CN110436690A - A kind of novel treatment technology of acrylic acid waste water - Google Patents
A kind of novel treatment technology of acrylic acid waste water Download PDFInfo
- Publication number
- CN110436690A CN110436690A CN201910751168.9A CN201910751168A CN110436690A CN 110436690 A CN110436690 A CN 110436690A CN 201910751168 A CN201910751168 A CN 201910751168A CN 110436690 A CN110436690 A CN 110436690A
- Authority
- CN
- China
- Prior art keywords
- acrylic acid
- reaction kettle
- waste water
- treatment technology
- acid waste
- 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.)
- Pending
Links
Classifications
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F11/00—Treatment of sludge; Devices therefor
- C02F11/12—Treatment of sludge; Devices therefor by de-watering, drying or thickening
- C02F11/121—Treatment of sludge; Devices therefor by de-watering, drying or thickening by mechanical de-watering
- C02F11/122—Treatment of sludge; Devices therefor by de-watering, drying or thickening by mechanical de-watering using filter presses
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F9/00—Multistage treatment of water, waste water or sewage
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C51/00—Preparation of carboxylic acids or their salts, halides or anhydrides
- C07C51/41—Preparation of salts of carboxylic acids
- C07C51/412—Preparation of salts of carboxylic acids by conversion of the acids, their salts, esters or anhydrides with the same carboxylic acid part
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C51/00—Preparation of carboxylic acids or their salts, halides or anhydrides
- C07C51/42—Separation; Purification; Stabilisation; Use of additives
- C07C51/43—Separation; Purification; Stabilisation; Use of additives by change of the physical state, e.g. crystallisation
-
- 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
-
- 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
- C02F1/38—Treatment of water, waste water, or sewage by centrifugal separation
-
- 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
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
- C02F1/5236—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using inorganic agents
- C02F1/5245—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using inorganic agents using basic salts, e.g. of aluminium and iron
-
- 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
- C02F1/66—Treatment of water, waste water, or sewage by neutralisation; pH adjustment
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/30—Organic compounds
- C02F2101/34—Organic compounds containing oxygen
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
- C02F2103/34—Nature of the water, waste water, sewage or sludge to be treated from industrial activities not provided for in groups C02F2103/12 - C02F2103/32
- C02F2103/36—Nature of the water, waste water, sewage or sludge to be treated from industrial activities not provided for in groups C02F2103/12 - C02F2103/32 from the manufacture of organic compounds
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2301/00—General aspects of water treatment
- C02F2301/08—Multistage treatments, e.g. repetition of the same process step under different conditions
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Engineering & Computer Science (AREA)
- Life Sciences & Earth Sciences (AREA)
- Hydrology & Water Resources (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Mechanical Engineering (AREA)
- Crystallography & Structural Chemistry (AREA)
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Abstract
A kind of novel treatment technology of acrylic acid waste water, belongs to acrylic acid waste water-treatment technology field.It is characterized by comprising following steps: after acrylic acid wastewater is heated to 70 ~ 80 DEG C by step 1) in investment reaction kettle (5)；Step 2 continuously adds calcium oxide into reaction kettle (5), and makes the pH 9.5 ~ 10 in reaction kettle (5)；The dregs of reaction kettle (5) bottom are sent into processing in plate and frame filter press (8) by step 3)；Step 4), to reuse or discharge after distillation water process, is packed the calcium acetate of crystallization and is collected to separating after mixed liquor evaporative crystallization.The treatment technology of acrylic acid waste water of the utility model had not only avoided the waste of material, but also was adequately handled waste water, can reach in line standard, not can cause environmental pollution.
Description
Technical field
A kind of novel treatment technology of acrylic acid waste water, belongs to acrylic acid waste water-treatment technology field.
Background technique
Processing acrylic acid wastewater mostly uses traditional heating power to burn waster water process at present, i.e., in incinerator burning fuels inside
Gas or fuel oil are added the waste water being discharged in acrylic acid production process, make in waste water after so that in-furnace temperature is reached 700~850 DEG C
Volatile organic matter at high temperature oxygenolysis become environmental sound carbon dioxide and water.But above-mentioned processing energy consumption
Height causes disaggregated cost high, and the utility in acrylic acid wastewater also directly decomposes discharge, causes the waste of raw material,
And treated that waste water is difficult to meet in line requirement, and it is larger to the pollution of environment.
Summary of the invention
It can either be to acrylic acid waste the technical problem to be solved by the present invention is overcoming the deficiencies of the prior art and provide one kind
Water is handled, additionally it is possible to the novel treatment technology of acrylic acid waste water recycled to the acrylic acid in waste water.
The technical solution adopted by the present invention to solve the technical problems is: the novel treatment technology of acrylic acid waste water,
It is characterized in that: including the following steps:
Step 1) is put into reaction kettle after acrylic acid wastewater is heated to 70 ~ 80 DEG C；
Step 2 continuously adds calcium oxide into reaction kettle, and makes the pH 9.5 ~ 10 in reaction kettle；
The dregs of reactor bottom are sent into plate and frame filter press and are handled by step 3)；
Step 4), to reuse or discharge after distillation water process, packs the calcium acetate of crystallization to separating after mixed liquor evaporative crystallization
It collects.
Preferably, the mixed liquor in reaction kettle described in step 2 is stirred by way of aeration.
Preferably, the reaction time in reaction kettle 5 described in step 2 is 0.5 ~ 1h.
Preferably, the amount for the calcium oxide being added into step 2 is that 38g is added in every liter of acrylic acid wastewater.
Preferably, evaporative crystallization described in step 4) carries out triple effect evaporation crystallization using evaporator, and evaporator is connected with
Forced circulation pump.
Preferably, centrifugal separator point is successively entered back into after thickener to the mixed liquor after the crystallization in step 4)
From to the evaporative crystallization again of the mother liquor after separation.
Preferably, reaction kettle described in step 1) ~ step 3) has at least two be arranged in parallel.
Preferably, negative pressure state is maintained in reaction kettle described in step 2.
Preferably, the mixed liquor in reaction kettle described in step 2 is sampled, when the formaldehydeless peculiar smell of sample, and color is
When rufous, then the reaction terminating in reaction kettle is judged.
Compared with prior art, the present invention has the beneficial effects that
1, the treatment technology of acrylic acid waste water of the utility model handles acrylic acid wastewater, and to the acrylic acid in waste water again
It utilizes, has obtained Ca-Acetate crystals, and can be with reuse or discharge, with existing acrylic acid waste water process phase after distillation water process
Than greatly reducing processing cost, and treated Ca-Acetate crystals can be obtained after the deep processing higher industrial second of purity
Sour calcium had not only avoided the waste of material, but also had adequately been handled waste water, can reach in line standard, will not be to environment
It pollutes.
2, it to the liquid agitation in reaction kettle by way of aeration, ensure that reaction in reaction kettle faster, and react
More sufficiently.
3, the reaction time in reaction kettle is 0.5 ~ 1h, reacts the acrylic acid wastewater in reaction kettle sufficiently with calcium oxide.
4,38g calcium oxide is put into every liter of acrylic acid wastewater, can either guarantee that the acrylic acid in acrylic acid wastewater is sufficiently anti-
It answers, and is able to maintain that the pH in reaction kettle.
5, it is crystallized using triple effect evaporation, improves the efficiency of crystallization, evaporator is connected with forced circulation pump, increases flowing
The phenomenon that effect, reduction crystallizes in evaporator, improves heat transfer efficiency, will not generate wall built-up and plugging, performance is relatively reliable.
6, it is separated by being entered back into centrifugal separator after the concentration of thickener raising crystallization, improves separative efficiency,
To mother liquor evaporative crystallization again, the acrylic acid in waste water is made full use of, also avoids in waste water that there are acrylic acid, it is dirty after discharge
Contaminate environment.
7, there are two reaction kettle is at least arranged in parallel, so that reaction kettle in parallel works alternatively, guarantee to realize continuous useless
Water process, treatment effeciency are high.
8, negative pressure state is maintained in reaction kettle, can be avoided the pernicious gas evolution pollution environment in reaction kettle.
9, by the taste of sample and color, it can be reacted and whether be terminated with accurate judgement, can guarantee the change in reaction kettle
It is more abundant to learn reaction.
Detailed description of the invention
Fig. 1 is the pipeline connecting figure of novel treatment technology of acrylic acid waste water.
Fig. 2 is the pipeline connecting figure of evaporated crystallization device.
In figure: 1,2 steam input pipe 3 of heat exchanger, steam output pipe 4, waste water input pipe 5, reaction kettle 6,
Sludge pump 7, elevator pump 8, plate and frame filter press 9, evaporated crystallization device 10, condensation water preheater 11, condensed water return
Water pipe 12, raw material input pipe 13, steam pipeline 14, circulating water inlet 15, the effect point of 1st effective evaporator 16, one
Separator 19, triple effect evaporator 20, triple effect separator 21, forced circulation are imitated from device 17,2nd effect evaporator 18, two
Pump 22, condenser 23, discharging pump 24, condensate water pot 25, condensate pump 26, vacuum pump 27, mother liquor tank 28,
Mother liquor pumps 29, centrifugal separator 30, thickener 31, recirculated water return pipe 32, condensed water delivery pipe 33, blower.
Specific embodiment
Fig. 1 ~ 2 are highly preferred embodiment of the present invention, and 1 ~ 2 the present invention will be further described with reference to the accompanying drawing.
Acrylic acid waste water treatment system, including heat exchanger 1, reaction kettle 5, plate and frame filter press 8 and evaporated crystallization device 9,
The shell side inlet of heat exchanger 1 is connected with steam input pipe 2, and the shell-side outlet of heat exchanger 1 is connected with steam output pipe 3, heat exchanger 1
Tube-side inlet be connected with waste water input pipe 4, the tube side outlet of heat exchanger 1 is connected with the inlet of reaction kettle 5, reaction kettle 5
Slag notch be connected with the feed inlet of plate and frame filter press 8, the liquid outlet of reaction kettle 5 is connected with evaporated crystallization device 9.This third
Olefin(e) acid waste water treatment system makes acrylic acid wastewater heat up by heat exchanger 1, and chemistry occurs instead with calcium oxide in reaction kettle 5
Answer, then mixed liquor crystallized by evaporated crystallization device 9, to obtain Ca-Acetate crystals, to acrylic acid wastewater into
Row processing, and utilizes the acrylic acid in waste water again, has obtained Ca-Acetate crystals, and distill after water process can with reuse or
Discharge, compared with existing acrylic acid waste water process, greatly reduces processing cost, and treated Ca-Acetate crystals are through depth
The higher industrial acetic calcium of purity can be obtained after processing, not only avoided the waste of material, but also adequately handled waste water,
In line standard can be reached, do not can cause environmental pollution.
The present invention will be further described combined with specific embodiments below, however persons familiar with the art it is to be appreciated that
Here in connection with the detailed description that attached drawing provides be in order to preferably explain, structure of the invention necessarily have exceeded it is limited these
Embodiment, and for some equivalents or common approach, it is no longer described in detail herein, but still fall within the guarantor of the application
Protect range.
Specific: the shell side inlet of heat exchanger 1 is connected with steam input pipe 2, the shell-side outlet of heat exchanger 1 as shown in Figure 1:
It is connected with steam output pipe 3, the tube-side inlet of heat exchanger 1 is connected with waste water input pipe 4, and the tube side of heat exchanger 1 is exported and reacted
The inlet of kettle 5 is connected, and waste water is heated up by heat exchanger 1, to reach suitable reaction temperature, guarantees in reaction kettle 5
It can preferably chemically react.
The top of reaction kettle 5 is additionally provided with feed opening, calcium oxide can be added into reaction kettle 5 by feed opening, with right
Acrylic acid wastewater is neutralized, and adjusts the pH of acrylic acid wastewater.The discharge port of 5 bottom of reaction kettle is connected with plate and frame filter press 8,
It is provided with sludge pump 6 between the discharge port and plate and frame filter press 8 of reaction kettle 5, by sludge pump 6 by the dregs of 5 bottom of reaction kettle
It is pumped into plate and frame filter press 8, and filters pressing separation is carried out to dregs by plate and frame filter press 8, facilitate carry out subsequent processing.
The middle part of reaction kettle 5 or the liquid outlet of middle and lower part are connected with evaporated crystallization device 9, the liquid outlet of reaction kettle 5 and steaming
It is provided with elevator pump 7 between hair crystallization apparatus 9, the mixed liquor in reaction kettle 5 can be pumped by evaporative crystallization by elevator pump 7
It is evaporated crystallization in device 9, obtains Ca-Acetate crystals.
The bottom plate of reaction kettle 5 is provided with aerator (being not drawn into figure), aerator connection and compressed air, and compressed air is logical
It crosses aerator to be stirred the mixed liquor in reaction kettle 5, to improve reaction speed, guarantees that the material in reaction kettle 5 is sufficiently sent out
Raw reaction.5 outer wall of reaction kettle is also wound with coil pipe (being not drawn into figure), and the input terminal of coil pipe is connected with steam input pipe 2, disk
The output end of pipe is connected with steam output pipe 3, and is provided with valve between coil pipe and steam input pipe 2, can by coil pipe
Guarantee that the temperature in reaction kettle 5 maintains the required temperature chemically reacted, guarantees that rapid reaction carries out.In reaction kettle 5
It is additionally provided with pH meter, with the pH in real-time monitoring reaction kettle 5.
Reaction kettle 5 is at least provided in parallel two, and in the present embodiment, there are two reaction kettle 5 is arranged in parallel, two anti-
The inlet of kettle 5 is answered to be connected simultaneously with the outlet of the tube side of heat exchanger 1, and the pipe of the inlet of each reaction kettle 5 and heat exchanger 1
Journey is provided with valve between outlet.The slag notch of two reaction kettles 5 passes through the feed inlet of sludge pump 6 Yu plate and frame filter press 8
It is connected, and is provided with valve between the slag notch and sludge pump 6 of two reaction kettles 5.The top of two reaction kettles 5 is and wind
The air inlet of machine 33 is connected.
As shown in Figure 2: evaporated crystallization device includes evaporator, separator and centrifugal separator 29, and evaporator includes one
Evaporator 15,2nd effect evaporator 17 and triple effect evaporator 19 are imitated, separator and evaporator correspond, and separator includes an effect
Separator 16, two imitates separator 18 and triple effect separator 20, the tube side outlet of 1st effective evaporator 15 and an effect separator 16
Input port is connected, and the discharge port of an effect separator 16 is connected with the tube-side inlet of 2nd effect evaporator 17,2nd effect evaporator 17
Tube side outlet with two effect separators 18 input port be connected, two effect separators 18 discharge port and triple effect evaporator 19 pipe
Journey entrance is connected, and the tube side outlet of triple effect evaporator 19 is connected with the input port of triple effect separator 20, triple effect separator 20
Discharge port be connected with the feed inlet of centrifugal separator 29.
The liquid outlet of one effect separator 16 is connected with the tube-side inlet of 1st effective evaporator 15, and two effect separators 18 go out liquid
Mouth is connected with the tube-side inlet of 2nd effect evaporator 17, the liquid outlet of triple effect separator 20 and the tube-side inlet of triple effect evaporator 19
It is connected.
The input terminal of 1st effective evaporator 15 is connected with condensation water preheater 10, and the shell side inlet of 1st effective evaporator 15 is connected with
The shell-side outlet of steam pipeline 13,1st effective evaporator 15 is connected with the shell side inlet of condensation water preheater 10, and condensed water is pre-
The shell-side outlet of hot device 10 is connected with condensate ruturn pipe 11, and the tube-side inlet of condensation water preheater 10 is connected with raw material input pipe
12, raw material input pipe 12 is connected with the delivery outlet of elevator pump 7, thus by mixed liquor by being sent to after condensation water preheater 10
In 1st effective evaporator 15, the input port or 1st effective evaporator 15 of the tube side outlet of condensation water preheater 10 and an effect separator 16
Tube-side inlet is connected, in the present embodiment, the input port phase of the tube side outlet of condensation water preheater 10 and an effect separator 16
Connection.
The tube-side inlet of triple effect evaporator 19 is connected with forced circulation pump 21, the input port of forced circulation pump 21 and triple effect point
Liquid outlet from device 20 is connected, and the delivery outlet of forced circulation pump 21 is connected with the tube-side inlet of triple effect evaporator 19.One effect
Acetic acid calcium concentration is lower during evaporator 15 and 2nd effect evaporator 17, therefore Natural Circulation can be met the requirements, and calcium acetate is in triple effect
It is precipitated in evaporator 19, therefore forced circulation pump 21 is added in triple effect evaporator 19, increase flow effect, reduced in evaporator
Crystallization improves heat transfer efficiency, unsuitable wall built-up and plugging, for can evaporative crystallization material or be easy the material to scab, performance is more
Add reliable.
Thickener 30 is provided between the discharge port and centrifugal separator 29 of triple effect separator 20, triple effect separator 20 goes out
Material mouth is connected with the feed inlet of thickener 30, and the feed inlet of centrifugal separator 29 is connected with the discharge port of thickener 30.From
The liquid outlet of centrifugal separator 29 is connected with mother liquor tank 27, and the bottom of mother liquor tank 27 is connected with mother liquor pump 28, the input of mother liquor pump 28
End is connected with mother liquor tank 27, and the output end of mother liquor pump 28 is connected with the feed inlet of triple effect separator 20.Triple effect separator 20
Discharge port and thickener 30 between be provided with discharging pump 23.
Evaporated crystallization device is including further including condenser 22 and condensate water pot 24, top and two effects of an effect separator 16
The shell side inlet of evaporator 17 is connected, and the shell-side outlet of 2nd effect evaporator 17 is connected with condensate water pot 24, two effect separators
18 top is connected with the shell side inlet of triple effect evaporator 19, and the shell-side outlet of triple effect evaporator 19 is connected with condensate water pot 24
Logical, the top of triple effect separator 20 is connected with the tube-side inlet of condenser 22, the tube side outlet of condenser 22 and condensate water pot
24 are connected, and the shell side inlet of condenser 22 is connected with circulating water inlet 14, and the shell-side outlet of condenser 22 is connected with circulation
Water return pipe 31, so that the vapor evaporated to triple effect separator 20 condenses.The shell-side outlet of condenser 22 is also connected with
Vacuum pump 26, for adjusting the pressure in an effect separator 16, two effect separator 18 and triple effect separator 20, to facilitate mixed liquor
Conveying.
Condensate water pot 24 is also connected with condensed water delivery pipe 32, and condensate pump 25 is provided in condensed water delivery pipe 32.
A kind of novel treatment technology of acrylic acid waste water carrying out water process using above-mentioned acrylic acid waste water treatment system, packet
Include following steps:
Step 1) is put into reaction kettle 5 after acrylic acid wastewater is heated to 70 ~ 80 DEG C；
For acrylic acid wastewater in heat exchanger 1 and after steam heat-exchanging, temperature is promoted to 70 ~ 80 DEG C, then puts into a reaction kettle 5
It is interior.
Step 2 continuously adds calcium oxide into reaction kettle 5, and makes the pH 9.5 ~ 10 in reaction kettle 5；
Calcium oxide is put into the reaction kettle 5, the quality of the corresponding calcium oxide of every liter of acrylic acid wastewater is 38g, and passes through coil pipe
The temperature of reaction kettle 5 is set to maintain 80 DEG C, by the aerator of bottom to aeration stirring in reaction kettle 5, the reaction time is 0.5 ~ 1h.
In reaction process, make to maintain negative pressure state in reaction kettle 5 by blower 33.In reaction process, the pH in maintenance reaction kettle 5 is
9.5~10。
The chemical reaction occurred in reaction kettle 5 are as follows: 2CH3COOH+CaO → (CH3COO)2Ca+H2O；Calcium acetate can also be straight
It connects to be incorporated into coal and burn, calcium acetate is heated to the chemical equation of the chemical reaction occurred at 160 DEG C are as follows: (CH3COO)2Ca+4O2=CaCO3+3CO2+3H2O；Calcium acetate at high temperature completely burned when chemical reaction chemical equation are as follows:
(CH3COO)2Ca+4O2=CaO+4CO2+3H2O.And that polycondensation occurs under the catalysed oxidn of calcium oxide is anti-for the formaldehyde in waste water
Glucose should be generated, color is rufous.
It is needed in reaction process to the mixed liquor sampling in reaction kettle 5, when the formaldehydeless peculiar smell of sample, and color is rufous
When, then judge the reaction terminating in reaction kettle 5.
The dregs of 5 bottom of reaction kettle are sent into plate and frame filter press 8 and are handled by step 3)；
Start sludge pump 6 and plate and frame filter press 8, the dregs in reaction kettle 5 are sent into filters pressing in plate and frame filter press 8.Simultaneously to another
Acrylic acid wastewater and calcium oxide are added in one reaction kettle 5.
Step 4) after mixed liquor evaporative crystallization to separating, to reuse or discharge after distillation water process, to the calcium acetate of crystallization
Packaging is collected.
It is evaporated and is separated by three-level, crystallization is evaporated to mixed liquor, mixed liquor enters 1st effective evaporator by elevator pump 7
Then concentration in 15 is separated by an effect separator 16；It is entered in 2nd effect evaporator 17 and is concentrated by evaporation by pressure difference, and through two
Separator 18 is imitated to separate；It is concentrated, and is separated by triple effect separator 20, and pass through being entered in triple effect evaporator 19 by pressure difference
Discharging pump 23 is pumped into thickener 30, then obtains calcium acetate solid by centrifugal separator 29, and mother liquor returns to triple effect evaporator 19
Continue to be concentrated.
Heat source by steam as 1st effective evaporator 15, the secondary gas that 1st effective evaporator 15 steams is as 2nd effect evaporator
17 heat source heats for 2nd effect evaporator 17.Heat source of the secondary gas that 2nd effect evaporator 17 steams as triple effect evaporator 19 be
Triple effect evaporator 19 heats.The secondary gas that triple effect evaporator 19 steams enters in condenser 22, and condensed water is entered after condensation
In tank 24.
The condensed water that 1st effective evaporator 15 generates, which enters after condensation water preheater continues heating to material, to be gone out-of-bounds to handle, and two
The secondary air cooling condensate of effect evaporator 17 enters triple effect shell side, and the condensed water in triple effect shell side and condenser enters condensed water
In tank 24, it is pumped to out-of-bounds by condensate pump 25.
Calcium acetate is purified by the process of above-mentioned evaporative crystallization, content is being carried out to the calcium acetate in sample respectively
The purification of measurement, sample carries out average test three times.For the purity variation of sample after investigation purification, to raw sample and sample is purified
Product are measured, for sample 1: the content of calcium acetate is 64.14% in raw sample, and the content of calcium acetate is in sample after purification
99.12%；For sample 2: the content of calcium acetate is 60.39% in raw sample, and the content of calcium acetate is in sample after purification
99.37%；For sample 3: the content of calcium acetate is 59.47% in raw sample, and the content of calcium acetate is in sample after purification
98.43%.The average content of raw sample calcium acetate is 61%, and recklessly by purification, the average content of the calcium acetate in sample then connects
Nearly 99%, the purity of calcium acetate is promoted obvious.
The above described is only a preferred embodiment of the present invention, being not that the invention has other forms of limitations, appoint
What those skilled in the art changed or be modified as possibly also with the technology contents of the disclosure above equivalent variations etc.
Imitate embodiment.But without departing from the technical solutions of the present invention, according to the technical essence of the invention to above embodiments institute
Any simple modification, equivalent variations and the remodeling made, still fall within the protection scope of technical solution of the present invention.
Claims (9)
1. a kind of novel treatment technology of acrylic acid waste water, characterized by the following steps:
After acrylic acid wastewater is heated to 70 ~ 80 DEG C by step 1) in investment reaction kettle (5)；
Step 2 continuously adds calcium oxide into reaction kettle (5), and makes the pH 9.5 ~ 10 in reaction kettle (5)；
The dregs of reaction kettle (5) bottom are sent into processing in plate and frame filter press (8) by step 3)；
Step 4), to reuse or discharge after distillation water process, packs the calcium acetate of crystallization to separating after mixed liquor evaporative crystallization
It collects.
2. novel treatment technology of acrylic acid waste water according to claim 1, it is characterised in that: by way of aeration pair
Mixed liquor in reaction kettle described in step 2 (5) is stirred.
3. novel treatment technology of acrylic acid waste water according to claim 1 or 2, it is characterised in that: described in step 2
Reaction kettle (5) in reaction time be 0.5 ~ 1h.
4. novel treatment technology of acrylic acid waste water according to claim 1, it is characterised in that: be added into step 2
The amount of calcium oxide is that 38g is added in every liter of acrylic acid wastewater.
5. novel treatment technology of acrylic acid waste water according to claim 1, it is characterised in that: steaming described in step 4)
Hair crystallization carries out triple effect evaporation crystallization using evaporator, and evaporator is connected with forced circulation pump (21).
6. novel treatment technology of acrylic acid waste water according to claim 1, it is characterised in that: to the crystallization in step 4)
Mixed liquor afterwards successively enters back into centrifugal separator (29) separation after thickener (30), evaporates again to the mother liquor after separation
Crystallization.
7. novel treatment technology of acrylic acid waste water according to claim 1, it is characterised in that: in step 1) ~ step 3)
The reaction kettle (5) has at least two be arranged in parallel.
8. novel treatment technology of acrylic acid waste water according to claim 1, it is characterised in that: anti-described in step 2
It answers and maintains negative pressure state in kettle (5).
9. novel treatment technology of acrylic acid waste water according to claim 1, it is characterised in that: to described in step 2
Mixed liquor sampling in reaction kettle (5) then judges in reaction kettle (5) when the formaldehydeless peculiar smell of sample, and when color is rufous
Reaction terminating.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201910751168.9A CN110436690A (en) | 2019-08-15 | 2019-08-15 | A kind of novel treatment technology of acrylic acid waste water |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201910751168.9A CN110436690A (en) | 2019-08-15 | 2019-08-15 | A kind of novel treatment technology of acrylic acid waste water |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN110436690A true CN110436690A (en) | 2019-11-12 |
Family
ID=68435598
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201910751168.9A Pending CN110436690A (en) | 2019-08-15 | 2019-08-15 | A kind of novel treatment technology of acrylic acid waste water |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN110436690A (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113429048A (en) * | 2021-06-15 | 2021-09-24 | 中石化南京化工研究院有限公司 | Treatment method of acrylic acid wastewater |
| CN115209972A (en) * | 2020-02-26 | 2022-10-18 | 三菱化学株式会社 | Method for separating crystal containing water, method for producing methacrylic acid, and method for producing methacrylic acid ester |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20030143143A1 (en) * | 2002-01-30 | 2003-07-31 | Yukihiro Matsumoto | Process for treating wastes from acrylic acid and polyacrylic acid production processes |
| CN204417273U (en) * | 2014-12-31 | 2015-06-24 | 石家庄鼎威化工设备工程有限公司 | Phosphorus-containing wastewater special processor in phosphorous chemical industry production |
| CN105198118A (en) * | 2015-09-17 | 2015-12-30 | 博天环境集团股份有限公司 | Method for treating and recycling waste water containing acrylic acid and acrylate |
| CN105218338A (en) * | 2014-06-19 | 2016-01-06 | 王志龙 | A kind for the treatment of process that can produce the furfural waste-water of acetone |
-
2019
- 2019-08-15 CN CN201910751168.9A patent/CN110436690A/en active Pending
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20030143143A1 (en) * | 2002-01-30 | 2003-07-31 | Yukihiro Matsumoto | Process for treating wastes from acrylic acid and polyacrylic acid production processes |
| CN105218338A (en) * | 2014-06-19 | 2016-01-06 | 王志龙 | A kind for the treatment of process that can produce the furfural waste-water of acetone |
| CN204417273U (en) * | 2014-12-31 | 2015-06-24 | 石家庄鼎威化工设备工程有限公司 | Phosphorus-containing wastewater special processor in phosphorous chemical industry production |
| CN105198118A (en) * | 2015-09-17 | 2015-12-30 | 博天环境集团股份有限公司 | Method for treating and recycling waste water containing acrylic acid and acrylate |
Non-Patent Citations (1)
| Title |
|---|
| 洪海等: "缩合-多效蒸发处理丙烯酸废水的能耗", 《化工进展》 * |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN115209972A (en) * | 2020-02-26 | 2022-10-18 | 三菱化学株式会社 | Method for separating crystal containing water, method for producing methacrylic acid, and method for producing methacrylic acid ester |
| CN113429048A (en) * | 2021-06-15 | 2021-09-24 | 中石化南京化工研究院有限公司 | Treatment method of acrylic acid wastewater |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN104986910B (en) | Mechanical steam recompression falling film evaporation process method and system | |
| CN101481189B (en) | Integrated process of furfural production as well as wastewater, waste slag and waste gas treatment | |
| CN110436690A (en) | A kind of novel treatment technology of acrylic acid waste water | |
| CN208553176U (en) | A kind of chemical industry distilling apparatus | |
| CN105523677B (en) | A kind of desulfurization wastewater zero-discharge treatment system | |
| CN110182874A (en) | A kind of super low energy consumption flash concentration desulfurization wastewater and industrial brine waste zero emission system | |
| CN109319996A (en) | A kind of processing method of high-COD waste water with high salt | |
| CN206901972U (en) | A kind of rubbish from cooking wastewater treatment production line | |
| CN109851161A (en) | Produce the processing method of biphenyl-benzyl dichloride and the produced sewage of ortho-sulfonic acid sodium benzaldehyde | |
| CN210505926U (en) | Acrylic acid effluent disposal system | |
| CN217757171U (en) | Utilize processing system of power plant waste heat resourceful desulfurization waste water | |
| CN208883643U (en) | A kind of full factory's wastewater discharge device in coal-burning power plant | |
| CN206368049U (en) | A kind of device for handling organic brine waste | |
| CN206337130U (en) | A kind of sewage sludge processing unit | |
| CN205442935U (en) | Concentrated processing system of waste lye | |
| CN216039097U (en) | Device for treating isooctyl thioglycolate concentrated wastewater | |
| CN101862586A (en) | System for industrial waste gas treatment and salt regeneration | |
| CN213885048U (en) | Waste water recovery system of fosetyl-aluminum esterification reaction | |
| CN211688662U (en) | High COD high salt effluent disposal system | |
| CN208087250U (en) | The device that high-salt wastewater low-temperature evaporation is concentrated using hot industry waste water | |
| CN218709789U (en) | High concentration making wine waste water resourceful comprehensive treatment equipment | |
| CN217202142U (en) | Device for preventing ammonium bisulfate from crystallizing, after-gas treatment system and tail gas fermentation system | |
| CN109181792A (en) | A kind of biofuel oil process equipment | |
| CN109761431A (en) | A kind of landfill leachate treatment integrated equipment and method for treating garbage percolation liquid | |
| CN204752564U (en) | Apparatus for producing of smart dimeric acid |
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 | ||
| RJ01 | Rejection of invention patent application after publication | ||
| RJ01 | Rejection of invention patent application after publication |
Application publication date: 20191112 |