steam consumption is big, and one ton of water of evaporation will consume 0.4t steam, and vapo(u)rization system evaporates the cost of one ton of water at 50 yuan or so.
And in comparative example 2,4,6, it is dense to be directly entered vapo(u)rization system evaporation without membrane filtration concentration systems for acid waste water
Contracting, whole waters will evaporate separation in vapo(u)rization system, and the cost that vapo(u)rization system evaporates 1 ton of water is about membrane filtration concentration
System separates 4 times of the cost of 1 ton of water.The moisture content for so resulting in membrane filtration concentration systems being used to separate originally will be with 4 times
Cost steamed in vapo(u)rization system.
As can be seen here, in embodiment 1-6, the cooling of acid waste water and preheating Cooling and Heat Source each other, by the heat in acid waste water
Amount makes full use of, and compared to comparative example 1-6, can reduce overall energy consumption, so as to reduce the processing cost of acid waste water.
The foregoing is only presently preferred embodiments of the present invention, be not intended to limit the invention, it is all the present invention spirit and
Within principle, any modification, equivalent substitution and improvements made etc., it should be included in the scope of the protection.
Claims (8)
1. the method for the heat integration during a kind of processing viscose rayon acid waste water, it is characterised in that including following
Step：
(1) acid waste water is cooled into membrane filtration concentration systems to carry out handling required temperature；
(2) acid waste water after cooling carries out filtering and concentrating using membrane filtration concentration systems, obtains acid waste water concentrate；
(3) the acid waste water concentrate is further concentrated by evaporation after preheating into vapo(u)rization system；
Wherein, acid waste water concentrate Cooling and Heat Source each other in acid waste water and step (3) in step (1), carries out heat exchange, simultaneously
Realize the cooling of acid waste water and the preheating of acid waste water concentrate.
2. the method for the heat integration during a kind of processing viscose rayon acid waste water according to claim 1, its
It is characterised by, the viscose rayon acid waste water is the Fiber wash for the entrainment acid bath discharged in production process of viscose fiber
Water, exhaust position is before fibre cutting or after fibre cutting.
3. the method for the heat integration during a kind of processing viscose rayon acid waste water according to claim 2, its
It is characterised by, the temperature of the viscose rayon acid waste water is 85-98 DEG C, and each component concentration is sulfuric acid 5-13g/L, sodium sulphate
15-40g/L, zinc sulfate 0.3-1.1g/L, turbidity 30-50ntu.
4. according to the heat integration during a kind of any one of claims 1 to 3 processing viscose rayon acid waste water
Method, it is characterised in that acid waste water described in step (1) cooling using heat exchange cooling and vacuum shwoot cooling side
Formula, acid waste water is cooled to 30-38 DEG C.
5. the method for the heat integration during a kind of processing viscose rayon acid waste water according to claim 4, its
It is characterised by, what the heat exchange cooling provided low-temperature receiver using heat exchanger, for heat exchanger is that the middle process membrane filtration of step (2) is dense
The acid waste water concentrate obtained after compression system processing, the vacuum shwoot cooling uses multi-stage vacuum shwoot, caused secondary
Steam is used for the vapo(u)rization system of step (3).
6. according to the heat integration during a kind of any one of claims 1 to 3 processing viscose rayon acid waste water
Method, it is characterised in that the temperature of acid waste water concentrate after the processing of membrane filtration concentration systems described in step (2) is
33-40 DEG C, each component concentration is sulfuric acid 25-30g/L, sodium sulphate 75-90g/L, zinc sulfate 2-2.5g/L.
7. according to the heat integration during a kind of any one of claims 1 to 3 processing viscose rayon acid waste water
Method, it is characterised in that acid waste water concentrate described in step (3) preheating using heat exchange heating by the way of, after preheating
Temperature be 82-90 DEG C.
8. the method for the heat integration during a kind of processing viscose rayon acid waste water according to claim 7, its
It is characterised by, what the heat exchange heating provided thermal source using heat exchanger, for heat exchanger is acid waste water in step (1).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201710892626.1A CN107686204B (en) | 2017-09-27 | 2017-09-27 | Method for comprehensively utilizing heat energy in viscose fiber acid wastewater treatment process |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201710892626.1A CN107686204B (en) | 2017-09-27 | 2017-09-27 | Method for comprehensively utilizing heat energy in viscose fiber acid wastewater treatment process |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN107686204A true CN107686204A (en) | 2018-02-13 |
| CN107686204B CN107686204B (en) | 2021-03-05 |
Family
ID=61156771
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201710892626.1A Active CN107686204B (en) | 2017-09-27 | 2017-09-27 | Method for comprehensively utilizing heat energy in viscose fiber acid wastewater treatment process |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN107686204B (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109293112A (en) * | 2018-10-17 | 2019-02-01 | 新疆中泰创新技术研究院有限责任公司 | A kind of processing method of viscose rayon acid waste water resource utilization |
| CN111268841A (en) * | 2020-02-25 | 2020-06-12 | 苏州翔铭化工设备有限公司 | Method for desalting yeast drum wastewater |
| CN111470560A (en) * | 2019-01-24 | 2020-07-31 | 山东雅美科技有限公司 | Method for recycling acid wastewater in viscose fiber production |
Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CA2442490A1 (en) * | 2001-03-29 | 2002-10-10 | Nippon Steel Chemical Co | Acidic-wastewater treating material and method of treating acidic wastewater |
| CN104058539A (en) * | 2014-07-07 | 2014-09-24 | 成都丽雅纤维股份有限公司 | Semi-fiber treatment process based on industrial waste water of viscose |
| US20160031727A1 (en) * | 2013-11-27 | 2016-02-04 | Sumitomo Electric Industries, Ltd. | Wastewater treatment method, membrane distillation module and wastewater treatment apparatus |
| CN205313131U (en) * | 2015-12-18 | 2016-06-15 | 许达人 | Sulfur acid and multiple effect evaporation enrichment facility of salt solution thereof |
| CN105692989A (en) * | 2014-11-27 | 2016-06-22 | 上海凯鑫分离技术股份有限公司 | A comprehensive utilization process for viscose fiber acidic waste water |
| CN106145496A (en) * | 2016-08-03 | 2016-11-23 | 上海凯鑫分离技术股份有限公司 | The comprehensive utilization process of viscose fiber acid waste water |
-
2017
- 2017-09-27 CN CN201710892626.1A patent/CN107686204B/en active Active
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CA2442490A1 (en) * | 2001-03-29 | 2002-10-10 | Nippon Steel Chemical Co | Acidic-wastewater treating material and method of treating acidic wastewater |
| US20160031727A1 (en) * | 2013-11-27 | 2016-02-04 | Sumitomo Electric Industries, Ltd. | Wastewater treatment method, membrane distillation module and wastewater treatment apparatus |
| CN104058539A (en) * | 2014-07-07 | 2014-09-24 | 成都丽雅纤维股份有限公司 | Semi-fiber treatment process based on industrial waste water of viscose |
| CN105692989A (en) * | 2014-11-27 | 2016-06-22 | 上海凯鑫分离技术股份有限公司 | A comprehensive utilization process for viscose fiber acidic waste water |
| CN205313131U (en) * | 2015-12-18 | 2016-06-15 | 许达人 | Sulfur acid and multiple effect evaporation enrichment facility of salt solution thereof |
| CN106145496A (en) * | 2016-08-03 | 2016-11-23 | 上海凯鑫分离技术股份有限公司 | The comprehensive utilization process of viscose fiber acid waste water |
Non-Patent Citations (2)
| Title |
|---|
| 于宏兵等: "《食品行业清洁生产及案例解析》", 30 November 2006, 新华出版社 * |
| 王永刚等: "《煤化工工艺学》", 30 September 2014, 中国矿业大学出版社 * |
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109293112A (en) * | 2018-10-17 | 2019-02-01 | 新疆中泰创新技术研究院有限责任公司 | A kind of processing method of viscose rayon acid waste water resource utilization |
| CN109293112B (en) * | 2018-10-17 | 2021-07-16 | 新疆中泰纺织集团有限公司 | Treatment method for recycling viscose fiber acid wastewater |
| CN111470560A (en) * | 2019-01-24 | 2020-07-31 | 山东雅美科技有限公司 | Method for recycling acid wastewater in viscose fiber production |
| CN111268841A (en) * | 2020-02-25 | 2020-06-12 | 苏州翔铭化工设备有限公司 | Method for desalting yeast drum wastewater |
| CN111268841B (en) * | 2020-02-25 | 2022-11-22 | 苏州翔铭化工设备有限公司 | Method for desalting yeast drum wastewater |
Also Published As
| Publication number | Publication date |
|---|---|
| CN107686204B (en) | 2021-03-05 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN107500464A (en) | A kind of method for handling viscose rayon factory acid waste water | |
| CN102351220B (en) | System and technology for recovering sodium nitrate from tin-containing waste liquid treatment tail water | |
| CN105523676B (en) | A kind of high-salinity wastewater zero-emission crystalline salt by evaporation sub-prime method | |
| CN107686204A (en) | A kind of method of heat integration during processing viscose rayon acid waste water | |
| CN1724339A (en) | Process of industrialize for waste acid concentrition recovering used in titanium white production by sulfuric acid method | |
| CN211770721U (en) | A refining system for sodium sulfate waste liquid in viscose fiber production | |
| CN206359427U (en) | Garbage flying ash water-washing pre-treatment and cement kiln collaboration disposal of resources system | |
| CN107352727B (en) | Method for realizing zero discharge of coal chemical industry wastewater | |
| CN108002642B (en) | A kind of viscose fiber wastewater, sludge, exhaust-gas treatment system and method | |
| CN109956690A (en) | A kind of domestic garbage incineration flyash processing method for cement industry | |
| WO2022142397A1 (en) | Recycling process for viscose fiber sodium sulfate waste liquid | |
| CN206089281U (en) | Steel industry sulphuric acid pickling liquid waste's processing recovery system | |
| CN106082516A (en) | A kind of point of salt-pepper noise technique and device | |
| CN104086011B (en) | Be applicable to the technique of zero discharge of viscose fibre industry acid station waste water | |
| CN109133447A (en) | A kind of on-line monitoring system and method for viscose glue waste liquid | |
| CN109019987A (en) | A kind of efficient recycling method of dyeing waste water | |
| CN206176948U (en) | Matter and dry water recycle system are put forward to brown coal drying | |
| CN109133446A (en) | A kind of on-line control system and method for viscose glue waste liquid | |
| CN205328787U (en) | Zinc borate waste water's resourceful treatment system | |
| CN105254100B (en) | A kind of saline sewage processing system and method | |
| CN110040892A (en) | High slat-containing wastewater, distilled ammonia wastewater Combined Treatment technique of zero discharge and system | |
| CN110877941B (en) | Ammonia distillation waste liquid recycling system and method by ammonia-alkali method | |
| CN209602283U (en) | A kind of on-line monitoring system of viscose glue waste liquid | |
| CN205099565U (en) | Deep dehydrating system for sludge | |
| CN208517182U (en) | High slat-containing wastewater, distilled ammonia wastewater Combined Treatment Zero discharging system |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |